Process for carefully preparing plant extracts.
Abstract
Es wird ein Verfahren zur schonenden Herstellung von Pflanzenextrakten, und insbesondere von qualitativ hochwertigem Kaffee-Extrakt durch mehrstufige Kaltextraktion von gemahlenem Röstkaffee beschrieben. Durch stufenweises Vermahlen der festen Bestandteile in wässriger Aufschlämmung bis zu kolloidaler Feinheit in der zweiten und dritten Extraktionsstufe kann bei niedrigen Temperaturen eine hohe Gesamtausbeute erzielt werden. Der Rückstand kann gegebenenfalls einer Hochtemperatur-Kurzzeit-Behandlung unterworfen werden.
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20 claims: 16 independent, 4 dependent
- 1Verfahren zur Herstellung von Kaffee-Extrakt durch Extrahieren von gemahlenem Röstkaffee mit kaltem Wasser, dadurch gekennzeichnet, daß man a) Röstkaffee, vermahlen zu einer üblichen Partikelgröße von 0,2 bis 2 mm, in kaltem Wasser aufschlämmt und nach Extraktion der löslichen Bestandteile die wäßrige Phase von den festen Bestandteilen abtrennt und sammelt und b) die festen Bestandteile aus Stufe a) einer weiteren Vermahlung in kaltem Wasser bis zu einer mittleren Partikelgröße von 50 bis 200 µm unterwirft und nach Extraktion der löslichen Bestandteile die wäßrige Phase von den festen Bestandteilen abtrennt und sammelt.
- 2Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß man den Röstkaffee für Stufe a) in kaltem Wasser mahlt.
- 3Verfahren nach den Ansprüchen 1 oder 2, dadurch gekennzeichnet, daß man c) die festen Bestandteile aus den Stufen a) und/oder b) einer zusätzlichen Vermahlung in kaltem Wasser bis zum Erreichen einer mittleren Partikelgröße von 5 bis 150 µm unterwirft und nach Extraktion der löslichen Bestandteile die wäßrige Phase von den festen Bestandteilen abtrennt und sammelt.
- 4Verfahren nach den Ansprüchen 1 bis 3, dadurch gekennzeichnet, daß man die nach der Vermahlung in den Stufen b) und/oder c) erhaltenen Aufschlämmungen anschließend einer Ultraschall-Behandlung unterwirft.
- 5Verfahren nach den Ansprüchen 1 bis 4, dadurch gekenn zeichnet, daß die Temperatur des zum Aufschlämmen der festen Bestandteile in den Stufen a), b) und gegebenenfalls c) verwendeten Wassers 0 bis 40, vorzugsweise 5 bis 25 und in besonders bevorzugter Weise 8 bis 12°C beträgt.
- 6Verfahren nach den Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß die mittlere Partikelgröße in Stufe a) 200 bis 400 µm beträgt.
- 7Verfahren den Ansprüchen 1 bis 6, dadurch gekennzeichnet, daß die mittlere Partikelgröße in Stufe b) 150 bis 200 µm beträgt.
- 8Verfahren nach den Ansprüchen 1 bis 7, dadurch gekennzeichnet, daß die mittlere Partikelgröße in Stufe c) 50 bis 150 µm beträgt.
- 9Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß die Aufschlämmungen in Stufe a) einen Trockenstoffgehalt von 20 bis 60 Gew.%, vorzugsweise etwa 40 Gew.% und in den Stufen b) und c) einen Trockenstoffgehalt von 10 bis 30, vorzugsweise etwa 20 Gew.% aufweisen.
- 10Verfahren den Ansprüchen 1 bis 9, dadurch gekennzeichnet, daß man das Wasser in den Stufen a), b) und gegebenenfalls c) vor dem Abtrennen 5 bis 300 Sekunden, vorzugsweise etwa 200 Sekunden lang auf die festen Bestandteile einwirken läßt.
- 11Verfahren nach den Ansprüchen 1 bis 10, dadurch gekennzeichnet, daß man d) die festen Bestandteile aus den Stufen b) und/oder c) in Wasser aufschlämmt, einer Temperatur-Behandlung bei Temperaturen im Bereich von 150 bis 200°C unterwirft und die wäßrige Phase von den festen Bestandteilen abtrennt und sammelt.
