DK147291B - CONTINUOUS PROCEDURE AND PLANT FOR MANUFACTURING FEEDS FROM A ROOM MATERIAL - Google Patents
CONTINUOUS PROCEDURE AND PLANT FOR MANUFACTURING FEEDS FROM A ROOM MATERIAL Download PDFInfo
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- DK147291B DK147291B DK553580A DK553580A DK147291B DK 147291 B DK147291 B DK 147291B DK 553580 A DK553580 A DK 553580A DK 553580 A DK553580 A DK 553580A DK 147291 B DK147291 B DK 147291B
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- pulp
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23N—MACHINES OR APPARATUS FOR TREATING HARVESTED FRUIT, VEGETABLES OR FLOWER BULBS IN BULK, NOT OTHERWISE PROVIDED FOR; PEELING VEGETABLES OR FRUIT IN BULK; APPARATUS FOR PREPARING ANIMAL FEEDING- STUFFS
- A23N17/00—Apparatus specially adapted for preparing animal feeding-stuffs
- A23N17/004—Apparatus specially adapted for preparing animal feeding-stuffs for treating by application of heat, e.g. by means of potato cookers
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K10/00—Animal feeding-stuffs
- A23K10/30—Animal feeding-stuffs from material of plant origin, e.g. roots, seeds or hay; from material of fungal origin, e.g. mushrooms
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
- Y02P60/87—Re-use of by-products of food processing for fodder production
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- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Polymers & Plastics (AREA)
- Food Science & Technology (AREA)
- Mycology (AREA)
- Health & Medical Sciences (AREA)
- Physiology (AREA)
- Animal Husbandry (AREA)
- Zoology (AREA)
- Molecular Biology (AREA)
- Botany (AREA)
- Biotechnology (AREA)
- Fodder In General (AREA)
- Apparatuses For Bulk Treatment Of Fruits And Vegetables And Apparatuses For Preparing Feeds (AREA)
Description
147291147291
Opfindelsen angår en fremgangsmåde til fremstilling af foder ud fra et roemateriale.The invention relates to a method of preparing feed from a beet material.
Ved fremstillingen af sukker ud fra sukkerroer underkastes roerne, som kommer fra marken, først en vaskning til fjernelse af 5 urenheder fra roernes overflader, hvorpå de omdannes til sukkerroesnitter.In the production of sugar from beet, the beets coming from the field are first subjected to a wash to remove 5 impurities from the beets' surfaces and then be converted into sugar beets.
Ved en i patentansøgning nr. 5580/78 beskrevet fremgangsmåde foretages en skrælning af de vaskede roer, inden de omdannes til sukkerroesnitter, idet man herved kan opnå et større sukkerudbyt-10 te end ved den ovenfor omtalte traditionelle vaskemetode. Sukkerroesnitterne ekstraheres derpå med vand til dannelse af en sukkersaft, som derpå oparbejdes, sædvanligvis til krystallinsk sukker. Ekstraktionen kan eksempelvis foretages i et ekstraktionsapparat bestående af et skråtstillet trug med to eller flere roterbare transportsnegle, der 15 fra trugets nedre indføringsende fører roesnitterne mod en øvre udtagsende i modstrøm med vand, der indføres ved den øvre ende, og som beriget med sukker udtages ved den nedre ende i form af sukkersaft.In a process described in Patent Application No. 5580/78, the washed beets are peeled before being converted to sugar beets, thereby obtaining a greater sugar yield than the traditional washing method mentioned above. The sugar beets are then extracted with water to form a sugar juice which is then worked up, usually into crystalline sugar. The extraction can be carried out, for example, in an extraction apparatus consisting of an inclined trough with two or more rotatable transport augers which guide from the lower feed end of the trough towards the upper outlet end countercurrent with water introduced at the upper end and which is enriched with sugar at the lower end in the form of sugar juice.
De ekstraherede roesnitter, der betegnes pulp, og som er 20 den rest, der bliver tilbage efter, at hovedparten af opløselige sukkerstoffer og salte er blevet fjernet ved ekstraktionen, underkastes normalt en presning, hvorved materialets tørstofindhold forøges til mellem 11 og 21%, afhængig af den type presse, der anvendes.The pulp extracts called pulp, which is the residue remaining after the majority of soluble sugars and salts have been removed by extraction, are usually subjected to a pressing, increasing the dry matter content of the material to between 11 and 21%, depending of the type of press used.
