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WO1995004579A1 - Utilisation de vapeur d'eau surchauffee pour le sechage, pratiquement exempt de gaz perdus, de substances recyclables et de melanges de substances recyclables sensibles a la temperature, et produits secs ainsi fabriques ayant des proprietes ameliorees - Google Patents

Utilisation de vapeur d'eau surchauffee pour le sechage, pratiquement exempt de gaz perdus, de substances recyclables et de melanges de substances recyclables sensibles a la temperature, et produits secs ainsi fabriques ayant des proprietes ameliorees Download PDF

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Publication number
WO1995004579A1
WO1995004579A1 PCT/EP1994/002528 EP9402528W WO9504579A1 WO 1995004579 A1 WO1995004579 A1 WO 1995004579A1 EP 9402528 W EP9402528 W EP 9402528W WO 9504579 A1 WO9504579 A1 WO 9504579A1
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WO
WIPO (PCT)
Prior art keywords
drying
superheated steam
substances
phase
dried
Prior art date
Application number
PCT/EP1994/002528
Other languages
German (de)
English (en)
Inventor
Wilfried Rähse
Johann-Friedrich Fues
Original Assignee
Henkel Kommanditgesellschaft Auf Aktien
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 Henkel Kommanditgesellschaft Auf Aktien filed Critical Henkel Kommanditgesellschaft Auf Aktien
Priority to JP7506204A priority Critical patent/JPH09501098A/ja
Priority to EP94924823A priority patent/EP0713412A1/fr
Publication of WO1995004579A1 publication Critical patent/WO1995004579A1/fr

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Classifications

    • 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
    • F26B3/12—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 in the form of a spray, i.e. sprayed or dispersed emulsions or suspensions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/001—Heating arrangements using waste heat
    • F26B23/002—Heating arrangements using waste heat recovered from dryer exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/02—Heating arrangements using combustion heating
    • F26B23/022—Heating arrangements using combustion heating incinerating volatiles in the dryer exhaust gases, the produced hot gases being wholly, partly or not recycled into the drying enclosure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/005—Treatment of dryer exhaust gases
    • 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
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the invention describes improvements in the field of drying processes which can be used on an industrial scale, in particular obtaining solid recyclables and mixtures of recyclables, with the aim of on the one hand being able to meet the increasingly urgent need to operate corresponding drying plants without exhaust gas and exhaust gas, and on the other hand to substantially improve the economy and the possible application range of such process types.
  • the invention seeks to provide the possibility of using the principle of the process of drying a water-containing feedstock with superheated steam as a drying gas flow even where, to date, this technology, which is known per se, has not been able to prevail for a variety of reasons.
  • the teaching according to the invention intends to show technical approaches to how the mentioned drying process can be put into practice in fields which hitherto do not appear to be accessible in practice to the principle of drying with superheated steam.
  • the following may be mentioned as examples: the production of dried, high-quality foodstuffs containing flavorings in particular from the area of foodstuffs and luxury foods and / or the starting materials for their production, the area of the flavoring concentrates for use in the product area mentioned, but also the field of cosmetic and pharmaceutical auxiliaries and / or valuable materials.
  • the task according to the invention also covers the area of converting potential hazardous substances from the class of herbicides, fungicides and insecticides into dry preparation forms within the scope of effective drying of corresponding aqueous preparations on a large industrial scale to form powdery formulations and / or agglomerated dry products with improved redispersibility or dissolution in water.
  • dry milk powder or agglomerate should not only show the desired rapid redissolubility in water, indispensable requirements are the white color of the dry product and the characteristic milk odor and taste. With regard to the last-mentioned requirements, other food technology products are even more demanding. Just as an example, reference should be made to dry preparations of coffee or coffee extracts and comparable beverages, in particular in the form of corresponding instant products.
  • the teaching according to the invention makes particular use of the technique of drying in the spray zone, in which a material to be dried is treated as a reverse phase with a closed phase of the drying gas in cocurrent and / or countercurrent.
  • the teaching according to the invention is not limited to spray technology.
  • Other possibilities which can be combined in particular with spray technology are fluidized bed drying, fluid bed drying or other known technologies.
  • a feature of continuous drying is that the hot drying gas, in particular drying air or fuel gases, is once passed through the system and the exhaust air is released into the atmosphere.
  • the dry product is discharged from the drying zone.
  • the exhaust gas stream is usually cleaned of entrained portions of good. Nevertheless, it is known that this technology can lead to considerable environmental pollution through the discharge of undesirable odorous substances, active and pollutant components and the like.
  • An inert drying gas generally nitrogen
  • An inert drying gas is passed through the system of work stages in a closed circuit so that no exhaust air is released into the atmosphere. reaches.
  • the gas stream drawn off from the drying zone and loaded with moisture to be evaporated and discharged good fractions is freed from carried solid fractions as far as possible and cooled to condense the discharged water fraction.
  • the inert gas phase as a whole is subjected to this condensation and washing step.
  • the gas phase separated from this is passed through a gas heater and returned to the drying zone.
  • a modification with a partially closed circuit provides a so-called self-inertizing air heater for heating the gas flow carried in the circuit, in which hot exhaust gas from the combustion of a suitable fuel is fed to the circuit gas flow with its simultaneous heating.
  • a corresponding exhaust gas flow must be taken from the gas phase in the circuit.
  • a suitable procedure can also be used to form a low-oxygen mixture which enables the drying of water-containing dust-explosive products under inert gas conditions. This manner of driving is nevertheless ruled out for the drying of demanding mixtures of valuable materials and in particular for the production of powdered or agglomerated dried foods such as milk powder and the like.
  • the preferred operating temperature of the superheated steam for drying such materials of biological origin is 200 ° C (400 ° F) (US, column 4, 23-25).
  • the problem of drying feedstocks which contain volatile components, in particular flavors or aromas is seen in this publication as a particular advantage that these vapor-proof constituents are largely returned to the drying zone together with the recycled superheated steam (US, columns 7, 30-38).
  • a special feature of hot steam drying according to WO 92/5849 cited above lies in the individual temperature profile of the aqueous droplet of material to be dried in the hot steam spray zone.
  • the aqueous drop is spontaneously heated to the boiling point of the water under working conditions, that is to say when working under normal pressure to temperatures of about 100 ° C.
  • This boiling temperature is maintained as a minimum temperature in the droplets during the entire drying period.
  • thermolabile aqueous material for example milk or milk products such as whey
  • the conceptual approach to drying these feedstocks with overheated Water vapor, especially in the spray zone has been proposed for about 25 years, see the previously cited FR-PS 2002088 (10/1969).
  • the maximum settable product temperature for the production of a high-quality milk dry product in the context of spray drying is around 80 to 85 ° C. Methods that allow the setting of maximum product temperatures in the range of approximately 60 ° C. are preferred.
  • a short-term heat treatment at elevated temperatures to prolong the shelf life and to eliminate pathogenic microorganisms is provided only in the course of processing the milk.
