EP0120984A1 - Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse - Google Patents

Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse Download PDF

Info

Publication number
EP0120984A1
EP0120984A1 EP83103235A EP83103235A EP0120984A1 EP 0120984 A1 EP0120984 A1 EP 0120984A1 EP 83103235 A EP83103235 A EP 83103235A EP 83103235 A EP83103235 A EP 83103235A EP 0120984 A1 EP0120984 A1 EP 0120984A1
Authority
EP
European Patent Office
Prior art keywords
steam
hexane
actual
gasoline
solvent
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.)
Withdrawn
Application number
EP83103235A
Other languages
German (de)
English (en)
Inventor
Heinz Schumacher
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to EP83103235A priority Critical patent/EP0120984A1/fr
Publication of EP0120984A1 publication Critical patent/EP0120984A1/fr
Priority to US06/769,766 priority patent/US4622760A/en
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/001—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement the material moving down superimposed floors
    • F26B17/003—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement the material moving down superimposed floors with fixed floors provided with scrapers
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/10—Production of fats or fatty oils from raw materials by extracting
    • C11B1/108—Production of fats or fatty oils from raw materials by extracting after-treatment, e.g. of miscellae

Definitions

  • This residue which for example can still have up to 0.5% by weight of residual oil and up to 30% by weight of solvent, is after the separation from the Miscella by pressing or sieving in a predominantly continuous process using steam or water Fluids containing water vapor are treated and freed from the solvent to an optimal degree.
  • the proportion of solvent in the solvent-wet residue, the scrap naturally depends on the type of solvent or extracting agent, the raw material, the extraction process with its special process parameters, etc. and can fluctuate within certain limits. However, it is not only necessary for process economy reasons to drive the solvent out of the scrap and to recover it optimally, the scrap itself, which is mainly processed for feed and food, can only be used if it is used for further processing practically solvent-free.
  • the relevant industry predominantly uses aliphatic hydrocarbons, in particular technical hexane (n-hexane) as an extractant for oil crops and oil seeds. Depending on the structure, this hexane has a boiling range of approximately 63 to 70 ° C.
  • US Pat. No. 2,585,793 describes a toaster developed in particular for extracted soy flakes, in which in the upper region of a multi-day system, the de-gasification takes place by feeding in direct water vapor.
  • the uppermost of a multi-floor system is provided with steam outlet openings, so that the goods placed on the top floor are directly exposed to the steam.
  • the direct steam is introduced via the bottom container bottom, which is designed as a perforated or sieve bottom, and is guided towards the goods from bottom to top over the entire container height via likewise perforated floor bases.
  • the double floor of the top floor - and all other floors - contains a lock, through which the de-petrified shot falls continuously into the floor below, the so-called drying.
  • the speed of the lock (s) enables a certain material level to be set on the individual floors.
  • the dryer floor which is connected after the gasoline removal, is also delimited at the bottom by a perforated floor designed as a double floor, through which hot air is introduced for drying the condensate-containing meal and $ accordingly is shared.
  • the air is pressed into the shot through the perforated bottom by a fan and - loaded with moisture - discharged to the side above the shot bed.
  • the grist is cooled on the lower level, with a fan drawing cold air through the grit through a simple perforated floor.
  • this "toaster dryer cooler”, or TTK is a single device, but in terms of process technology it is a matter of intermeshing. the result of three working stages, because a different treatment of the shot takes place on each floor.
  • the TTK is of particular economic advantage due to its low investment costs, since three otherwise independent processes can be carried out with independent systems in a single container.
  • the vertical sequence of work processes means that conveyor elements such as conveyors, elevators, screw conveyors, etc. are saved.
  • the consumption of energy is also significantly lower than with a system consisting of three separately operating systems, e.g. an isolated varnish, a connected fluid bed dryer and a tube cooler or the like.