Ved kemikalietilsætning, f.eks. tilsætning af AI^SO^)^ kan 25 tørstofindholdet forøges med yderligere 1-2%.For chemical additives, e.g. addition of Al 2 SO 2, the solids content can be increased by a further 1-2%.
Den pressede pulp kan anvendes til kreaturfoder, enten uden yderligere behandling eller efter ensilering.The pressed pulp can be used for livestock feed, either without further treatment or after silage.
Som følge af den pressede pulps relativt store vandindhold er det ikke hensigtsmæssigt at transportere den over større afstande, 30 og i så fald foretages normalt en tørring af pulpen. Det herved dannede produkt findes i handelen under betegnelsen "Pulpetter ".Due to the relatively high water content of the pressed pulp, it is not convenient to transport it over larger distances, and in this case drying of the pulp is usually carried out. The resulting product is commercially available under the designation "Pulpets".
Det tørrede produkt kan eventuelt tilsættes melasse, og et produkt af sidstnævnte art findes i handelen under betegnelsen "Ko- ® setter ". Begge disse produkter er velegnede som kreaturfoder.The dried product may optionally be added to molasses and a product of the latter type is commercially available under the designation "Composer". Both of these products are suitable as livestock feed.
35 Såvel presningen af pulpen som tørringen af den pressede pulp er stærkt energikrævende, og med de stadigt stigende energipriser er der et stadigt voksende behov for ud fra roer at fremstille et relativt vandfattigt foderstof ved en mindre energikrævende metode end de ovenfor omtalte kendte metoder.35 Both the pressing of the pulp and the drying of the pressed pulp are highly energy intensive, and with the ever increasing energy prices there is an ever growing need to produce, from beets, a relatively water-poor feed by a less energy intensive method than the above-mentioned methods.
2 14729 12 14729 1
Dette opnås ved fremgangsmåden ifølge opfindelsen, hvilken fremgangsmåde er ejendommelig ved, at roematerialet under opvarmning til en temperatur på 104-165°C og ved et tryk på 0-7 ato underkastes en syrehydrolyse, at det således behandlede produkt skilles i en 5 væskefraktion, der derpå neutraliseres og inddampes, og en faststoffraktion.This is achieved by the process according to the invention, which is characterized in that the raw material is heated to a temperature of 104-165 ° C and at a pressure of 0-7 ato, an acid hydrolysis, which separates the thus treated product into a liquid fraction. then neutralized and evaporated, and a solid fraction.
Opfindelsen er baseret pi den erkendelse, at roematerialer, såsom roepulp og roeskræl, er opbygget af en række polymerer, såsom pektin og pentosaner, som under tryk og forhøjet temperatur 10 kan hydrolyseres med syre under dannelse af et væskeformigt produkt, der let inddampes til dannelse af et melasselignende produkt med et stort tørstofindhold, f.eks. på ca. 60%. Således har det vist sig, at der ved fremgangsmåden ifølge opfindelsen kræves ca. 20% mindre energi til fremstilling af et hydrolyseprodukt med tilnærmelses-15 vis samme foderværdi som for tørrede ekstraherede snitter end ved den kendte fremgangsmåde til fremstilling af sådanne snitter.The invention is based on the recognition that beet materials, such as beet pulp and beet peel, are made up of a number of polymers such as pectin and pentosans which can be hydrolyzed with acid under pressure and elevated temperature to form a liquid product which is readily evaporated to form of a molasses-like product with a high solids content, e.g. of approx. 60%. Thus, it has been found that the method according to the invention requires approx. 20% less energy to produce a hydrolysis product having approximately the same feed value as for dried extracted cuts than in the known process for producing such cuts.