  • pasteurization high-temperature heating to 85 ° C. for 2 to 3 seconds
  • short-term heating in the plate heater 72 to 75 ° C. for 15 to 30 seconds
  • continuous heating 62 to 65 ° C. for 30 to 32 min
  • ultra high temperature heating UHT either by indirect heating (136 to 138 ° C / 5 to 8 sec) in the tube or plate heat exchanger and by direct heating (140 to 145 ° C / 2 to 4 sec) by steam injection with subsequent aseptic packaging.
  • the Bactother process which consists of a combination of centrifugal disinfection in Bactofugen (65 to 70 ° C.) and UHT heating of the separated sediment (2 to 3% of the milk) with subsequent recombination, can be used to adjust the taste advantages . This avoids heating the entire amount of milk.
  • sterilization at 107 to 115 ° C. for 20 to 40 minutes or at 120 to 130 ° C. for a period of 8 to 12 minutes in the packaging in the autoclave is known.
  • taste impairments are consciously accepted.
  • Belitz et al. “Textbook of life chemistry” 4th edition, Springer-Verlag, Berlin, chapter 10 "Milk and milk products”.
  • micro-drying relates in particular to the areas of material degeneration under the influence of the increased drying temperatures and the formation of hard crusty shaped drying products, particularly in late stages of the
  • the invention relates to a process for treating a water-containing, flowable and finely divided valuable material (disperse phase) with superheated water vapor (closed phase) in cocurrent and / or countercurrent in a spray zone through which the superheated water vapor flows, with discharge of water and steam-volatile ingredients from the disperse feed and formation of a fine-particle dry material.
  • the method is characterized in that in the disperse phase valuable substances and preparations from the following areas are used: nutrients, in particular foods (food and beverages) and starting materials for their production, aromatic substances (smell and taste) preparations) containing preparations, preparations from the fields of cosmetic and pharmaceutical auxiliaries and / or valuable substances as well as herbicides, fungicides and insecticides.
  • the process according to the invention particularly provides for the feed to be used in the form of water-containing solutions, emulsions, suspensions and / or pastes and, in particular, to work in the range of normal pressure. Since the superheated steam is used as the closed phase and as the drying medium, the temperature of the product in the range of about 100 ° C.
  • the invention relates to food or feed suitable for consumption by humans and / or animals and auxiliaries suitable for this purpose in the form of an at least largely dried solid carrier which has been subjected to further physiologically compatible auxiliaries and / or valuable substances can.
  • the teaching of the invention is characterized in that the solid carrier in the dried but not yet acted upon state is provided with an absorbent porous internal structure and has been produced by drying a water-containing nutrient or a corresponding nutrient mixture in superheated steam as the drying gas.
  • the solid support with a porous internal structure has been produced in particular by spray and / or fluidized bed drying of a flowable wet material, in particular by drying aqueous solutions, emulsions, suspensions and / or pastes of the valuable substances forming the solid support.
  • the dried porous carrier is present as a solid in the temperature range from about 100 to 110 ° C., the plasticity and surface tack of which are restricted in such a way that substantial bonding of the particles to one another and / or bonding of their open-pore internal structure also excrete under the conditions of exposure to superheated steam. This ensures the possibility of impregnating such a porous carrier with freely selectable application materials which are at least substantially incorporated in the porous inner structure of the carrier.
  • the invention relates to the use of spray drying a disperse aqueous valuable material in cocurrent and / or countercurrent in superheated steam as the drying gas for the production of free-flowing and free-flowing dry products in the field of dairy products, as well as dry products in the fields of coffee and coffee. Extracts, corresponding decaffeinated or coffee substitute products, tea and tea extracts, vegetable and / or fruit powder, dry soups and sauces, cocoa, cocoa / milk or fruit / milk preparations, vitamin / fruit or Fruchtaro a combinations.
  • the invention relates to dry milk and dry milk products, produced by spray drying the aqueous material in the presence of superheated steam as the drying medium, and furthermore at least largely water-soluble dry coffee or coffee extract in pourable and free-flowing form, and corresponding preparation forms for tea and tea extracts , Cocoa, vegetable and fruit powders, optionally in admixture with other water-soluble components from the field of food and beverages.
  • a characteristic of all these products is that they have been produced by spray drying in the presence of superheated steam as the drying medium and preferably contain further auxiliaries and / or valuable substances introduced into the porous basic structure of the dried material. Examples of such auxiliaries and valuable substances are aroma substances (odorants and flavors), physiologically compatible solubilizers, sweeteners and the like.
  • the invention furthermore relates to flavor concentrates in the form of pourable and free-flowing solid powder and / or agglomerates containing a porous carrier solid, produced by drying an aqueous preparation of a physiologically compatible value and / / value which is solid in the temperature range from about 100 to 110 ° C. or auxiliary, in particular from the area of food and beverages, which has been produced by spray and / or fluidized-bed drying of aqueous preparations of the carrier material with superheated steam as the drying gas.
  • this porous carrier solid has been loaded with liquid and / or solid flavoring agents and their flowable preparations, whereupon preferably a final covering of the carrier filled with flavoring agents has been carried out with a physiologically compatible and storage-tight coating.
  • the method according to the invention works due to the chemical nature of the drying medium - superheated steam as a closed gas phase - based on the drying step selected in a closed cycle. From the drying stage, in particular the spray zone, superheated steam laden with additionally evaporated water is drawn off and - after separating off the vapor stream corresponding to the evaporated water content - is returned to the drying zone in the circuit.
  • the possibility of reheating the superheated steam to the predetermined operating temperature of the drying medium is provided - preferably in indirect heat exchange and immediately before the steam flow re-enters the spray zone.
  • the material to be dried is introduced into the drying zone in finely divided form in its water-containing form of use - spray-sprayed, in particular, into the space through which superheated steam flows, or finely distributed in another form therein - while the dried material from this area is known per se, usually at the bottom of the spray zone.
  • the concept of the closed and practically exhaust-gas-free cycle also relates to the evaporated water portion of the dried-up valuable material that is branched off as a vapor partial stream.
  • This partial steam flow leaves the drying zone at outlet temperatures which result from the specified inlet temperatures and the extent of water evaporation in the drying stage.
  • the evaporated water portions discharged in the field affected by the invention, in particular when drying food and beverages, steam-volatile components are usually also drawn off with this vapor component.
  • the solid matter I obtained during drying in superheated steam forms a very specific structure under the conditions which will be detailed below .
  • the characteristic elements are a continuous microporous solid structure without the formation of a closed crust in the outside area.
  • a temperature and humidity gradient quickly forms in the drop from the surface inwards.
  • the surface of the drop dries quickly, and a solid, closed crust is formed.
  • Liquid diffuses outward from the inside of the drop, substances dissolved in the water crystallizing out as soon as their solubility is exceeded. The result is a further consolidation and thickening of the outer shell. Residues of microdisperse air remain enclosed in the sealed bead.