  • TTKs such as those e.g. are used in the de-benzinating of petrol-soybean meal
  • the consumption of electrical energy is higher than in known classic de-benzinating plants with cascade coolers, tube bundle dryers, etc.
  • the consumption of electrical energy at the TTK is essentially determined by the power of the main shaft, on which stirring arms are attached for each floor of the multi-day system, which move through the shot in order to convey it evenly over the floors and the formation of to prevent the inflowing gases (water vapor, hot air, cooling air) from forming channels.
  • the steam is used as direct steam at the lowest point, i.e. introduced below the bottom floor of a multi-day system and distributed over perforations.
  • This device is also provided with a central shaft, by means of which the stirring arms are moved little above each perforated floor.
  • the individual floors can in turn be designed as raised floors, which have a large number of specially designed perforations through which a so-called spray effect is achieved. This makes it possible to guide the steam blown into the lowest area of the vertical device from floor to floor on its way upwards without hindrance and thereby practically preclude the formation of steam channels.
  • this device has a solvent (hexane) / water vapor vapor temperature of 66 to 68 ° C allows without any loss of the degree of petrol treatment, ie residual solvent content in the shot and general economic efficiency of the system.
  • the moisture content (water content) of the shot increases in the course of the demining, whereby, by the transfer of evaporation heat on the hexane the water vapor condenses itself.
  • the water content during the descent of hexane-soybean meal increases in the final phase of the descent according to a typical evaporative-condensation process close to the factory from approx. 12% by weight to approx. 22 to 23% by weight when it is received in the descent.
  • This relatively high water content in the demineralized meal is naturally offset by an increased energy expenditure during drying.
  • This energy expenditure can e.g. for hot air, the efficiency of the gasoline and thus the entire oil production system may be called into question.
  • this object is achieved in that the actual de-benzination with water vapor is preceded by a so-called pre-de-benzination with indirect steam or another indirect form of energy transferring heat in a continuous system equipped with several stages or floors.
  • pre-petrol treatment with indirect heat transfer when steam is used, such are required, as mentioned, other forms of energy such as electr. Energy possible however, the condensate of indirect heat transfer by steam is obtained as free water, which no longer has to be steamed out of the meal.
  • the pre-petrol treatment relieves the actual de-petrol treatment with direct steam - which cannot be completely dispensed with for procedural and product-quality reasons - while further reducing the energy required to drive the stirrer shaft in the petroleum spirit (TTK, DT, etc.) and allowing either to reduce the size of the drying and cooling units that follow the gasoline removal, or to combine them into a single unit.
  • the overall improved energy yield is also to be assessed, which has an effect, for example, in an average saving of 50 kg and more steam for the demining process per 1000 kg of processed seed (soy).
  • indirect steam is preferred because it does not require any additional supply devices because it is readily available in an oil production plant.
  • the amount of solvent to be expelled during the pre-petrol treatment, especially with indirect steam heating, e.g. Hexane from soybean meal is on average between 20 and 70%, in particular between 40 and 60%, preferably 50% of the solvent present in the wet meal.
  • the pre-gasoline not only saves energy, especially water vapor, it can also combine the drying and cooling process, thereby significantly reducing the size of the equipment. This is e.g. in principle possible when using a petroleum spirit as described in EP-A-0 070 496 and which goes back to the TTK according to "Fette-Soap-Paints" (1.c.). It is also advantageous to use superheated steam in accordance with European patent application .82 106 498.7.
  • Simultaneous drying and cooling can e.g. can be achieved in that the cooling air (primary air) is led directly through the demineralized but still warm meal, while the exhaust air from the cooling system via a heat exchanger converts the cold fresh air for drying (secondary air) to the required temperature without significant additional effort for heating the secondary air e.g. 55 ° C and above.