Det har ligeledes vist sig, at faststoffraktionen efter at være blevet befriet for hydrolyserbare bestanddele let kan presses til opnåelse af et tørstofindhold på over 30%, d.v.s. væsentligt over de 20 22-23%, som maksimalt kan opnås ved den kendte fremgangsmåde med kemikalietilsætning.It has also been found that, after being liberated from hydrolyzable constituents, the solid fraction can easily be pressed to obtain a dry matter content of more than 30%, i.e. substantially above the 20 to 22%, which can be maximally obtained by the known method of chemical addition.
Det skal dog bemærkes, at faststoffraktionen uden presning også kan anvendes til fremstilling af glukose ved hydrolyse, idet udgangsmaterialets celluioseindhold efter fjernelsen af de hydrolyserbare 25 stoffer er blevet væsentligt forøget.However, it should be noted that the solid fraction without compression can also be used to produce glucose by hydrolysis, since the cellulosic content of the starting material after the removal of the hydrolysable substances has been substantially increased.
Under hydrolysetrinnet opvarmes udgangsmaterialet til en temperatur på 100-165°C, fortrinsvis ca. 130°C, og opvarmningen foretages særligt hensigtsmæssigt ved direkte dampindblæsning.During the hydrolysis step, the starting material is heated to a temperature of 100-165 ° C, preferably approx. 130 ° C, and the heating is particularly convenient by direct steam supply.
Trykket under hydrolysetrinnet er ifølge opfindelsen mellem 30 0 og 7 ato og især mellem 2 og 4 ato.According to the invention, the pressure during the hydrolysis step is between 30 and 7 ato and especially between 2 and 4 ato.
Den anvendte syre er fortrinsvis en stærkt uorganisk syre, såsom svovlsyre, phosphorsyre og saltsyre. Det foretrækkes at imprægnere udgangsmaterialet med syre før opvarmningen under tryk.The acid used is preferably a highly inorganic acid such as sulfuric acid, phosphoric acid and hydrochloric acid. It is preferred to impregnate the starting material with acid before heating under pressure.
Opfindelsen angår også et anlæg til udøvelse af den ovenfor 35 beskrevne fremgangsmåde. Dette anlæg er ejendommeligt ved, at det omfatter et blandeapparat til blanding af roemateriale eller findelt grøn afgrøde med syre, en med blandeapparatet forbundet hydrolysebeholder, hvori der er anbragt en konus på det sted, hvor blandingen af roemateriale eller findelt grøn afgrøde og syre under tryk indføres 3 147291 i beholderen, opvarmningsorganer samt en ventil til udtagning af behandlet materiale, et filter til opdeling af det ved hydrolysen dannede produkt i en væskefraktion og en faststoffraktion samt beholdere til neutralisering og inddampning af væskefraktionen.The invention also relates to a plant for carrying out the method described above. This plant is characterized in that it comprises a mixer for mixing beet material or finely divided green crop with acid, a hydrolysis container connected to the mixer, in which a cone is placed at the place where the mixture of beet material or finely divided green crop and acid is pressurized. No. 3,147,291 is introduced into the vessel, heating means and a valve for extracting treated material, a filter for dividing the product formed by the hydrolysis into a liquid fraction and a solid fraction, and vessels for neutralizing and evaporating the liquid fraction.
5 Anlægget ifølge opfindelsen kan endvidere omfatte en af spændingsbeholder anbragt mellem hydrolysebeholderen og filteret.The plant according to the invention may further comprise one of a voltage container disposed between the hydrolysis vessel and the filter.
Blandeapparatet består fortrinsvis af et kar, hvori der er monteret to parallelle roterbare aksler forsynet med propel-lignende skovle, der er således udformede, at der dels kan foretages en sam-10 menblanding af udgangsmateriale og syre og dels kan iværksættes en fremføring af blandingen.Preferably, the mixer consists of a vessel in which are mounted two parallel rotatable shafts provided with propeller-like blades, which are designed so that a mixing of the starting material and acid can be made and a feeding of the mixture can be initiated.
Opfindelsen skal herefter beskrives nærmere under henvisning til tegningen, der i form af en principskitse viser et anlæg til udøvelse af fremgangsmåden ifølge opfindelsen.The invention will then be described in more detail with reference to the drawing, which shows in the form of a principle sketch an installation for carrying out the method according to the invention.