  • This high porosity of the solid material can be the basis for multifaceted elements of the action according to the invention and for the advantages when using the teaching according to the invention.
  • the high porosity of the solid material can be the basis for a substantially improved water solubility and wettability and / or for a greatly increased absorbency of the steam-dried material compared to flowable phases in comparison to the conventionally dried material.
  • the outer particle surface of the granular carrier bead can be covered with an application mass, in particular the inner surface and ultimately the entire freely accessible interior of the carrier bead grain dried in superheated steam can be coated or filled with application mass. It immediately lights up:
  • the steam-capable components of the feedstock which are circulated via the vapor flow but are also accessible there, as previously indicated, in the closed process cycle can be recombined with the absorbent and highly porous dry product in a way which has not hitherto been possible.
  • These vapor-efficient fractions can namely be returned to the inside of the solid material that has now been processed into a porous carrier. part of the input material are entered.
  • a prerequisite for the perception of these advantages of the action according to the invention is, among other things, that the fine-grained dry material can form as a microporous, stable carrier bead without a closed crust.
  • the dried porous carrier is present as a solid in the working temperature range of the drying zone, the plasticity and surface stickiness of which are so limited that substantial bonding of the particles to one another and / or bonding of their open-pore internal structure also under the conditions of Eliminate exposure to superheated steam.
  • the temperature range of approximately 100 to 110 ° C. is set as the material temperature in the material particles underlying the drying process. The previously given requirements must therefore be met for this area.
  • the predominant part of the recyclable materials to be subjected to the process according to the invention fulfills these requirements due to its natural compositions. This applies in particular to the natural material-bound feedstocks of the foodstuffs to be converted in a dried solid phase, the plants and plant parts supplying flavorings, but also to a large number of the other materials defined for use in the process according to the invention. If, in special cases, this prerequisite for the formation of the dried valuable material as a solid carrier with a highly porous internal structure is not met, then this condition can be easily met by using suitable auxiliary substances.
  • the open-pore structure of the resulting dry material and the prevention of crust formation from intermediate gel-like layers enables - in cooperation with certain process elements described in detail below - such a shortening of the drying process in the phase of superheated steam that even highly degenerate Materials at risk of reorganization, such as milk and milk products, can be subjected to the drying process according to the invention with a high degree of maintenance.
  • the volatile components which are separated from the recyclable material mixture and extracted from the process cycle with this vapor partial stream - in particular, for example, portions of complex mixtures of flavorings - are obtained to a certain extent in a purified form during the condensation of the vapor stream, which is particularly easy and inexpensive to recover Allow flavoring substances in their entirety.
  • the vapor component freed from entrained solids now only contains water and the volatile, especially organic, components.
  • These last-mentioned substances can be separated from the purely aqueous phase in any manner and in particular without hindrance by other mixture components, as are usually to be taken into account when extracting aromas from, for example, fruits, parts of plants and the like.
  • the teaching according to the invention provides for the use of the entire range of the prior art methods developed for flavor extraction.
  • the transferred organic portion can be effectively separated from the aqueous phase by membrane separation processes.
  • the complex organic mixture of substances does not have to be separated. It can be reunited as a whole with the porous solid support and absorbed by it in its internal structure.
  • the teaching according to the invention enables optimized reunification of all desired components of the starting material present in aqueous preparation in the finished product.
  • the teaching according to the invention is not restricted to this.
  • the microporous structure of the solids fraction obtained in isolation creates the possibility of storing additional valuable substances or also valuable substances other than the fractions discharged via the vapor partial flow in the carrier and, if desired, sealing them in a stable manner. It is immediately clear that paths that have not yet been opened up are opened here for the field of water-soluble instant products in the field of food and beverages. But it is not just this area of food for human consumption that is affected. In the same way, animal feed can be worked up to form compounds which can be predetermined and which can be given high storage stability by a final coating.
  • Another important aspect of the teaching according to the invention deals with the potential usability of the withdrawn vapor stream in parts of the overall process.
  • the invention intends to make practical use of this (partial) product of the process, which is produced in a continuous stream.
  • This (partial) product of the process which is produced in a continuous stream.
  • the possibilities given here are discussed in detail below.
  • the vapor partial flow can be used to separate off volatile components - in particular flavors - of the valuable material to be dried, so that a water-containing material depleted in these volatile valuable components of the drying process with the superheated Steam is supplied.
  • use can be made of the energy content of the vapor stream, in particular in the context of its condensation and transfer of the heat of condensation to the aqueous feed material, in a sensible manner. In this way, for example, the aqueous material to be dried can be concentrated with superheated steam before it is introduced into the drying stage.
  • a first embodiment of the teaching according to the invention relates to the method for drying a water-containing feed material from the specified areas using superheated steam as the drying phase, the material to be dried forming the disperse phase and the superheated steam forming the closed phase.
  • the technology preferably used is the known spray drying, in which the material to be dried is conducted in finely divided form in cocurrent and / or in countercurrent to the closed drying gas phase and dried to the desired extent.
  • spray towers are used here.
  • the water-containing feed material to be dried can be finely introduced into the tower through which the drying gas flows, using spray nozzles, but also in other ways, for example by means of rotary disks or centrifugal atomizers.
  • the feed material is expediently used in the form of water-containing solutions, emulsions, suspensions and / or pastes.
  • aqueous preparations either from the outset - an example of this is milk - or else corresponding aqueous preparations.
  • Preparations can be produced in simple form, for example by extraction processes of plants and parts of plants with water and / or aqueous / organic systems. Examples of the latter case are coffee extracts in the broadest sense.
  • the methodology according to the invention is equally suitable for coffee extracts as for decaffeinated coffee extract or also for coffee substitutes and coffee additives.
  • the two basic types of drying milk on one side and coffee extracts on the other are deliberately placed side by side.
  • the drying of milk in the industrial process is dominated by the problem of the possible degeneration of important milk constituents, in particular the milk proteins, which can be associated with an irreversible transformation of the dry substance into a difficultly soluble or largely insoluble dry product.
  • Loss of aromas through the discharge of appropriate aroma substances with the drying gas play no or at best a completely subordinate role.
  • undesirable changes in the solids content - again due to undesirable degeneration reactions - have to be taken into account.
  • the teaching according to the invention provides, in a preferred embodiment, when desired components are obtained in superheated steam, to at least partially recover these portions - for example the portion of aroma substances discharged - and, if desired, to combine them again with the dry matter obtained in the drying stage
  • the teaching according to the invention provides the possibility already described above of disposing of the contaminants in a suitable manner and in particular of incinerating them. A corresponding part of the product flow can be fed to the burner, which - in indirect heat exchange - serves to reheat the circulated flow of superheated steam to the operating temperature.
  • the working conditions of the drying stage are adapted according to the invention to the material or material to be dried. This is particularly valid for the selection of the operating temperature of the superheated steam and the exit temperature of the closed phase from the drying zone determined by controlling the drying process. Details are given below. Uniformly for a preferred embodiment of the teaching according to the invention, the drying of the respectively selected wet material takes place in the range of normal pressure.