  • This warm secondary air is blown in above the scrap bed, which is initially still wet with water, which is moved in the combined drying and cooling unit. It dries the material and then combines with the cooling air, which is also heated by the cooling process
  • the secondary air requires considerably less energy (only electrical energy for driving a fan) and the amount of primary air is reduced by the circulation of the secondary air, not only is less electrical energy required overall, but the apparatus pool is also reduced by combining dry air - and cooling level, it reduces the performance and the design of the blower and finally the above measures also shorten the time of the shot throughput, ie the overall capacity of a plant can be increased.
  • Miscella (8) which contains approx. 20 to 40% oil (remainder solvent and water), is continuously withdrawn from the extractor (1) and fed to the processing (distillation, oil refining, possibly further solvent distillation, etc.)
  • the hexane-wet soybean meal - used here as an example for the overall process - passes from the extractor (1) via line (15) to the gasoline (2), which is generally in direct connection with the scrap drying (3) and the shot cooling (4) without these three stages of shot processing must form a single unit.
  • the gasoline in (2) is carried out with the help of water vapor, which according to the latest knowledge is preferably fed in at the bottom of the gasifier (2), which operates frequently continuously, via line (7).
  • the ne in EP-A-0070496 described b e Entbenzinierer has proven particularly useful. This consists of a predominantly cylindrical container with several levels, which are provided with sieve or perforated plates with discharge elements (locks) as floors that close at the bottom. Stirring elements are provided on a common shaft for each floor. that keep the shot in constant motion. This enters the device above the top floor and arrives by gravity below, to be redirected via a lock into the drying and cooling zones.
  • this steam is directed towards it from the lowest floor, whereby the steam is constantly redistributed due to a particularly advantageous construction of the intermediate floors, so that any channel formation is excluded and optimal de-benzinating takes place.
  • part of the steam condenses, thus moistening the shot.
  • the vaporizer vapors consisting of water vapor and hexane vapor are also processed, i.e. Separation of the water from the hexane and possibly distillation of the latter before it is returned to the extraction.
  • TTK petroleum spirit
  • the hexane-free but condensate-enriched meal is largely freed of water in the drying stage (3) - with the help of warm or hot air - and then cooled to ambient temperature in (4) with cold air.
  • the hexane-free, dry and cooled grist can be used again.
  • the actual de-benzinating (2) is preceded by a pre-de-gasing (12).
  • a pre-de-gasing (12) This leads to the fact that up to 70%, possibly even more, of the hexane contained in the hexane wet shot is expelled.
  • the pre-gasoline works with indirect heat transfer, especially with indirect steam, which means that the water content in the shot does not increase.
  • the pre-gasoline is directly connected to the transport route between the extractor (1) and the gasifier (2) and can, for example, accomplish the transport through line (15) as a steam-heated screw.
  • the solvent expelled in the pre-benzine (12), in the special case hexane, is fed to the solvent preparation via (14), as are the vapors (9) escaping from the gasoline.
  • main petrol engine (2) which is constructed on the basis of the device according to EP-A-0 070 496 or European patent application 82 106 498.7.
  • the water-containing scrap reaches the drying and cooling stages, which either act as isolated units (3, 4) according to Fig. 1, or as a combined drying and cooling stage (11 ) are connected downstream of the mineral spirits (2).
  • FIG. 3 Shown in the block diagram is a system which, according to the invention, contains a pre-gasoline, and is equipped with a combined drying and cooling unit, which in turn forms a unit with the actual or main-gasoline, so that drying and cooling take place in one work step.
  • the hexane-wet good coming from the extraction for example: Soybean meal (100) with approx. 25 to 35% hexane is heated to the evaporation temperature of the hexane in the pre-gasoline (120), whereby between 58 and 62% of the hexane evaporate during the passage of the shot through the pre-gasifier. This is continuously discharged -GG f .u n t he a weak vacuum and fed via (140) of the preparation.
  • the warm shot which still contains about 10 to 15% of hexane, flows from the pre-tinder (120) via line (122) in a continuous flow into the actual or main-teller denoted overall by (200).