15 På tegningen betegner 1 et blandeapparat omfattende et kar, hvori der er monteret to vandretliggende roterbare aksler forsynet med skovle, der tjener dels til at blande roepulp med syre, såsom svovlsyre, phosphorsyre og saltsyre, og dels til at føre blandingen frem gennem karret. Ved hjælp af tilledningsorganer 2 og 3 tilledes 20 roepulp med et tørstofindhold på f.eks. 12-16% henholdsvis varm, fortyndet svovlsyre til karrets ene ende, og det imprægnerede materiale føres med en snegl 4 ind i en hydrolysebeholder 5. Materialet skrues ind i beholderen mod en konus 6, hvis modtryk er fastsat til et tryk, der er lidt højere end overtrykket i hydrolysebeholderen. Hydrolysen 25 gennemføres ved et overtryk på op til 7 ato, og med en hydrolysetid på 10 min. når trykket er højt og med længere hydrolysetid ved lavere tryk. Opvarmning af massen gennemføres ved indblæsning af damp gennem damptilførselsrør 7.In the drawing, 1 denotes a mixer comprising a vessel in which are mounted two horizontal rotatable shafts provided with blades which serve partly to mix beet pulp with acid such as sulfuric acid, phosphoric acid and hydrochloric acid and partly to advance the mixture through the vessel. By means of supply means 2 and 3, 20 beet pulp having a dry matter content of e.g. 12-16% respectively of hot, dilute sulfuric acid to one end of the vessel, and the impregnated material is introduced with a auger 4 into a hydrolysis vessel 5. The material is screwed into the container against a cone 6, the back pressure of which is set at a slight pressure. higher than the overpressure in the hydrolysis vessel. Hydrolysis 25 is carried out at an excess pressure of up to 7 ato and with a hydrolysis time of 10 min. when the pressure is high and with longer hydrolysis time at lower pressure. Heating of the pulp is carried out by blowing steam through steam supply pipe 7.
Gennem en passende ventil 8, f.eks. en stor roterende kug-30 leventil med hulrum, der er kendt fra celluloseindustrien, ledes den hydrolyserede pulp til en afspændingsbeholder 9, hvor massen afspændes til atmosfæretryk under frigørelse af damp, der udtages gennem et rør 10, og som eventuelt kan udnyttes andetsteds.Through an appropriate valve 8, e.g. a large rotary ball valve with cavities known from the cellulose industry, the hydrolyzed pulp is fed to a relaxation vessel 9, where the mass is relaxed to atmospheric pressure, releasing steam discharged through a tube 10 and which may be utilized elsewhere.
Fra afspændingsbeholderen 9 pumpes den afspændte hydro-35 lyserede pulp gennem en ledning 11 til et filter 12, der f.eks. kan være et båndfilter, hvor den ikke-hydrolyserede masse skilles fra den hydrolyserede del af pulpen. Det væskeformige hydrolyseprodukt føres gennem en ledning 13 til en neutralisationsbeholder 14, hvor der tilsættes base, f.eks. CaCOg, kalkmælk, NagCOg eller en NHg-opløs- 4 U7Z9i ning gennem en ledning 15. Efter neutralisering til pH ca. 6 føres blandingen gennem en ledning 16 til et filter 17, hvor der sker en frafiltrering af faststof, og hvorfra det neutraliserede hydrolyseprodukt gennem en ledning 18 pumpes til et flertrinsinddampningsanlæg 5 19, hvor ekstrakten inddampes til et tørstofindhold pi ca. 60%. Det herved opnåede væskeformige produkt, som udtages gennem en ledning 20, er velegnet til kreaturfoder til erstatning af melasse fra roesukker- eller rørsukkerproduktionen.From the relaxation vessel 9, the relaxed hydrolysed pulp is pumped through a conduit 11 to a filter 12 which e.g. may be a band filter where the non-hydrolyzed mass is separated from the hydrolyzed portion of the pulp. The liquid hydrolysis product is passed through a conduit 13 to a neutralization vessel 14 to which base is added, e.g. CaCOg, lime milk, NagCOg or an NHg solution through a conduit 15. After neutralization to pH ca. 6, the mixture is passed through a conduit 16 to a filter 17 where a solid filtration is effected and from which the neutralized hydrolysis product is pumped through a conduit 18 to a multi-stage evaporation plant 5 19 where the extract is evaporated to a dry matter content of approx. 60%. The liquid product thus obtained, which is withdrawn through a conduit 20, is suitable for livestock feed to replace molasses from beet sugar or cane sugar production.