  • This term of normal pressure generally includes the ranges up to about 150 mbar overpressure or underpressure, with corresponding pressure deviations up or down to about 100 mbar and in particular up to about 50 mbar being preferred. In many applications, very small pressure deviations from the ambient pressure are used. processes, which can then be, for example, in the range up to about 10 or 15 mbar.
  • the temperature of the material in the aqueous preparation of the disperse valuable substance or mixture of valuable substances in the drying zone corresponds to the boiling temperature of the water under the working pressure, and is therefore usually in the range of about 100 ° C.
  • important adaptations to the conditions specified in the particular individual case can be provided or carried out by varying in particular the temperature of the superheated steam used and the temperature range between the inlet and outlet temperatures of the water vapor phase . If, for example, temperature-stable materials are used, operating temperatures of the superheated steam can be set to values in the range up to 500 ° C or even higher, for example values up to about 700 ° C.
  • Such temperature-stable materials are, however, special cases for the area of application of the principle of drying with superheated steam as drying gas, which is defined according to the invention.
  • the areas of application of the foodstuffs and stimulants, the flavorings, but also preparations from the areas of cosmetic and pharmaceutical auxiliaries and / or valuable substances, which are particularly affected according to the invention, generally relate to temperature-sensitive valuable substances and mixtures of valuable substances, which, because of their temperature sensitivity, have hitherto been unsuitable use materials have been regarded as drying gas for the application of the principle of drying with superheated steam.
  • a first important working parameter lies in the concrete temperature control of the phase of the superheated water used as the drying gas. steam.
  • the following preferred working conditions of this superheated vapor phase apply at least to the areas of the input materials containing food and / or flavorings: operating temperatures of the superheated steam below 200 ° C. and preferably at most about 180 ° C.
  • Particularly suitable operating temperatures of the superheated steam for the working area mentioned here can be in the range from approximately 140 to 180 ° C. and in particular in the range from approximately 145 to 160 ° C.
  • the outlet temperatures of the superheated vapor phase in this working area of the highly sensitive materials do not exceed the value of approximately 150 ° C.
  • Particularly suitable ranges for the steam outlet temperatures are in the range from approximately 105 to 130 ° C. and in particular in the range up to approximately 115 ° C.
  • Lower temperature limits for the steam outlet temperatures are accordingly in the range of the normal pressure chosen according to the invention at about 105 or 110 ° C.
  • the steam outlet temperature should generally not be above 150 ° C and preferably not above 140 to 145 ° C.
  • Particularly suitable outlet temperatures of the superheated steam are in the range from approximately 105 to 130 ° C. and in particular in the range from approximately 105 to 115 ° C.
  • an important process parameter for overcoming the difficulties mentioned here can be the correct choice and adaptation of the mean residence times of the disperse phase in the area of the superheated steam.
  • the teaching according to the invention usually works with corresponding residence times of at most a few minutes, for example 2 to 10 minutes and in particular not more than about 5 minutes. Much shorter residence times can be selected for materials at risk of temperature, which are then preferably less than about 1 minute and expediently in the range of at most about 30 seconds.
  • This form of supply of the water-containing material phase to be dried with a substantially enlarged surface creates the possibility of extreme intensification and / or acceleration of drying.
  • the flowable material phase to be dried is sprayed with the aid of a propellant gas.
  • a propellant gas e.g., a propellant gas.
  • the relevant technology knows the most diverse configurations of such spray devices, in particular spray nozzles. Reference is made to the relevant specialist literature, see here, for example, H. Brauer "Fundamentals of Single-Phase and Multi-Phase Currents” in BASICS OF CHEMICAL TECHNOLOGY, Process Engineering of Chemical and Related Industries, Verlag Sauerators, Aarau and Frankfurt am Main (1971 ), Pages 308 - 323, AH Lefebvre "Atomization and Sprays" Hemisphere Publishing Corp. New York (1989), pages 10-20, Chemical Engineering, Vol.
  • the mode of operation of this embodiment of the method according to the invention may be understood taking into account the respective history of origin of the sprayed drops described in the cited literature.
  • a lamellar liquid phase spread occurs with an extremely small thickness of the liquid phase. This makes an extremely large surface accessible for mass transfer with the superheated water vapor phase, based on the volume of the liquid in question.
  • the intensity and acceleration of the drying result is understandable.
  • the general technical knowledge of the process engineer for enhancing this effect by selecting suitable multi-component nozzles can also be used in the context of the action according to the invention.
  • the flowable material to be dried - for example a milk concentrate - can be fed to the spray nozzles at temperatures which are practically not or only very slightly elevated.
  • the superheated steam in this process step already releases its excess content of thermal energy to the sprayed material and heats it up with it. In this way, heating and spraying are combined in a short process step. It is obvious that substantial reductions in the period of temperature exposure of a temperature-sensitive material are possible.
  • a propellant can also be a substantial process aid in a completely different way: Especially in the field of drying temperature-sensitive materials such as milk, it is known to first concentrate the material to be dried using thin-film evaporator systems under mild conditions to an increased content of dry matter - cf. . the literature reference Belitz et. al. "Textbook of Food Chemistry". Such a concentration can, however, quickly lead to such a strong increase in the viscosity and thus in the mobility of the starting solution that working restrictions are derived therefrom in practice.
  • the use of a propellant gas in the spraying and in the same time also the superheated steam used as a drying agent as a propellant creates the opportunity to concentrate more in the pretreatment processed and therefore more viscous feed material to process without problems.
  • Preferred feedstocks for drying in the sense of the action according to the invention are recyclable materials, which contain at least partially dissolved and / or suspended solids from the area of liquid and / or solid foodstuffs and luxury foods and thus the drying to be stable in storage, in particular free-flowing and pourable solids - preferably of the type of instant products - enable.
  • the preferred determination elements described below are of particular importance.
  • auxiliaries to be selected here should be of such a nature that they do not interfere with the intended use of the material or material that is ultimately obtained.
  • General specialist knowledge provides sufficient suggestions for action in the sense of the teaching according to the invention for the respective specific individual case.
  • the result of such a selection or configuration of the feed material to be dried ensures the open-pore microporous material structure in the dried solid base body.
  • the ideal carrier for subsequent loading with freely selectable given application masses which, in the embodiment preferred according to the invention, penetrate into the interior of the porous dry solid and occupy the interior at least partially or completely.
  • auxiliaries can also be suitable for making temperature-sensitive feedstocks accessible for drying in the process according to the invention and, in particular, for drying them to form a solid, which are at least partially at risk of degeneration in the temperature range from about 100 to 110 ° C.
  • the open, microporous basic structure which is reliably established here in the sense of the inventive action allows the rapid exit of the water components present in the interior of the material, without the droplet being sealed, for example by gel formation in the outer region, as is characteristic Appearance for drying in hot air.