- 12Verfahren nach den Ansprüchen 1 bis 10, dadurch gekennzeichnet, daß man d) die festen Bestandteile aus den Stufen b) und/oder c) in Wasser aufschlämmt und einer Hochtemperatur-Kurzzeit-Behandlung bei Temperaturen im Bereich von von 200 bis 400°C über einen Zeitraum von 5 Minuten bis 0,01 Sekunden unterwirft.
- 13Verfahren nach den Ansprüchen 1 bis 12, dadurch gekennzeichnet, daß man die in den Stufen a), b), c) und/oder d) gesammelten wäßrigen Phasen getrennt oder vereinigt einer Nachklärung in einer Vorrichtung unterwirft, die das gleichzeitige Abtrennen des Kafffee-Öls zuläßt.
- 14Verfahren nach den Ansprüchen 1 bis 13, dadurch gekennzeichnet, daß man das Verfahren kontinuierlich durchführt, indem man i) den Röstkaffee sowie die festen Bestandteile aus den Stufen a) bis d) der jeweils folgenden Verfahrensstufe kontinuierlich durch geeignete Fördereinrichtungen zuführt und ii) die wäßrigen Phasen aus den Stufen a) bis d) kontinuierlich sammelt.
- 15Verfahren nach Anspruch 14, dadurch gekennzeichnet, daß man die wäßrige Phase aus Stufe c) in die Stufe b) rückführt.
- 16Verfahren nach den Ansprüchen 1 bis 15, dadurch gekennzeichnet, daß man die in den Stufen a), b), c) und/oder d) gesammelten wäßrigen Phasen getrennt oder vereinigt durch Evaporieren und/oder Membranbehandlung und/oder Gefrierkonzentrieren aufkonzentriert.
- 17Verfahren nach den Ansprüchen 1 bis 16, dadurch gekennzeichnet, daß man die in den Stufen a), b), c) und/oder d) gesammelten wäßrigen Phasen getrennt oder vereinigt bis zu einem Restwassergehalt von 2 - 4 Gew.% trocknet.
- 18Verfahren nach Anspruch 17, dadurch gekennzeichnet, daß die Trocknung durch Gefriertrocknen erfolgt.
- 19Verfahren nach den Ansprüchen 1 bis 16, dadurch gekennzeichnet, daß man die in den Stufen a), b), c) und/oder d) gesammelten wäßrigen Phasen getrennt oder vereinigt durch Tiefgefrieren stabilisiert.
- 20Verwendung der aus den Stufen a), b) und gegebenenfalls c) des Verfahrens nach den Ansprüchen 1 bis 10 und 13 is 18 gewonnenen Kaffee-Extrakte zum Aromatisieren von für den menschlichen Verzehr geeigneten Produkten und/oder zum Veredeln von Pulverkaffee.
Independent claims20
58 paragraphs, as filed
The invention relates to a process for the gentle preparation of plant extracts and, in particular for the gentle preparation of high-quality coffee extract by cold extraction of ground roasted coffee.
Aqueous coffee extract is the starting material for the production of instant coffee, a powder which is completely or substantially soluble in water. The production in the industrial scale is generally carried out in such a manner that 5 to 8 are filled with ground coffee columns connected in series, and extracted in counter-current process at temperatures of 120 to 200 ° C and elevated pressures, with fresh extractant in each of the largely extracted column is passed. After completion of extraction, the first column is disconnected and filled with fresh coffee column at the end downstream (see RJ Clark and R. McRae, Coffee, vol. 2:. Technology, Elsevier Applied Sciences, pages 109-133 (1987)). According to this method, although good extract yields can be achieved, the quality of the obtained extract and thus of the final product instant coffee, however, suffers as a result of application of high temperatures and pressures. For one thing, while the volatile aromatic substances are lost or adversely changed, and on the other hand, the microstructure of the coffee will be destroyed, and there are formed or released substances which interfere with the flavor impact (see. Page 126, paragraph 2 supra) ,
To improve the quality of coffee extract has been proposed, the temperature and the pressure in the past, the freshest coffee containing column so to
result that a balance between the vapor phase and the liquid phase occurs. Thereafter, the vapor phase containing the volatile aromatic substances, which are added after condensing the extract (see. U.S. Patent No. 3,700,463). However, the process can only lead to a slight improvement in taste, because the entire process is still carried out under high temperatures and pressures.