  • this section (122) should also be insulated and, if necessary, indirectly heated in such a way that the grist essentially maintains the temperature at the outlet from the pre-tinder until it enters the main de-tanner (200).
  • the example of the main de-benzinator with direct steam admission (200) shown by way of example and only schematically in FIG. 3 comprises three de-benzinating stages (a, b, c) with retracted perforated plates designed as raised floors, the floors being able to be fed with both indirect and direct steam .
  • stirring arms move slightly above each floor, as a result of which the shot is constantly moved and circulated.
  • Direct steam in particular superheated steam (107), is blown in below the bottom floor of the main de-benzinization, i.e. below the floor (201) forming the end of stage (c), and as it passes through floor (201) over the entire cross-sectional area of the main Entbenzierers (200) evenly distributed.
  • Suitable gasoline units for main gasoline and fully continuous operation are described in EP-A-0 070 496 and in European patent application 82 106 498.7, the European patent application 82 106-498.7 in particular relates to a gasoline unit for direct, superheated steam .
  • stage d Enriched hot shot continuously - via a lock (104) in the bottom floor (201) of the actual debenzining the now hexanbuild, but with water up to 22 to 23 wt .-%, in operation only to 15 to 19 weight reached into the combination of drying and cooling according to the invention (stage d).
  • This unit is similar, if not identical, to stages (a, b, c), which means that stirring elements are also effective here abut the common central shaft and be moved over raised floors that correspond to those of steps (a, b, c).
  • the base (202) is designed as a perforated base, so that the cooling medium introduced via connection piece (2C3) is uniformly distributed over the entire cross section of the base.
  • cold air primary air
  • line (150) from the blower (151) through support bracket (203) into the room (204) under the distributor floor (202) and through the Soil (202) on the warm, but already largely dried grist moved in (d).
  • the grist cools down and passes through a further lock (105) in the bottom (202) via line (110) for final processing or recycling.
  • the primary air warmed when passing through the warm, largely dry grist in (d) leaves the system via line (141), passes a cyclone (140) or a similar device for separating dust and grit particles and reaches an average temperature of 45 to 65 ° C, in particular 50 to 60 ° C, over the heat exchanger (130) Freihe (135).
  • the heated primary air gives off most of its heat input to new fresh air (131), which heats up as secondary air to about 44 to 64 ° C, in particular 50 to 60 ° C.
  • the secondary air heated in this way passes via line (132) and fan (133) and line (134) into the space above the scrap bed in stage (d).
  • warm primary air and warm secondary air combine and have a drying effect on the wet shot falling down via lock (104) into step (d).
  • the dry and cooled grist leaves the plant via (110) in a chemical and physical state, which it z.2. can be used directly for most feed.
  • the measures of the invention not only optimize the energy consumption figures for the de-benzination of solvent-wet extraction residues - a particular consequence of the pre-de-benzination according to the invention - the scope of the apparatus can also be reduced by the main de-benzination + combined drying and cooling that occurs as a unit. It has been shown, for example, that the condensate of the indirect steam that arises in the prebenting as feed water of the steam boiler contributes to its relief, that the path between the extractor and the denaturing by using an indirectly steam-heated screw conveyor or an equivalent conveyor unit makes the investments for the prebenting practically balances, since this way in everyone must be covered.
  • the pre-petrol treatment can also reduce the effort for solvent preparation from the main de-petrol treatment, since the solvent obtained in the pre-petrol Hexane, no separation of water is required.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
  • Beans For Foods Or Fodder (AREA)
  • Processing Of Solid Wastes (AREA)
EP83103235A 1983-03-31 1983-03-31 Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse Withdrawn EP0120984A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP83103235A EP0120984A1 (fr) 1983-03-31 1983-03-31 Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse
US06/769,766 US4622760A (en) 1983-03-31 1985-08-27 Apparatus for desolventizing and drying solvent-containing residue meal