  • the process according to the invention is particularly suitable for products which, when necessary, degenerate permanently in the temperature range from about 100 to 110 ° C. during drying in the presence of air, nitrogen and / or combustion gases.
  • the invention provides for these steam-volatile components to be recovered in order to recover discharged steam-volatile components - for example, in particular flavorings from foods.
  • this recovery is carried out after the condensation of the vapor phase of the vapor stream withdrawn to form the aqueous liquid phase.
  • aTTe processes known per se for separating organic components from their aqueous mixtures or combinations of different process types can be used.
  • the appropriate technical action is determined according to the requirements that the respective mixture of substances places. For example, separation processes such as phase separation, extraction, separation by distillation or adsorption on solids with a large surface area such as carbon are suitable. In detail, reference can be made to the specialist knowledge.
  • the recyclable materials separated from the aqueous phase are the portion expelled from the recyclable material in the drying zone, which can be directly re-combined with the dried solid material with a microporous structure. If desired, any additional auxiliaries and valuable substances - for example additional aroma components - can be introduced into the microporous solid material. It is obvious: the teaching according to the invention opens up access to high-quality drying products, in particular also in the field of food and beverages with technologically simple work tools that have not previously been available in the field concerned.
  • the processing of the vapor partial stream withdrawn from the drying process in the sense described so far does not exhaust the technical possibilities of teaching the invention.
  • An important partial aspect of the invention is to ensure the continued use of this vapor part current and thus the evaporated water portion of the disperse phase in the sense of an improved overall process.
  • the separated vapor partial flow is to be used in particular as additional working aid in at least one further stage of the overall process.
  • Typical examples of such an additional use of the withdrawn vapor stream are the partial evaporation of the flowable raw material feed using the amount of energy contained in the vapor stream, the exhaust Carrying of aroma substances from the feed material prior to spray drying it and / or very generally the energy transfer from the vapor flow to the material to be heated or fractions thereof.
  • the teaching according to the invention aims to ensure that the step of discharging steam-volatile aroma substances is ensured as far as possible before the aqueous valuable substance is introduced into the spray-drying zone.
  • the superheated steam of the vapor stream is, according to technology known per se, ideally suited to at least largely achieve the desired goal in preparatory work stages and thus to arrive at flavor concentrates which can be stored temporarily and subsequently combined with the microporous dry material.
  • the technical advantage of this modification of the teaching according to the invention is of multiple forms: on the one hand, a pre-concentration of water vapor-liquid flavoring substances succeeds under adjustable working conditions.
  • the at least extensive discharge of the steam-volatile portion of the aroma substances from the aqueous material succeeds, which must be introduced into the drying zone and treated there with the superheated steam.
  • the excessive thermal load on the flavoring substances in this working stage is prevented by their partial circulation in admixture with the circulating flow of the superheated steam which is repeatedly heated up to the operating temperature.
  • the drying process according to the invention can be carried out in one stage with respect to the drying stage, depending on the temperature sensitivity of the material or mixture of materials to be dried, but if desired also in several stages. If the material is treated in several stages, at least one of these processing stages is spray drying and / or fluidized bed drying of the disperse material phase in superheated steam in the sense of the teaching according to the invention.
  • the Work within the meaning of this teaching provides, in particular, to combine spray drying with a subsequent agglomeration and / or drying stage, in particular as part of a post-treatment in the fluidized bed and / or in the fluidized bed, these secondary work steps being provided separately from the spray zone or else in Form of integrated work stages can be directly linked to spray drying.
  • Particularly important representatives of valuable substances and mixtures of valuable substances for processing within the meaning of the invention are aqueous feedstocks in the field of dairy products, aqueous feedstocks based on foodstuffs containing volatile aromatic compounds (food and beverages) and feedstocks providing flavor and / or odorants, for example the area of plants containing spices and / or parts of plants such as leaves, fruits and / or seeds.
  • feedstocks providing flavor and / or odorants, for example the area of plants containing spices and / or parts of plants such as leaves, fruits and / or seeds.
  • the teaching of the invention thus covers in particular food or feed suitable for human and / or animal consumption and auxiliary substances suitable for this purpose in the form of an at least largely dried solid carrier which may have been subjected to further physiologically compatible auxiliary substances and / or valuable substances.
  • these foodstuffs or feedstuffs are characterized in that the solid carrier, in the dried but not yet acted upon state, is provided with an absorbent porous internal structure and has been produced by drying a water-containing nutrient or a corresponding nutrient mixture in superheated steam as the drying gas.
  • Agents of the type mentioned here are characterized in particular in that the solid support with a porous internal structure has been produced by spray and / or fluidized-bed drying of a flowable wet material, in particular by drying aqueous solutions, emulsions and / or suspensions of the valuable substances forming the solid support is.
  • dried porous supports are particularly preferred which are in the temperature range of about 100 to 110 ° C as a solid and their plasticity and surface stickiness are restricted in this temperature range in such a way that substantial bonding of the particles to one another and / or bonding of their open-pored inner structure does not or not at all even under the conditions of the action of the superheated steam substantial extent occur.
  • the finished products according to the invention contain auxiliaries and / or valuable materials applied to the porous carrier - also referred to below as "application mass" - which are at least substantially introduced into the porous inner structure of the carrier. It may be preferred that at least 10% by volume, expediently at least 50% by volume, based on the accessible internal volume of the porous support, is coated with the coating composition. In an important embodiment of the invention it is provided that no or only a limited amount of application mass is present on the outer surfaces of the porous carrier. Not only can a particularly effective protective function of the solid carrier against the application mass be used here, it is in particular possible to substantially increase the storage stability of the dried mixture of valuable substances even for storage under difficult conditions.
  • the teaching according to the invention provides for the porous carrier material, which has been dried to give free-flowing material, to be applied in at least one subsequent working step with a preparation of the application composition which is flowable at the application temperature and preferably to be impregnated therewith.
  • the material loaded with auxiliary and / or valuable materials can then be covered with a cover layer and in particular sealed in a storage-stable manner.
  • the selection of the material of this covering layer and the technology used for applying this covering layer in each individual case is determined by the respective resource, by the loads to be taken into account of the resource to be protected, in the sense of general specialist knowledge, to which express reference is made here. Examples are also given below.
  • Dried solids the application masses of which have only been entered in traces into the microporous basic structure, for example in the range below about 1% by weight, based on the dry weight of the porous carrier solid fall within the scope of the invention.
  • a classic example of this is the known application of solubilizing auxiliaries to dry milk powder.
  • the scope of the invention includes dry products to which the application composition has been added in substantial amounts or up to the maximum fillability of the porous carrier grain. Understandably, the teaching of the invention also includes substance mixtures in which secondary components or application composition have also been added in larger amounts than they correspond to the accessible inner volume of the porous solid support.
  • the dry products according to the invention are preferably in the form of storage-stable, pourable and free-flowing masses which, if necessary, have been dried again after the good application of the second stage, the content of unbound residual water preferably being less than 10% by weight. %, in particular not more than 5% by weight, is% by weight, based on the loaded carrier solid.
