CA1043097A - Method and apparatus for drying stillage - Google Patents
Method and apparatus for drying stillageInfo
- Publication number
- CA1043097A CA1043097A CA226,532A CA226532A CA1043097A CA 1043097 A CA1043097 A CA 1043097A CA 226532 A CA226532 A CA 226532A CA 1043097 A CA1043097 A CA 1043097A
- Authority
- CA
- Canada
- Prior art keywords
- stillage
- gas
- moisture
- conduit
- introducing
- 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
Links
- 238000001035 drying Methods 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title claims description 12
- 239000000463 material Substances 0.000 claims abstract description 32
- 235000019645 odor Nutrition 0.000 claims abstract description 5
- 239000000779 smoke Substances 0.000 claims abstract description 5
- 235000015097 nutrients Nutrition 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 16
- 239000002245 particle Substances 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 5
- 230000005012 migration Effects 0.000 claims description 3
- 238000013508 migration Methods 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims 2
- 239000013618 particulate matter Substances 0.000 claims 2
- 238000005086 pumping Methods 0.000 claims 2
- 230000003134 recirculating effect Effects 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract 1
- 230000008569 process Effects 0.000 description 6
- 238000002156 mixing Methods 0.000 description 4
- 239000006188 syrup Substances 0.000 description 4
- 235000020357 syrup Nutrition 0.000 description 4
- 239000006185 dispersion Substances 0.000 description 2
- 238000010981 drying operation Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000011236 particulate material Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000011343 solid material Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000011067 equilibration Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000000050 nutritive effect Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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
- F26B17/102—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 material recirculation, classifying or disintegrating means
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K30/00—Processes specially adapted for preservation of materials in order to produce animal feeding-stuffs
- A23K30/20—Dehydration
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Polymers & Plastics (AREA)
- Microbiology (AREA)
- Animal Husbandry (AREA)
- Zoology (AREA)
- Food Science & Technology (AREA)
- Drying Of Solid Materials (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
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°F to about 425°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) nut-rient food substance without emitting significant amounts of smoke or odors.
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°F to about 425°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) nut-rient food substance without emitting significant amounts of smoke or odors.
Description
BACKGROUND OF THE INVENTION
Spent stillage lS the grain slurry remaining aftercompletion of the fermentation and distillation processes in the production of distilled liquors. Stillage has for years been -treated to produce a conglomerate of particulate material suitable for animal consumption.
Spent stillage is initially a slurry consisting of over 90~ water which is first mechanically treated to separate the liquid from the solid materials by mechanical 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 temp-eratures and material circulation techniyues which often caused the emission of substantiaI 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 sub-stantially 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-moviny air column heated to a temperature in the range of about 325F to about 425F, is 3~
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 T~IE DRAWI~GS
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 EM DIMENT
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 peri-pheries 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 150F. 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 ~ed further in subsequent conveyors 22 or mixer~ 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.
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 r 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 con-tent 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, pro-vides 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 out-side 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 removal 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 or gases can be used.
Spent stillage lS the grain slurry remaining aftercompletion of the fermentation and distillation processes in the production of distilled liquors. Stillage has for years been -treated to produce a conglomerate of particulate material suitable for animal consumption.
Spent stillage is initially a slurry consisting of over 90~ water which is first mechanically treated to separate the liquid from the solid materials by mechanical 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 temp-eratures and material circulation techniyues which often caused the emission of substantiaI 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 sub-stantially 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-moviny air column heated to a temperature in the range of about 325F to about 425F, is 3~
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 T~IE DRAWI~GS
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 EM DIMENT
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 peri-pheries 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 150F. 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 ~ed further in subsequent conveyors 22 or mixer~ 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.
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 r 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 con-tent 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, pro-vides 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 out-side 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 removal 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 or gases can be used.
Claims (6)
1. A method of drying moist stillage material composed of moisture and moist particles having moisture pervaded through-out the particles comprising (a) maintaining a rapidly-moving gas stream heated to a temperature sufficient to volatize moisture on and at the surface area of the particulate matter mixed therewith;
(b) continuously introducing material into 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;
(d) 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 back into the 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.
(b) continuously introducing material into 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;
(d) 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 back into the 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 425°F to 150°F.
3. The method of claim 1 in which the gas is air.
4. The method of claim 1 in which the gas is super-heated 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) stillage introducing means for introducing the stillage into the conduit as gas passes through the conduit;
(d) heating means for heating the gas prior to its entering the conduit;
(e) 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.
(b) gas pumping means for pumping a gas at high speed through the conduit;
(c) stillage introducing means for introducing the stillage into the conduit as gas passes through the conduit;
(d) heating means for heating the gas prior to its entering the conduit;
(e) 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.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US469790A US3925904A (en) | 1974-05-14 | 1974-05-14 | Method and apparatus for drying stillage |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1043097A true CA1043097A (en) | 1978-11-28 |
Family
ID=23865068
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA226,532A Expired CA1043097A (en) | 1974-05-14 | 1975-05-08 | Method and apparatus for drying stillage |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US3925904A (en) |
| CA (1) | CA1043097A (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| YU211189A (en) * | 1988-11-03 | 1992-05-28 | Akt Consultants | Device and a process for drying and grinding |
| US7296129B2 (en) | 2004-07-30 | 2007-11-13 | International Business Machines Corporation | System, method and storage medium for providing a serialized memory interface with a bus repeater |
| EP1955599A1 (en) * | 2007-02-09 | 2008-08-13 | Braunschweigische Maschinenbauanstalt AG | Method and device for drying by-products |
| US9254449B2 (en) | 2011-07-28 | 2016-02-09 | Greenfield Specialty Alcohols Inc. | Solid and liquid separation process |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2345238A (en) * | 1938-07-26 | 1944-03-28 | Chemical Foundation Inc | Treatment of distillery residues |
| US2393766A (en) * | 1942-11-28 | 1946-01-29 | Comb Eng Co Inc | Drying apparatus |
| SE341909B (en) * | 1971-04-06 | 1972-01-17 | Karlstad Mekaniska Ab |
-
1974
- 1974-05-14 US US469790A patent/US3925904A/en not_active Expired - Lifetime
-
1975
- 1975-05-08 CA CA226,532A patent/CA1043097A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| US3925904A (en) | 1975-12-16 |
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