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP83103235A EP0120984A1 (fr) 1983-03-31 1983-03-31 Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse

Publications (1)

Publication Number Publication Date
EP0120984A1 true EP0120984A1 (fr) 1984-10-10

Family

ID=8190386

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83103235A Withdrawn EP0120984A1 (fr) 1983-03-31 1983-03-31 Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse

Country Status (2)

Country Link
US (1) US4622760A (fr)
EP (1) EP0120984A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1336426A1 (fr) * 2002-02-06 2003-08-20 De Smet Engineering N.V. Procédé et dispostif pour enlever du solvant contenu dans des résidus solides d'extraction
US8720082B2 (en) 2009-06-05 2014-05-13 Desmet Ballestra North America, Inc. Desolventizer toaster with vapor recycle

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6270736B1 (en) 1999-01-21 2001-08-07 Frazier, Barnes Research Llc Identity preserved oilseed mill
US6996917B2 (en) * 2001-10-15 2006-02-14 Crown Iron Works Company Two stage apparatus for desolventizing food grain meal
US7195394B2 (en) * 2004-07-19 2007-03-27 Vijay Singh Method for resonant wave mixing in closed containers
WO2007055913A1 (fr) * 2005-11-08 2007-05-18 Desmet Ballestra North America Systeme et processus mecaniques de desolvantation partielle
BRPI0808487A2 (pt) * 2007-03-14 2014-07-15 Desmet Ballestra North America Inc Secador/resfriador de alimentos aperfeiçoado.
EP2028258A1 (fr) 2007-08-01 2009-02-25 N.V. Desmet Ballestra Engineering S.A. Procédé pour la désolvantation d'équipement sous pression réduite
BRPI1002765B1 (pt) * 2010-08-02 2020-03-03 Granol Indústria, Comércio E Exportação S/a Processo de purificação de óleos vegetais mediante retirada de sólidos por centrifugação na fase miscela
US9683778B2 (en) 2011-04-25 2017-06-20 Crown Iron Works Company Solvent scavenger for a desolventizer toaster using a vapor recovery system
AR086118A1 (es) * 2011-04-26 2013-11-20 Crown Iron Works Co Eliminador de solvente para un tostador desolventizador que emplea un sistema de recuperacion de vapor
US9709330B2 (en) * 2012-10-25 2017-07-18 Crown Iron Works Company Desolventizer toaster
EP3194044B1 (fr) 2014-09-18 2022-02-02 Bridgestone Corporation Extracteur et procédé associé
JP6289334B2 (ja) * 2014-09-30 2018-03-07 日清オイリオグループ株式会社 植物油粕の製造方法
GB2553793A (en) 2016-09-14 2018-03-21 Desmet Ballestra Eng N V /S A Apparatus for the treatment of solvent extraction residue
US11661564B2 (en) * 2016-11-11 2023-05-30 Desmet Usa, Inc. Apparatus for the desolventisation of extraction residue

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE658037A (fr) * 1964-01-11 1965-04-30
DE2348734A1 (de) * 1973-09-28 1975-04-10 Dravo Corp Verfahren zum konzentrieren eines mit oel angereicherten loesungsmittels
EP0070496A2 (fr) * 1981-07-20 1983-01-26 Heinz Schumacher Appareil pour le traitement des matériaux floconneux ou granuleux avec des gaz ou des vapeurs dans un procédé contre-courant et en continu

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3126285A (en) * 1964-03-24 Method of desolventizing and toasting soybean meal
US2676668A (en) * 1949-06-13 1954-04-27 Fmc Corp Apparatus for contacting gaseous fluids and granular solids
US2585793A (en) * 1950-11-10 1952-02-12 Central Soya Co Soybean treating process
US2639973A (en) * 1950-12-16 1953-05-26 Standard Oil Dev Co Method of and apparatus for improving gas distribution in bubble-cap tower operating on fluidized solids
US2776894A (en) * 1954-07-29 1957-01-08 Central Soya Co Meal-treating process and apparatus
GB1438847A (en) * 1973-09-20 1976-06-09 Dravo Corp Process for treating an oil-enriched solvent
US4332092A (en) * 1980-09-24 1982-06-01 Dravco Corporation Process and apparatus for desolventizing and drying solvent wet materials
FR2510736B1 (fr) * 1981-07-28 1986-07-18 Beghin Say Sa Procede de sechage par recompression de vapeur