  • the setting of lower residual water contents, as are often required in practice, is currently possible.
  • the residual water content of a coffee extract dried to powder can be at most about 4% by weight or less, residual water contents in milk and milk products can be selected at a maximum of 3% by weight.
  • the teaching according to the invention thus provides in a particularly important embodiment the use of spray drying a disperse aqueous valuable material in cocurrent and / or countercurrent in superheated steam as drying gas for the production of free-flowing and free-flowing dry products in the field of dairy products, in particular for Production of dry milk in powder and / or agglomerate form, with corresponding products with instant properties being preferred.
  • this relates to the use of spray and / or fluidized bed drying of a disperse aqueous valuable material in cocurrent and / or countercurrent in superheated water.
  • serdampf as drying gas for the production of free-flowing and free-flowing dry products in the field of coffee and coffee extracts, corresponding decaffeinated or coffee substitute products, tea and tea extracts, vegetable and / or fruit powder, dry soups and sauces, cocoa, cocoa / Milk or fruit / milk preparations, vitamin / fruit or fruit flavor combinations.
  • the invention furthermore relates to the correspondingly produced products based on dry milk and dry milk products, on the one hand, and dry coffee or coffee extract in pourable and pourable form, in particular with instant character, and the corresponding forms of preparation of tea and tea extracts, cocoa, vegetables - and fruit powders, dry soups and sauces, optionally in a mixture with other water-soluble components from the field of food and beverages.
  • An important object of the invention are flavor concentrates in the form of pourable and free-flowing solid powder and / or agglomerates, containing a porous carrier solid, produced by drying an aqueous preparation of a physiologically compatible value and / or value that is solid in the temperature range from about 100 to 110 ° C.
  • Excipient in particular from the field of food and beverages, produced in particular by spray and / or fluidized-bed drying of aqueous preparations of the carrier material with superheated steam as the drying gas, subsequent loading of the porous carrier with liquid and / or solid aroma substances and their flowable substances Preparations and preferably final wrapping of the carrier filled with flavorings with a physiologically compatible and storage-tight coating.
  • Carbohydrate compounds which can be used in a variety of forms both as valuable substances and in particular as auxiliary substances in the sense of the teaching according to the invention are both monosaccharides, in particular pentoses and hexoses, for example ribose or glucose, oligosaccharides, to which sugar with 2 to 6 acetal-like compounds is usually present connected monosaccharide units and polysaccharides.
  • oligosaccharides are di-saccharide compounds of the type of cane sugar, malt sugar and milk sugar.
  • Typical representatives for the class of polysaccharides are high-molecular natural substances, for example of the type of starch, glycogen and cellulose, which, as derivatives and / or compounds partially degraded in molecular weight, are typical representatives of the fields concerned here for valuable substances, valuable substance mixtures and auxiliary substances are in the sense of the teaching according to the invention.
  • cheese, casein and caseinates also fall into the field of milk-based foods or dairy products, as well as corresponding synthetic representatives such as coffee whiteners.
  • synthetic representatives such as coffee whiteners.
  • Typical examples of representatives from the field of plant extracts and comparable foodstuffs or flavorings are plant proteins and protein hydrolysates, soy milk and soy paste, pasty preparations of cooked or also uncooked vegetable plants such as potatoes, beets, in each case in pure form or as, in addition to the representatives previously mentioned Preparation, for example in the form of corresponding soups, cereals and cereal products, legumes, fruits and fruit products, but also, of course, also foodstuffs or flavorings based on animals, in particular based on meat and extracts obtained therefrom, blood and other customary products Recyclable material of origin.
  • auxiliaries and / or valuable substances are, for example, vitamins, natural or synthetic blood serums and blood substitutes, such as plasma / plasma substitutes, vaccines, pain relievers, antibiotics and the like.
  • blood substitutes such as plasma / plasma substitutes, vaccines, pain relievers, antibiotics and the like.
  • auxiliaries are used in practice which, in the sense of the teaching according to the invention, can also be used in the drying and / or can be used for subsequent coating of the porous solid body laden with flavorings.
  • auxiliary substances are in particular polysaccharides, for example gum arabic, maltodextrins and modified starches. Formation of inclusion complexes with cyclodextrins is also contemplated.
  • FIG. 1 shows the drying zone 1, shown here as a spray tower.
  • the water-containing material to be dried is fed to the head of the spray tower by means of the pump 3 via line 4 and finely divided here via the distribution device (s) 2.
  • the discharge device 5 for the dry material is located at the foot of the spray tower.
  • Superheated steam is fed in direct current by means of the fan 6 via the lines 10 and 12 into the head of the spray tower. This superheated steam flow is heated to the required operating temperature by indirect heating in FIG. 11.
  • the superheated steam stream loaded with the evaporated water portion leaves the drying zone via line 7 and passes the separating device 8 for entrained solid matter, shown here as a cyclone, at the foot of which the discharge device 9 is provided for discharging the separated solid portion. At the top of this cyclone, the superheated steam freed from solid matter is fed to the fan 6.
  • the solid matter discharged via 5 from the spray tower and via 9 from the cyclone is fed via lines 13 and 14 to a subsequent treatment in the fluid
  • the vapor component corresponding to the vaporized water content is removed via line 16, passed through the heat exchanger 17 and partially condensed here.
  • this partial condensation for example 5 to 95% by weight and in particular 5 to 50% by weight of the vapor part stream can be converted into the liquid phase.
  • the condensed portion of the vapor stream is withdrawn from the heat exchanger 17 via line 19, its non-condensed portion is fed via line 57 to the washing and separation column 18.
  • the liquid phase obtained at the bottom of this washing and separation column is combined with the vapor condensate drawn off via line 19 and fed to the membrane separation unit 21 via the heat exchanger 20.
  • the non-volatile fraction of the volatile components discharged from the valuable material to be dried with the vapor component is drawn off in concentrated form from the membrane separation stage via line 22 by means of the pump 23 and applied to the solid material post-treated here via line 24 and the dividing device 25 in the fluidized bed 15 , for example sprayed on.
  • the recombined dried valuable material leaves the fluidized bed via 26.
  • the stream of the water obtained during drying in the membrane separation system 21 is removed via 27.
  • the gaseous component withdrawn from the washing and rectification column 18 passes through the heat exchanger 28.
  • the liquid material condensed here is returned via line 29 to the top of the column 18, which is filled, for example, with conventional packings.
  • the uncondensed gaseous fraction is drawn off by means of the fan 30 via line 31 and fed to the burner 32, which is in indirect heat exchange with the superheated steam flow circulated via line 33 and the heat exchanger 11.
  • the burner exhaust gases are partly circulated by the fan 34 for better heat utilization.
  • the rest of the fuel gas is discharged via 36, before - again for better energy utilization - a heat exchange in 35 with the burner supply air is provided, which is also drawn in via the fan 30 and fed to the burner.