Presset roepulp fremstillet som ovenfor beskrevet indeholder 10 normalt over 30% organisk uopløst tørstof og kan anvendes i en af to følgende processer. For det første kan den ekstraherede pulp neutraliseres og tørres ligesom ubehandlet pulp men under anvendelse af mindre energi pr. kg tørret produkt pi grund af det forøgede tørstofindhold. For det andet kan den pressede pulp underkastes en 15 hydrolyse ved høj temperatur, d.v.s. mellem 200 og 250°C, hvorved pulpens cellulose vil blive omdannet til glukose under indvirkning af den i pulpen tilstedeværende syre. Den herved dannede glukose kan ved gæring omdannes til ethanol, som ved destillation kan oparbejdes til ethanol.Pressed beet pulp prepared as described above usually contains more than 30% organic undissolved solids and can be used in one of two following processes. First, the extracted pulp can be neutralized and dried just like untreated pulp but using less energy per day. kg of dried product due to the increased dry matter content. Second, the pressed pulp may be subjected to high temperature hydrolysis, i.e. between 200 and 250 ° C, whereby the pulp's cellulose will be converted to glucose under the action of the acid present in the pulp. The resulting glucose can be converted to ethanol by fermentation, which can be processed into ethanol by distillation.
20 Opfindelsen skal herefter beskrives under henvisning til følgende eksempel:The invention will now be described with reference to the following example:
EKSEMPELEXAMPLE
Roepulp med et indhold af organisk tørstof på 15% og en 25 temperatur pi 65°C føres til en blandebeholder i en mængde på 80 kg pr. time. Der tilsættes samtidigt pr. time 3,55 kg svovlsyre med en koncentration på 25% (vægt/vægt) og en temperatur på 90°C. Efter grundig sammenblanding i blandebeholderen føres blandingen til en velisoleret hydrolysebeholder, hvor blandingen med damp opvarmes til 30 131°C, og den holdes opvarmet ved denne temperatur i 30 min. Fra hydrolysebeholderen ledes blandingen kontinuert til en afspændingsbeholder, hvor materialet trylaflastes, hvorved der sker et temperaturfald til ca. 100°C. Den hydrolyserede masse på ca. 92 kg pr. time føres til et båndfilter, hvor et væskeformigt hydrolyseprodukt fraskil-35 les. Fra 92 kg opnås 17,6 kg af en faststoffraktion med et indhold af organisk tørstof på ca. 32%. Det væskeformige hydrolyseprodukt sammen med vaskevand fra vaskningen af pulpen beløber sig til 90 kg, og blandingen indeholder 6,3 kg organisk materiale i opløsning.Beet pulp with a content of organic dry matter of 15% and a temperature of 65 ° C is fed to a mixing container in an amount of 80 kg per liter. hour. At the same time, hourly 3.55 kg of sulfuric acid with a concentration of 25% (w / w) and a temperature of 90 ° C. After thorough mixing in the mixing vessel, the mixture is passed to a well insulated hydrolysis vessel, where the mixture with steam is heated to 30 131 ° C and kept heated at this temperature for 30 minutes. From the hydrolysis vessel, the mixture is continuously fed to a relaxation vessel where the material is unloaded, thereby causing a temperature drop to approx. 100 ° C. The hydrolyzed mass of approx. 92 kg per hour is passed to a belt filter where a liquid hydrolysis product is separated. From 92 kg, 17.6 kg of a solid fraction with an organic dry matter content of approx. 32%. The liquid hydrolysis product together with wash water from the washing of the pulp amounts to 90 kg, and the mixture contains 6.3 kg of organic matter in solution.