In U.S. Patent 3,788,860 a modification of the initially described Column extraction method is described in which each the freshest columns and especially the one from which the liquid is drawn off, is filled with whole coffee beans. The beans should be at a late stage as possible and at the latest before moving into the autoclave level ground. The quality of the withdrawn from the whole beans extract to be significantly better than that of extracts which are extracted from ground coffee. The process is technically complex, as it makes the emptying of the filled columns whole beans, the subsequent milling of whole beans and the re-filling of columns with the crushed beans required. A continuous carrying out this method is not possible.
Finally, US-PS 3,682,649 a process for the cold extraction of roasted coffee is described, can be obtained at the relatively small amounts of high-quality coffee extract. After coarsely ground (see. Example 1), roasted coffee with cold water and the mixture is allowed to stand for 5 to 15 minutes. The mixture is then subjected to pressures bar 69-828 to obtain an aqueous extract. The remaining residue is re-used as a normal coffee, that is, it is sold as either ground coffee, or else used in conventional extraction columns for the recovery of coffee extract. The method is thus only the "levy" a small amount of flavor and aroma, which are soluble in water under the conditions selected. It is also cumbersome and difficult to implement because of the partially extracted coffee as such is hardly marketable. It is necessary to fill the wet Kaffeebrei in extraction columns or dry these to facilitate handling prior to filling. In both cases, costly and technically complex measures are needed in order to realize the partially extracted coffee on.
There is so far no economic method for producing large quantities of high-quality coffee extract, in which on the one hand the taste, visual and sensory characteristics of freshly brewed coffee can be achieved and which on the other hand produces yields that are comparable to those in conventional column extraction.
It is accordingly an object of the invention to provide a gentle, but at the same time economical and feasible on an industrial scale process, by means of which high-quality coffee extract may be produced, the freshly brewed coffee is comparable in quality.
To achieve the object of the invention cold-extraction method is proposed to extreme in which, contrary to the previously recommended in the prior art procedure (see above) Coffee gradually in aqueous slurry, ie colloidal fineness ground and is extracted cold.
The starting material for the novel process is roasted ground coffee having an average particle size of 0.2 to 2 mm. The grinding can be carried out in a conventional manner by grinding the dry roasted beans; preferably the average particle size of the coffee in the output stage (stage a)) of the inventive process 200 to 400 microns. The coffee is then slurried in cold water and, after extraction of the soluble components the aqueous phase is separated and collected from the solid components.
According to a particularly preferred embodiment of the invention, the whole roasted beans are at the beginning of the process combined with cold water and milled in water up to the above particle size. For grinding the water-added whole roasted coffee beans, for example, is a Nemo-Macerator, as it is brought by Netsch on the market.
Preferably, in step a) of milled roast coffee is metered dry or wet via a conveying screw into a mixing device, which is simultaneously fed to the cold water. For the purposes of the present invention, cold water temperatures of 0 to 40, preferably 5 to 25 and particularly preferably 8 to 12 ° C.
The ratio of water to roasted coffee should be selected so that the dry matter content of the slurry produced in the mixing device 20 to 60 and preferably about 40 wt.% Is. However, it can also be carried out with more or less water. Usually, the ratio of water to roast coffee 1: 1 to 5: 1 and preferably 2: 1 to 3: 1.
The required residence time of the slurry in the mixer is extremely short. Thus, it is sufficient if the water before phase separation is applied 5 to 300 seconds, and preferably about 200 seconds on the solid constituents.
the slurry is fed to an apparatus suitable for liquid-solid separation device from the mixer. The separation can in principle be carried out by any suitable method, for example by pressing, centrifuging or decanting.
According to a particularly preferred embodiment of the invention, the separation is carried out in a sieve centrifuge. For this purpose, for example Siebmantelzentrifugen, screen centrifuges, peeler centrifuges, Druckfilter- or reversible-filter centrifuge can be used. Particularly suitable a SCREENBOWL centrifuge has proven.
The aqueous extract obtained in step a) is collected during the residue according to the invention subsequently fed to a step b) mixer and is reslurried in cold water. The slurry is, for example, by weight on a dry matter content of about 10 to 30 and preferably about 20.% Adjusted and then fed to a colloidal milling to a particle size in the range of 50 to 200 and preferably 150 to 200 microns. For this purpose, for example, colloid mills or ball mills have been successful.