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE658037A (fr) * 1964-01-11 1965-04-30
DE2348734A1 (de) * 1973-09-28 1975-04-10 Dravo Corp Verfahren zum konzentrieren eines mit oel angereicherten loesungsmittels
EP0070496A2 (fr) * 1981-07-20 1983-01-26 Heinz Schumacher Appareil pour le traitement des matériaux floconneux ou granuleux avec des gaz ou des vapeurs dans un procédé contre-courant et en continu

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1336426A1 (fr) * 2002-02-06 2003-08-20 De Smet Engineering N.V. Procédé et dispostif pour enlever du solvant contenu dans des résidus solides d'extraction
US8720082B2 (en) 2009-06-05 2014-05-13 Desmet Ballestra North America, Inc. Desolventizer toaster with vapor recycle
US9250013B2 (en) 2009-06-05 2016-02-02 Desmet Ballestra North America, Inc. Desolventizer toaster with vapor recycle

Also Published As

Publication number Publication date
US4622760A (en) 1986-11-18

Similar Documents

Publication Publication Date Title
EP0120984A1 (fr) Procédé et installation pour l'enlèvement de l'essence de résidus restant après extraction, au moyen de solvants organiques, de matières premières végétales contenant de l'huile ou de la graisse
EP0077436B1 (fr) Procédé et appareil pour déparaffiner des matériaux végétaux résiduaires de forme floconneux et granuleux après leur extraction
DD150077A5 (de) Verfahren und vorrichtung zur oelgewinnung aus gereinigten oelfruechten und oelsaaten
DE112011101131B4 (de) Flachbett-lösungsmittelextrahierer
DE3137575A1 (de) Verfahren und vorrichtung zur befreiung eines mit loesungsmittel extrahierten materials von loesungsmittel
DE2641143A1 (de) Verfahren und vorrichtung zum gewinnen von oelen aus oelhaltigen rohstoffen
DE3513021A1 (de) Verfahren und vorrichtung zum waermebehandeln von fliessfaehigen materialien
DE2700791A1 (de) Verfahren und vorrichtung zum herstellen von feinem, von geruch befreitem sojabohnenpulver
DE112013005028B4 (de) Verbessertes Quetschverfahren für Sojabohnen
DE102017120680A1 (de) Vorrichtung zur Behandlung eines Lösungsmittelextraktionsrückstands
DE112017005696B4 (de) Verbesserte Vorrichtungen zum Desolventieren der Extraktionsrückstände
DE2556485A1 (de) Verfahren zur herstellung eines proteinkonzentrates unter minimaler denaturierung des proteins
WO2000036058A1 (fr) Procede pour traiter des flocons de graines oleagineuses
DE3815726A1 (de) Verfahren und vorrichtung zur thermischen behandlung von stoffen und stoffgemischen im fliess- oder wirbelbett
DE8309554U1 (de) Vorrichtung zum entbenzinieren von rueckstaenden, die bei der extraktion von pflanzlichen, oel- und fetthaltigen rohstoffen mit organischen loesemitteln anfallen
DE2900362C2 (de) Verfahren und Anlage zum Trocknen von Zuckerrübenschnitzeln
EP2940414B1 (fr) Procédé et dispositif de séchage de produits végétaux
DE2734198A1 (de) Anlage zum waermebehandeln von guetern
DE936946C (de) Verfahren und Einrichtung zur Loesungsmittelextraktion fester Stoffe
DE102021128991A1 (de) Verfahren und Vorrichtung zur Extraktion
CH652893A5 (en) Treatment of extracted soya bean flakes
AT389466B (de) Verfahren und anlage zur thermischen behandlung von guetern mit feststoffanteil
DE1016238B (de) Vorrichtung und Verfahren zur Entfernung von Loesungsmitteln aus Feststoffen
DE559830C (de) Verfahren und Vorrichtung zur kontinuierlichen Destillation eines festen Brennstoffes
DE487234C (de) Verfahren zur Verwertung der Bruedenabwaerme bei Trockenanlagen

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19840326

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE FR GB IT LI LU NL SE

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

RBV Designated contracting states (corrected)
18W Application withdrawn

Withdrawal date: 19850810