Denne væske neutraliseres, filtreres og inddampes. Det dannede væ- 5 147291 skeformige produkt har typisk følgende data: Tørstof, % 57,6This liquid is neutralized, filtered and evaporated. The liquid product formed typically has the following data: Solids,% 57.6
Aske ved 550°C, % 13,0 5 Aske ved 1050°C, % 11,8Ash at 550 ° C,% 13.0 5 Ash at 1050 ° C,% 11.8
Reducerende sukkerarter (Mtiller) %/l00RT 20,5Reducing Sugars (Mtiller)% / 100RT 20.5
Uronsyrer og pentoser bestemt ved omdannelse til furfural 10 %/l00RT ca. 50Uronic acids and pentoses determined by conversion to furfural 10% / 100RT approx. 50
Hexoser (enzymatisk bestemt) %/100RT ca. 2,5Hexoses (enzymatically determined)% / 100RT approx. 2.5
Eddikesyre (enzymatisk bestemt) %/100RT 0,8 15 Myresyre (enzymatisk bestemt) I/100RT 0,03.Acetic acid (enzymatically determined)% / 100RT 0.8 Formic acid (enzymatically determined) I / 100RT 0.03.
Priority Applications (15)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DK553580A DK147291C (en) | 1980-12-23 | 1980-12-23 | CONTINUOUS PROCEDURE AND PLANT FOR MANUFACTURING FEEDS FROM A ROOM MATERIAL |
CH814281A CH646584A5 (en) | 1980-12-23 | 1981-12-21 | METHOD AND DEVICE FOR PRODUCING AN ANIMAL FEED FROM A BEE MATERIAL. |
SE8107672A SE8107672L (en) | 1980-12-23 | 1981-12-21 | PROCEDURE FOR PREPARING ANIMALIC FEED FROM BET MATERIAL AND APPARATUS FOR CARRYING OUT THE PROCEDURE |
JP56206808A JPS57194754A (en) | 1980-12-23 | 1981-12-21 | Method and apparatus for producing animal feedstuff |
DE19813150592 DE3150592A1 (en) | 1980-12-23 | 1981-12-21 | METHOD AND DEVICE FOR PRODUCING AN ANIMAL FEED FROM BEET |
FI814139A FI814139L (en) | 1980-12-23 | 1981-12-22 | REFERENCE FITTING FOR FRAMING PROCESSING OF ROTARY PRODUCTS |
IT8125768A IT1211152B (en) | 1980-12-23 | 1981-12-22 | METHOD AND APPARATUS TO PREPARE ANIMAL FEED FROM BEETS. |
YU3056/81A YU42028B (en) | 1980-12-23 | 1981-12-22 | Method and device for storing fodder of sugar-beet origin |
AT0552381A AT375246B (en) | 1980-12-23 | 1981-12-22 | METHOD AND DEVICE FOR PRODUCING ANIMAL FEED FROM BEET MATERIAL |
FR8123990A FR2496410B1 (en) | 1980-12-23 | 1981-12-22 | METHOD AND DEVICE FOR PRODUCING FEED FOR ANIMAL FROM BEET MATERIAL |
PL1981234377A PL130574B1 (en) | 1980-12-23 | 1981-12-22 | Method of obtaining animal feed from a material of beet origin |
NL8105766A NL8105766A (en) | 1980-12-23 | 1981-12-22 | METHOD AND APPARATUS FOR MAKING ANIMAL FEED FROM BEET MATERIAL |
ES508246A ES508246A0 (en) | 1980-12-23 | 1981-12-22 | "A METHOD OF MANUFACTURING A FEED FROM BEET MATERIAL". |
BE0/206906A BE891582A (en) | 1980-12-23 | 1981-12-22 | PROCESS AND APPARATUS FOR MANUFACTURING ANIMAL FEED FROM BEETS |
GB8138680A GB2089640B (en) | 1980-12-23 | 1981-12-23 | Method of and apparatus for making an animal feed from a beet material |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DK553580A DK147291C (en) | 1980-12-23 | 1980-12-23 | CONTINUOUS PROCEDURE AND PLANT FOR MANUFACTURING FEEDS FROM A ROOM MATERIAL |
DK553580 | 1980-12-23 |
Publications (3)
Publication Number | Publication Date |
---|---|
DK553580A DK553580A (en) | 1982-06-24 |
DK147291B true DK147291B (en) | 1984-06-12 |