The slurry of microfine ground residue in step b) is subsequently fed as indicated above to step a) a separation device. Also in this stage, the use of a centrifuge and a particular SCREENBOWL centrifuge has been found to be particularly suitable.
The obtained in step b) aqueous extract contains more quality flavorings and extract components as they were a cold extraction previously inaccessible.
According to a particularly preferred embodiment of the invention, the process after step b) is in a subsequent to that stage c) is repeated by the solid components of step b) again passed into a mixer, and to specify to a dry matter content as for step b), are mixed with cold water. The slurry is subjected to an additional fine grinding to a mean particle size of 5 to 150 microns, and preferably up to 50 to 150 microns. For this purpose, in turn, a colloid mill, preferably, be used a toothed colloid mill or a ball mill. To achieve particle sizes below 100 microns, a homogeniser or a ball mill, should be used. The slurry is as in steps a) and b) a separating device described fed and separated and collected the aqueous phase from the solid components.
According to the invention, it is also possible to supply the solid components of step a) in whole or in part, directly to step c). According to a particularly preferred embodiment of the invention, the slurry is c) treated in the steps b) and c) and in particular in stage subsequent to the colloidal grinding with ultrasound. To this end, known Ultraschalldesintegratoren can be used as they are available on the market, for example under the name Sonifier Ⓡ. Following the ultrasonic treatment, the slurry is separated as described above in aqueous phase and solid components and is collected, the aqueous phase.
The extract obtained in the step c) has a relatively low dry substance concentration. According to a particularly preferred embodiment of the invention, it is accordingly returned to the stage b), where it can be co-used to suspend the from step a) originating, solid components or.
The temperature of the slurrying the solid components in steps a), b) and c water used) is 0 to 40, preferably 5 to 25 and particularly preferably 8 to 120 ° C. The temperature of the slurry in the various stages of the process should be, if appropriate, by cooling in the temperature ranges given above. As already explained above, it is sufficient if the water is applied 5 to 300 seconds in the individual process stages on the solid constituents. The extract extraction accordingly takes place within a very short time, and it is also avoided in this way damage to the flavorings.
The extracts obtained in steps a), b) and optionally c) may according to the invention separately or combined of a secondary clarification are subjected to separate the coffee oil on the one hand and coarse particulate matter on the other hand. For this purpose, for example a 3-phase decanter centrifuge and / or a separator may be used.
The freed of coffee oil and suspended matter can now extract by known methods to the desired concentration, preferably to a dry matter content of 30 to 50 wt.%, Can be accommodated. Concentration may be effected for example by vacuum evaporation (evaporation), by membrane treatment such as ultrafiltration or reverse osmosis and by freeze concentration.
Further, the extracts can be dried separately or combined. In this respect, freeze-drying% has up to a residual water content of about 2 to 4 wt. Proven particularly suitable. It also discusses other drying methods such as spray drying, into consideration. Further, the extracts can be stabilized by freezing, for example in the form of granules.
The extracts from the steps a), b) and optionally c) of the inventive process contain surprisingly substantially the full range of coffee constituents that determine the flavor and other sensory characteristics of freshly brewed coffee percent with a yield of about 20 to 30th %, relative to the roast coffee used. The extracts are excellently suitable for finishing conventionally prepared instant coffee and they can also for flavoring for human consumption before seen products such as drinks, desserts, biscuits and confectionery, as well as substances for use in the pharmaceutical field are used.
To obtain an instant coffee matrix also can the solid components of steps a), b) and / or c) are digested in a subsequent step d) to convert the higher molecular weight carbohydrates in the soluble compounds.
This can be done by conventional heat treatment at temperatures between 150 to 200 ° C. To this end, is slurried in a conventional manner, the solids obtained in the respective stages during centrifugation in water, preferably a dry matter content of about 20 wt.% Is set. The slurry is heated in a known manner under pressure at 150 to 200 ° C and the mass after cooling as in steps a) and b) a liquid-solid separation described supplied. The extract has a dry substance content of about 3 to 10 wt.%, With the yield based on the raw coffee used 10 to 20 percent at this stage.% May be.
According to a particularly preferred embodiment of the invention, the solid ingredients in stage d) are lysed by subjecting them to a high temperature short time treatment at temperatures in the range of 200 to 400 ° C over a period of 5 to 0.01 seconds. This can for example be carried out by transferring the slurry in a pressure vessel and injected via a nozzle superheated steam or an inert gas. However, there may be other sources of concentrated energy such as microwaves, lasers and the like used for short-term heating.