  • FIG. 1 provides for the gas phase emerging from the top of the washing and separation column 18, by means of the blower 37 and the line 38, a recombination of this portion of, for example, particularly volatile aromatic substances with the circulating stream of the superheated steam before it Reentry into the drying zone.
  • the drying and processing of the aqueous material to be processed and previously described is assigned a pretreatment stage which is used, for example, to concentrate an aqueous material and / or to separate at least a substantial proportion of volatile aroma substances before the aqueous material is introduced into the drying zone .
  • the condensation energy from the (partial) condensation of the withdrawn vapor part stream in the heat exchanger 17 is used or carried out to carry out this pretreatment.
  • Drying zone 1 is preceded by a work step for concentrating the aqueous fresh material supplied via line 40.
  • This preconcentration takes place in a thin-film evaporator 39, which is kept under (partial) vacuum by means of the fan 41.
  • the thin film evaporator is provided with a double jacket 43.
  • the pump 42 By means of the pump 42, the heat of condensation of the vapor part current accumulating in the heat exchanger 17 becomes the double jacket 43 of the thin-film evaporator via lines 46, 49 and 47 fed.
  • the liquid phase used for heat transfer is drawn off again via 48 and fed back into the heat exchanger 17 via line 50.
  • the discharge rate from the thin film evaporator can be regulated via the heat exchanger 45.
  • the vapor or gaseous phase drawn off is removed via 44.
  • FIG. 1 also indicates an alternative possibility for the further refinement of recombined mixtures of valuable materials from dried material and valuable substances, in particular aroma substances, separated from the vapor phase.
  • the flavor concentrate withdrawn from the membrane separation 21 can be fed by means of the pump 51 via line 52 to a continuously operated coater system 53/54 shown here in two stages. Dried solid to be loaded and to be coated is removed from the discharge devices 5 and 9, for example — in the form not shown in detail in the figure — and fed to the work stages 53 and, if appropriate, 54. However, the solid material from 26, which has already been loaded with a portion of the aroma substance, can also be subjected to this aftertreatment. Via 55, a preparation of the coating material is fed to work step 53 and distributed on the surface of the valuable material stored, for example, on turntables or disks. The final coated goods are discharged over 56.
  • FIG. 2 shows a modification of the processing of the vapor part stream, which can be of particular importance if a large proportion of volatile aroma substances is obtained in the course of the drying stage.
  • the drying zone 1 which in turn is operated in cocurrent, is the aqueous material to be dried via 4 and the dividing device (s) 2 fed. Finely divided dry material is discharged via 5 and line 13.
  • the superheated superheated steam stream laden with the evaporated water leaves the dryer 1 via line 7 and is fed back here to the separation stage 8 for the separation of entrained solid material.
  • the solids fraction separated here leaves the system via 9 and line 14.
  • the blower 6 feeds the superheated steam flow, which has in the meantime been heated up again to the operating temperature, back into the drying zone 1 via the lines 10 and 12.
  • the vapor partial flow corresponding to the evaporated water portion is drawn off via 16 and is almost completely condensed in the heat exchanger 17.
  • the resulting liquid phase is introduced via line 61 into the bottom of the rectification column 62.
  • Gaseous residual fractions leave the heat exchanger 17 via line 58.
  • the cooling stage 59 which is again provided, the last condensable residues of the vapor part stream are transferred into the liquid phase and are likewise introduced into the rectification column 62.
  • the remaining small proportion of permanent gas phase is withdrawn above 60, it can either be fed to the burner or - if there are sufficient valuable substance components - returned to the spray tower.
  • the condensate of the withdrawn vapor stream obtained in 17 is subjected to material separation in the rectification column 62; the condensation energy obtained in 17 is used to operate the rectification column.
  • the liquid phase is drawn off from the bottom of this column by means of pump 63 and partly passed via line 64 into the indirect heat exchanger 17 and from here back into the column via line 65.
  • Non-volatile valuable substances in particular the non-volatile fraction of hot steam-volatile aromas, accumulate in the liquid material obtained at the bottom of column 62. From the liquid circuit guided by means of the pump 63, the proportion of corresponding aroma substances over 66 obtained in the continuous process can be discharged.
  • the gas phase leaves the top of the separation column via line 67 under the influence of fan 69.
  • This gaseous fraction passes through heat exchanger 68, which in the preferred embodiment is designed such that virtually total condensation of the valuable materials still to be recovered here or recyclables.
  • the gaseous fractions which are now remaining are disposed of in the manner already stated several times.
  • the liquid phase obtained in the condenser 68 is drawn off over 70.
  • FIG. 2 shows the alternative to the additional separation via the membrane process both for the proportion of the low-volatility flavoring substances to be taken off at the bottom of the separation column 62 and for the light-volatile flavoring substances to be removed at the top of this column.
  • the portion of the liquid phase drawn off by means of the pump 63 and not to be circulated is fed to the membrane separation 73 via line 79, and the concentrate of low-volatility aroma substances which is formed is removed via 74.
  • the aqueous portion can be returned to the bottom of column 62 via line 75.
  • the condensate of the cooler 68 can accordingly be introduced into the membrane separation stage 46.
  • the resulting concentrate of the highly volatile aroma substances is removed via 77, while the freed aqueous permeate can be recycled via 78 into the top of the separation column.
  • FIG. 3 shows an embodiment for particularly effective pre-cleaning and separation of the aqueous material to be subjected to drying.
  • the vapor part stream drawn off from the circuit of the superheated steam used as the drying medium is used as strip steam in an upstream rectification column for the greatest possible removal of portions of the mixture of recyclable materials which are capable of steam absorption.
  • the variant of the method according to the invention can thus be optimized, as far as possible a separation of the valuable material to be dried into steam vapors. portions and correspondingly non-volatile portions before the aqueous valuable phase is fed to the drying step in the superheated steam.
  • Carrying out the step of drying of the valuable material in the spray tower 1 and the circulation of the superheated steam by means of the fan 6 via the intermediate stages 7, 8, 10, indirectly working heater 11 and recirculating via 12 into the spray tower and the feeding of the aqueous valuable material in the drying zone 1 via line 4 - by means of pump 90 - and distribution device (s) 2 corresponds to the representations from FIGS. 1 and 2. The same applies to the discharge of the finely divided solid material via 5 or 9 from the spray zone and Separation device for the separation of entrained solid material.
  • the vapor partial stream drawn off over 16 is now fed to the bottom of a strip or rectification column 80.
  • the aqueous fresh material to be subjected to the treatment is introduced into this rectification column via 81.
  • the column is equipped in a manner known per se with elements for intensifying the phase or mass exchange - for example with appropriate packings.
  • the vapor part stream used as strip steam is brought to intensive exchange in this column with the aqueous feed material, the vapor phase absorbs the volatiles of the feed material which are volatile in steam, in particular the corresponding aromatic substances, and leaves the top of the column with them via 82.