DK147291C DK147291C (en) | 1984-12-24 |
Family
ID=8143277
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DK553580A DK147291C (en) | 1980-12-23 | 1980-12-23 | CONTINUOUS PROCEDURE AND PLANT FOR MANUFACTURING FEEDS FROM A ROOM MATERIAL |
Country Status (15)
Country | Link |
---|---|
JP (1) | JPS57194754A (en) |
AT (1) | AT375246B (en) |
BE (1) | BE891582A (en) |
CH (1) | CH646584A5 (en) |
DE (1) | DE3150592A1 (en) |
DK (1) | DK147291C (en) |
ES (1) | ES508246A0 (en) |
FI (1) | FI814139L (en) |
FR (1) | FR2496410B1 (en) |
GB (1) | GB2089640B (en) |
IT (1) | IT1211152B (en) |
NL (1) | NL8105766A (en) |
PL (1) | PL130574B1 (en) |
SE (1) | SE8107672L (en) |
YU (1) | YU42028B (en) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA1324022C (en) * | 1987-08-07 | 1993-11-09 | Hiroshi Yamazaki | Process for preparing flour from jerusalem artichoke tubers |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
IT1095442B (en) * | 1977-03-08 | 1985-08-10 | Process Engineering Co | PROCEDURE FOR PRODUCING A MIXTURE OF FEED |
IT1096191B (en) * | 1978-05-02 | 1985-08-17 | Ciba Geigy Spa | CONCENTRATED PROTEIN FEED AND RELATED MANUFACTURING PROCEDURE |
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1980
- 1980-12-23 DK DK553580A patent/DK147291C/en active
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1981
- 1981-12-21 CH CH814281A patent/CH646584A5/en not_active IP Right Cessation
- 1981-12-21 DE DE19813150592 patent/DE3150592A1/en not_active Withdrawn
- 1981-12-21 SE SE8107672A patent/SE8107672L/en not_active Application Discontinuation
- 1981-12-21 JP JP56206808A patent/JPS57194754A/en active Pending
- 1981-12-22 BE BE0/206906A patent/BE891582A/en not_active IP Right Cessation
- 1981-12-22 IT IT8125768A patent/IT1211152B/en active
- 1981-12-22 NL NL8105766A patent/NL8105766A/en not_active Application Discontinuation
- 1981-12-22 PL PL1981234377A patent/PL130574B1/en unknown
- 1981-12-22 FR FR8123990A patent/FR2496410B1/en not_active Expired
- 1981-12-22 FI FI814139A patent/FI814139L/en not_active Application Discontinuation
- 1981-12-22 YU YU3056/81A patent/YU42028B/en unknown
- 1981-12-22 AT AT0552381A patent/AT375246B/en not_active IP Right Cessation
- 1981-12-22 ES ES508246A patent/ES508246A0/en active Granted
- 1981-12-23 GB GB8138680A patent/GB2089640B/en not_active Expired
Also Published As
Publication number | Publication date |
---|---|
AT375246B (en) | 1984-07-10 |
FR2496410B1 (en) | 1985-12-13 |
FI814139L (en) | 1982-06-24 |
DK553580A (en) | 1982-06-24 |
IT1211152B (en) | 1989-09-29 |
NL8105766A (en) | 1982-07-16 |
ES8304769A1 (en) | 1983-03-16 |
CH646584A5 (en) | 1984-12-14 |
GB2089640B (en) | 1984-03-21 |
DE3150592A1 (en) | 1982-08-26 |
IT8125768A0 (en) | 1981-12-22 |
YU42028B (en) | 1988-04-30 |
DK147291C (en) | 1984-12-24 |
PL234377A1 (en) | 1982-08-16 |
BE891582A (en) | 1982-04-16 |
YU305681A (en) | 1983-09-30 |
ES508246A0 (en) | 1983-03-16 |
ATA552381A (en) | 1983-12-15 |
JPS57194754A (en) | 1982-11-30 |
PL130574B1 (en) | 1984-08-31 |
FR2496410A1 (en) | 1982-06-25 |
SE8107672L (en) | 1982-06-24 |
GB2089640A (en) | 1982-06-30 |
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