The extract obtained in step d) can be released separately or described together with the extracts from the preceding steps as above and concentrated or dried or frozen. If the extracts were combined from the steps a) to d) and dried to an instant coffee with very good quality and in a yield of 30 to 45 percent is.%, Based on the obtained roasted coffee used.
Preferably, the inventive method is carried out continuously. For this purpose, the starting material and the solid component is conveyed by suitable conveying means in each case to the next following process step. For transportation of roasted coffee in step a) can be used for example a screw conveyor with a flexible hose. The transport of the solid components from the respective separation stages in the downstream mixer can be done by a known screw in the separation device, while the slurries are preferably transported from the mixers by pumping. The extracts may continuously from the separation devices of the various process stages by a Nachkläranlage are collected as a 3-phase decanter and directed separately or combined. At the same time can be collected continuously that while coffee oil.
As described above in particular within the continuous process flow the aqueous phase from step c) are recycled into stage b) and the residue from the final clarification of the extracts can be co-processed in step d). In this way a closed continuous process flow is created in which only the beginning, the starting material is fed, and the solid components of step d) are discarded at the end. The duration of a cycle is under the above conditions only about 15 to 20 minutes, while for the extraction of a corresponding quantity of water in conventional column method about 120 minutes are required.
The inventive multi-stage extraction process has therefore the ability to achieve fast and extremely gentle way coffee extract of the highest quality in a high yield. As set forth above, in the steps a) to c) with an overall yield of about 20 to 30 wt.% Are calculated relative to the roast coffee used. Step d) can further 10 to 15 wt.% Provide components of the extract, so that, when carrying out the overall process, a yield of about 40 to 45 wt.%, Can be obtained relative to the roast coffee used.
The inventively produced product forms an instant coffee with superior properties in terms of its flavor and fragrances one hand, and its viscosity and mouthfeel imparted on the other hand.
According to the invention, therefore, an extremely rapid and economical method has been created, which allows the production of coffee extract highest quality level in previously untapped yields.
The method is explained below with reference to examples.
example 1
100 kg of roasted, ground coffee filter fine (mix Robusta / Arabica 80:20) were added with stirring 250 liters of water at a temperature of 15 ° C. The slurry was stirred gently for 2 minutes. They had a dry matter content of about 38 wt.% To.
The mixture was transferred to a reversible-filter centrifuge and centrifuged at 1500 g. There 190 liters of an aqueous extract obtained with a dry matter content of 10% based accordingly 19% yield to the roast coffee used.
The amount of the residue was 160 kg. a second slurry having a dry substance content was 20 percent by adding 245 kg of water. received%. This was first in a colloid mill (Gear mill) and then to a homogenizer (high-pressure, 700 bar) passed. The size of the particles in the slurry was about 10 to 40 microns.
Subsequently, the slurry was separated as previously described in a reversible-filter centrifuge in the aqueous extract and residue. 229.5 l aqueous extract%% yield were having a dry matter content of 6 wt. Percent correspondingly 13.7. Obtained relative to the roast coffee used.
The amount of the residue was 156.23 kg. By adding 159.92 kg of water, a slurry% was again with a dry matter content of about 20 wt. Prepared. The mixture was heated in a pressure vessel at 10 to 11 bar at 180 ° C, cooled and centrifuged as described above. Here l 190.5% aqueous extract were having a dry matter content of 6 wt. Based accordingly 11.43% yield to the roast coffee used.