  • the stripping steam loaded with aroma substances passes through the cooling stage 84.
  • the steam portion drawn off at the top of the column is condensed to the aqueous phase, at the same time the comparatively less volatile portions of the recycled materials stripped off with the superheated steam pass into the condensate phase.
  • the condensate can be partly returned to the top of the rectification column via 85.
  • a significant proportion of the separated flavor concentrate is removed via 86 and reused in the sense of the teaching according to the invention, in particular combined again with the dried-on solid fraction.
  • the gas phase portion of the stripped product drawn off via the ventilator 83 can also contain valuable substances which are then again, for example, via a membrane seal. driving are separable, as has already been mentioned several times in the description of the invention.
  • FIG. 3 shows the alternative possibility of the subsequent concentration via the membrane separation method for the flavor concentrate drawn off over 86.
  • the aqueous aroma concentrate is fed to the membrane system 87.
  • the aqueous per-eat phase is drawn off at 88, while the concentrated flavor substance phase can be taken off at 89.
  • FIG. 4 finally shows a schematic representation of the processing of the vapor stream by adsorption / desorption treatment, known per se, of the vapor stream 16 loaded with valuable substances on an adsorption material with a large surface area, in particular activated carbon in the adder towers 91 and 92
  • these towers are used alternately for the adsorption of the valuable substances or for their desorption with, for example, saturated steam.
  • this figure consciously only refers to characteristic additional elements in the sense of the inventive action.
  • the superheated steam of the vapor stream passing through the tower switched to adsorption is removed via line 99 and subjected to the most complete condensation possible in the condenser 93.
  • the resulting wastewater is discharged over 94, small portions of a possibly remaining gaseous phase over 100 can be drawn off and disposed of in the manner described above - for example burned or returned to the drying cycle.
  • the steam stream leaving the tower connected to desorption and loaded with the separated valuable materials leaves the separation device via line 98 and can, for example, be subjected to a downstream membrane separation 95.
  • the flavor concentrate is taken from over 96.
  • the aqueous permeate leaves the plant via 97.
  • a skimmed milk concentrate with 48% by weight solids was converted into a free-flowing milk powder.
  • the milk concentrate was sprayed via a two-component nozzle according to the "fountain principle", i.e. sprayed upwards through a spray nozzle arranged in the lower part of the spray tower.
  • the superheated steam as drying gas flows from top to bottom through the spray tower. Thus, drying was carried out simultaneously in cocurrent and countercurrent.
  • the superheated steam was circulated. After drying, the temperature of the superheated steam was above the condensation temperature of water at normal pressure, i.e. above 100 ° C.
  • the entrained fine particles were separated in a cyclone and by a bag filter.
  • the steam is then electrically superheated to the required drying temperature and used again as the drying gas.
  • the water evaporated from the milk solution was removed from the circuit after the filter. This vapor stream could be worked up again in a rectification column.
  • the water portion evaporated in a structured packing column and was removed as distillate. The higher boiling constituents formed the concentrate in the bottom of the column.
  • the bulk weight of the powdered milk was 250 g / l.
  • the residual moisture was 2% by weight.
  • the spray-dried product is characterized by very good flowability and water solubility.
  • Example 1 The procedure was as in Example 1.
  • the milk concentrate with a dry matter content of 40% by weight consisted of whole milk.
  • the milk contained a higher fat content.
  • the milk powder spray-dried with superheated steam was again characterized by very good pourability and solubility.
  • Example 3 The procedure was as in Example 3, i.e. the drying was carried out according to the direct current principle. A coffee extract with a dry matter content of 51.5% was used as the starting material. The following operating parameters have been set:
  • Extract throughput 7.3 kg / h
  • Temperature of the extract before spraying 58 ° C
  • Oxygen content in the circuit 0.4 vol.%
  • the bulk weight of the coffee powder was 210 g / 1, the residual moisture was 4%.

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Abstract

La présente invention concerne l'application du procédé de séchage par de la vapeur d'eau surchauffée, comme gaz de séchage, de substances recyclables dispersées, à des substances recyclables et à des préparations de substances recyclables du domaine des substances nutritives, en particulier des aliments et des substances de base destinées à leur fabrication, des préparations contenant des substances aromatiques, des préparations du domaine des substances auxilaires et/ou substances recyclables cosmétiques et pharmaceutiques, ainsi qu'au domaine des herbicides, fongicides et insecticides. L'invention concerne le procédé de séchage proprement dit, et également des agents contenant des substances valables et des mélanges de substances recyclables des domaines mentionnés, sous forme de produits séchés à la vapeur.
PCT/EP1994/002528 1993-08-09 1994-07-29 Utilisation de vapeur d'eau surchauffee pour le sechage, pratiquement exempt de gaz perdus, de substances recyclables et de melanges de substances recyclables sensibles a la temperature, et produits secs ainsi fabriques ayant des proprietes ameliorees WO1995004579A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP7506204A JPH09501098A (ja) 1993-08-09 1994-07-29 回収可能な物質およびその温度感受性混合物の廃ガスが実質的に存在しない乾燥のための過熱水蒸気の使用ならびにそのように製造される向上特性を有する乾燥生成物
EP94924823A EP0713412A1 (fr) 1993-08-09 1994-07-29 Utilisation de vapeur d'eau surchauffee pour le sechage, pratiquement exempt de gaz perdus, de substances recyclables et de melanges de substances recyclables sensibles a la temperature, et produits secs ainsi fabriques ayant des proprietes ameliorees

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEP4326468.9 1993-08-09
DE4326468A DE4326468A1 (de) 1993-08-09 1993-08-09 Verwendung von überhitztem Wasserdampf zur praktisch abgasfreien Trocknung von Wertstoffen und temperatursensitiven Wertstoffgemischen und damit hergestellte Trockenprodukte mit verbesserten Eigenschaften

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WO1995004579A1 true WO1995004579A1 (fr) 1995-02-16

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FR2754269A1 (fr) * 1996-10-04 1998-04-10 Rhodia Chimie Sa Procede de preparation d'une composition comprenant une substance thermosensible
RU2324872C1 (ru) * 2006-10-13 2008-05-20 Олег Савельевич Кочетов Распылительная сушилка
RU2324876C1 (ru) * 2006-11-14 2008-05-20 Олег Савельевич Кочетов Распылительная сушилка
RU2328671C1 (ru) * 2007-01-09 2008-07-10 Олег Савельевич Кочетов Распылительная сушилка
RU2341743C1 (ru) * 2007-07-03 2008-12-20 Олег Савельевич Кочетов Распылительная сушилка типа импульс
US10006714B2 (en) 2007-08-07 2018-06-26 Mars, Incorporated Apparatus for drying a material
CN110613943A (zh) * 2019-10-22 2019-12-27 无锡市华立石化工程有限公司 自过滤蒸发器系统

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CN110613943B (zh) * 2019-10-22 2024-04-26 无锡华立聚能装备有限公司 自过滤蒸发器系统

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