The extract yield relative to the roast coffee used is summarized in the table below. <tables id="tabl0001" num="0001"><table frame="all"><title>table</title><tgroup cols="4" colsep="1" rowsep="0"><colspec colnum="1" colname="col1" colwidth="39.37mm" /><colspec colnum="2" colname="col2" colwidth="39.37mm" /><colspec colnum="3" colname="col3" colwidth="39.37mm" /><colspec colnum="4" colname="col4" colwidth="39.37mm" /><thead valign="top"><row><entry namest="col1" nameend="col1" /><entry namest="col2" nameend="col2" align="center">volume extract</entry><entry namest="col3" nameend="col3" align="center">TS extract</entry><entry namest="col4" nameend="col4" align="center">Total extract</entry></row></thead><tbody valign="top"><row><entry namest="col1" nameend="col1" align="left">Step a)</entry><entry namest="col2" nameend="col2" align="char" char=",">190 l</entry><entry namest="col3" nameend="col3" align="right">10%</entry><entry namest="col4" nameend="col4" align="char" char=",">19.00 kg</entry></row><row><entry namest="col1" nameend="col1" align="left">Step b)</entry><entry namest="col2" nameend="col2" align="char" char=",">229.5 l</entry><entry namest="col3" nameend="col3" align="right">6%</entry><entry namest="col4" nameend="col4" align="char" char=",">13.77 kg</entry></row><row><entry namest="col1" nameend="col1" align="left">Step d)</entry><entry namest="col2" nameend="col2" align="char" char=",">190.5 l</entry><entry namest="col3" nameend="col3" align="right">6%</entry><entry namest="col4" nameend="col4" align="char" char=","><u>11.43 kg</u></entry></row><row><entry namest="col1" nameend="col1" /><entry namest="col2" nameend="col2" /><entry namest="col3" nameend="col3" /><entry namest="col4" nameend="col4" align="char" char=",">44.10 kg</entry></row></tbody></tgroup></table></tables> As the table shows, a total of about 33% of the roast coffee used were gained as an extract Retired in stages a) and b). The total yield was 40.43 kg coffee extract as dry matter related corresponding 44.1% to the roast coffee used, these extracts still contained the while coffee oil and small amounts of other, removable in the final sedimentation fines.
example 2
Roasted coffee having an average particle size of about 200 to 400 microns was passed in at a rate of 120 kg / hr by a screw conveyor in a Ruberg-mixer (mixer I). Before the mixer tap water having a temperature of about 15 ° C in an amount of 160 l / h was fed into the line. The slurry formed in the mixer had a dry matter content of about 40% and a temperature was 20 to 21 ° C to. the slurry was continuously supplied to a screen screw centrifuge (Centrifuge I) with a Siebporendurchmesser of 150 microns and separated into an aqueous phase and solid components from the mixer I. The aqueous phase whose dry matter content about 12 to 13% wt. Was, was passed to a collection vessel I. The solids were again transferred to a Ruberg-mixer (mixer II), wherein the recycled aqueous phase was fed from the subsequent separation stage just before the mixer II (see below) with a metering rate of about 230 l / h in the line. The dry matter content of the slurry in the mixer II was about 20 wt.%.
The slurry was continuously passed through a Mohno-pump to a colloid mill (Colloid Mill I) from the mixer II, in which the particle size of the solid ingredients have been reduced to an average of about 150 to 200 microns. From colloid mill I, the slurry was then passed to a screen screw centrifuge II with a Siebporendurchmesser of 100 microns and separated into aqueous phase and solid components. The aqueous phase, which had a dry matter content of about 6.5 to 7%, was also fed into the collection I.
The solids from the centrifuge II were as described above led to a colloid mill II with the addition of cold water temperature indicated in at a rate of 250 l / h in a Ruberg-mixer (mixer III) and from there via a Mohno Pump II in which the particle size of the solid components has been reduced to an average of about 100 to 150 microns. The mixture was passed through an ultrasonic disintegrator (Sonifier Ⓡ and following it, separated the aqueous phase in a Screen bowl III from the solid components.
The aqueous phase from the centrifuge III was fed through a decanter I as already mentioned above in the line immediately before the mixer and II was continuously to the slurry of the solid components from the centrifuge I.
The solids from the centrifuge III as well as the sludge from decanters I were like the foregoing steps described led to a mixer IV and slurried with water. The dry matter content of the slurry in the mixer IV was about 18 wt.%. The mixture was passed through a pump into a pressure vessel V which has been fed via a nozzle at a pressure of 8 bar with steam at a temperature of 170 ° C. The residence time of the mixture in the pressure vessel was about 40 to 50 seconds. It was then passed through a cooler into a depressurization vessel and then pumped into a 3-phase decanter by a pump VI with a capacity of about 500 l / h. The dry matter content of the mixture was at this stage about 12 wt.%, And had a temperature 90 to 100 ° C.
After separating the mixture into solid components, coffee oil and aqueous phases, the solid constituents were discarded as waste, collected the coffee oil and the aqueous phase, hereinafter referred to as "hot extract", passed through a cooler into a collection vessel II.
The combined in the collecting vessel I aqueous phases from the centrifuges I and II, referred to as "cold extract" (dry matter content about 7-9 wt.%) Were also fed to the secondary clarification to a 3-phase decanter and in aqueous phase, coffee -Oil and sludge separated.
The sludge was returned to the mixer and subjected to IV together with the solid constituents from the screen centrifuge III the temperature treatment described above.
The clarified cold extract was combined with the clarified hot extract by reverse osmosis containing up to a dry matter content of 40.% Concentrated, cooled to 3 to 5 ° C and then freeze-dried.
The total yield of coffee extract as dry matter averaged about 40 percent.% Relative to the roast coffee used, with about 25 wt.% On the cold extract and about 15 wt.% To the hot extract accounted for.
The duration of a cycle by feeding the starting material to the ejection of the drop in the connection to the hot extraction was about 18 minutes.
example 3
The freeze-dried end product according to Example 1 was tasted as instant coffee, wherein in each case about 2.5 g of the product were dissolved in 180 ml of hot water. There was obtained a coffee, its viscosity and mouthfeel consistent with the corresponding properties of freshly brewed coffee and its taste and flavor have been designated in the tasting by a panel of experts as excellent (grade 1).
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Members11
| Document | Office | Kind | |
|---|---|---|---|
| FI892592A | Finland | A | |
| EP0343678A2This record | European Patent Office (EPO) | A2 | |
| DE3818035A1 | Germany | A1 | |
| DE3818035C2 | Germany | C2 | |
| JPH0297356A | Japan | A | |
| EP0343678A3 | European Patent Office (EPO) | A3 | |
| KR900017492A | Republic of Korea | A | |
| EP0343678B1 | European Patent Office (EPO) | B1 | |
| AT87178T | Austria | T | |
| DE58903865D1 | Germany | D1 | |
| JP2001017083A | Japan | A |
32 legal events, as 2 offices reported them to INPADOC
Over the term
Point at a mark for the eventEvents
| Event | Code | Office | |
|---|---|---|---|
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Annual fee paid to national office [announced via postgrant information from national office to epo]GrantedPGFP | PGFP | EP | |
| No opposition filedOpposition26N | 26N | EP | |
| Patent ceasedCeasedPL | PL | CH | |
| No opposition filed within time limitOppositionORIGINAL CODE: 0009261PLBE | PLBE | EP | |
| Information on the status of an ep patent application or granted ep patentGrantedSTATUS: NO OPPOSITION FILED WITHIN TIME LIMITSTAA | STAA | EP | |
| Gb: ep patent (uk) treated as always having been void in accordance with gb section 77(7)/1977 [no translation filed]GBV | GBV | EP | |
| Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents actLapsedNLV1 | NLV1 | EP | |
| Fr: translation not filedEN | EN | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Corresponds to:REF | REF | EP | |
| Designated contracting statesAK | AK | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Lapsed in a contracting state [announced via postgrant information from national office to epo]LapsedPG25 | PG25 | EP | |
| Corresponds to:REF | REF | EP | |
| (expected) grantORIGINAL CODE: 0009210GRAA | GRAA | EP | |
| First examination report despatched17Q | 17Q | EP | |
| Party data changed (applicant data changed or rights of an application transferred)RAP1 | RAP1 | EP | |
| Request for examination filed17P | 17P | EP | |
| Designated contracting statesAK | AK | EP | |
| Search report despatchedORIGINAL CODE: 0009013PUAL | PUAL | EP | |
| Designated contracting statesAK | AK | EP | |
| Public reference made under article 153(3) epc to a published international application that has entered the european phaseORIGINAL CODE: 0009012PUAI | PUAI | EP |
Numbers
- Publication
- 0343678
- Publication, DOCDB
- 0343678
- Publication, EPODOC
- EP0343678
- Application
- 89109520
- Application, DOCDB
- 89109520
- Application, EPODOC
- EP19890109520
Titles3
- German
- Verfahren zur schonenden Herstellung von Pflanzenextrakten
- English
- Process for carefully preparing plant extracts
- French
- Procédé de préparation ménagée d'extraits de plantes
Classification
- CPC, 2
- A23F5/26
- A23F5/08
- IPC, 5
- A23F5 24
- A23F5 08
- A23F5 26
- A23F5 28
- A23F5 32
Designated states1
- Contracting states, 1
- Sweden