WO1989003240A1 - Process and plant for clarifying liquids, in particular raw juice - Google Patents

Process and plant for clarifying liquids, in particular raw juice Download PDF

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Publication number
WO1989003240A1
WO1989003240A1 PCT/CH1988/000191 CH8800191W WO8903240A1 WO 1989003240 A1 WO1989003240 A1 WO 1989003240A1 CH 8800191 W CH8800191 W CH 8800191W WO 8903240 A1 WO8903240 A1 WO 8903240A1
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WO
WIPO (PCT)
Prior art keywords
cross
flow filtration
filtration device
retentate
plant according
Prior art date
Application number
PCT/CH1988/000191
Other languages
German (de)
French (fr)
Inventor
Walter Gresch
Original Assignee
Bucher-Guyer Ag Maschinenfabrik
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Filing date
Publication date
Application filed by Bucher-Guyer Ag Maschinenfabrik filed Critical Bucher-Guyer Ag Maschinenfabrik
Publication of WO1989003240A1 publication Critical patent/WO1989003240A1/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/149—Multistep processes comprising different kinds of membrane processes selected from ultrafiltration or microfiltration
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/70—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter
    • A23L2/72—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by filtration
    • A23L2/74—Clarifying or fining of non-alcoholic beverages; Removing unwanted matter by filtration using membranes, e.g. osmosis, ultrafiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
    • B01D29/01—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with flat filtering elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
    • B01D29/50—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition
    • B01D29/52—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition in parallel connection
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
    • B01D29/88—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices
    • B01D29/94—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for discharging the filter cake, e.g. chutes
    • B01D29/945—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for discharging the filter cake, e.g. chutes for continuously discharging concentrated liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
    • B01D35/12—Devices for taking out of action one or more units of multi- unit filters, e.g. for regeneration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D37/00—Processes of filtration
    • B01D37/03—Processes of filtration using flocculating agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration
    • B01D61/146—Ultrafiltration comprising multiple ultrafiltration steps
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12H—PASTEURISATION, STERILISATION, PRESERVATION, PURIFICATION, CLARIFICATION OR AGEING OF ALCOHOLIC BEVERAGES; METHODS FOR ALTERING THE ALCOHOL CONTENT OF FERMENTED SOLUTIONS OR ALCOHOLIC BEVERAGES
    • C12H3/00—Methods for reducing the alcohol content of fermented solutions or alcoholic beverage to obtain low alcohol or non-alcoholic beverages
    • C12H3/04—Methods for reducing the alcohol content of fermented solutions or alcoholic beverage to obtain low alcohol or non-alcoholic beverages using semi-permeable membranes

Definitions

  • the invention relates to a method and a system for clarifying liquids, in particular raw juice from fruit, grapes, berries or other fruits, vegetables and seeds or wine by means of cross-flow filtration and a device for reducing the cloudiness in the pension.
  • a prerequisite for the production of a uniformly clear product is that all membranes have the same separation limit. As a result, however, the average filtration capacity or the average flux decreases, which, compared to semi-continuous systems, leads to systems with a large membrane area and is very expensive.
  • at least three stages are necessary for optimal operation. This means, especially in the case of small and medium-sized plant sizes, higher acquisition costs and more complicated operation of the plant.
  • the last stage runs continuously with the highest concentration factor and thereby jeopardizes problem-free operation of the system with regard to blockage of the modules.
  • the invention is based on the object of avoiding the disadvantages mentioned and of creating a method of the type mentioned at the outset which, in a simple and inexpensive manner, enables a reduction in the turbidity content in the retentate and thereby an improvement in the filtration performance and the yield .
  • this object is achieved in that retentate is subjected to the cross-flow filtration at least one second coarser cross-flow filtration and the permeate from the second or further cross-flow filtration is returned to the retentate side of the first cross-flow filtration.
  • the first crossflow filtration is carried out by ultra or microfiltration tion and the second cross-flow filtration by micro or coarse filtration.
  • Finishing agents can be added to the retentate before or during the filtration in the second cross-flow filtration in order to reduce the tendency of the membranes to clog.
  • the system for carrying out the method consists of a first crossflow filtration device, the retentate side of which is connected via a line to the retentate side of a second crossflow filtration device, a line leading from the permeate side of the second crossflow filtration device to the retentate side of the first crossflow filtration device.
  • the pore size of the membrane of the second crossflow filtration device is larger than .. the pore size of the membrane of the second crossflow filtration device.
  • the second cross-flow filtration device is advantageously equipped with micro- or coarse filtration membranes.
  • the pore size is approximately 0.1 to 20 ⁇ m.
  • the second cross-flow filtration device In order to be able to work with the highest possible pressures in the micro or coarse filtration of the second cross-flow filtration device, the latter is equipped with metal or ceramic modules, the permissible transmembrane pressure of which is greater than with the filtration modules of the first cross-flow filtration device.
  • the maximum transmembrane pressure of the metal or ceramic modules is preferably at least 6 bar.
  • the channel cross section of the filtration modules of the second crossflow filtration device is larger than that of the filtration modules of the first crossflow filtration device.
  • the second crossflow filtration device is advantageously equipped with tube modules which have a tube diameter of at least 6 mm.
  • the advantages achieved by the invention are, in particular, that a high flux with a small membrane area is achieved by the coarse filtration in the second crossflow filtration device, with less membrane surface means a reduction in the investment costs.
  • the metal membranes used for the higher pressures and coarser separation limit of the second crossflow filtration device which are not or only costly to manufacture for small separation limits, can be combined with relatively inexpensive plastic membranes for the first crossflow filtration device.
  • the use of membranes instead of the known side-stream centrifuge to reduce the sludge content results in better selectivity.
  • the trub content in the retentate is greatly reduced and the yield is improved.
  • the service life of the first cross-flow filtration device until cleaning is extended in the case of relatively modest additional investments and the service life of the membrane is increased.
  • a high concentration factor only occurs towards the end of the process cycle.
  • the raw juice to be clarified is fed via a feed line 1 to a first crossflow filtration device 2, which consists of an ultra or a microfiltration device.
  • the clear juice is separated from the residue on a membrane surface 3 of the crossflow filtration device 2 and discharged through a permeate discharge line 4 to a collection point.
  • Cheap plastic modules for low pressures are used for the membrane surface 3.
  • a line 5 for retentate leads to a second crossflow filtration device 6, which consists of a micro or coarse filtration device.
  • the membrane surface 7 of the cross-flow filtration device 6 is preferably formed by metal or ceramic modules which have a larger pore size of approximately 0.1 to 20 ⁇ m compared to the plastic modules of the first cross-flow filtration device 2. Since higher pressures are used in coarse filtration than in ultrafiltration in cross-flow filtration device 2, the metal or ceramic modules are designed for a maximum transmembrane pressure of more than 6 bar.
  • the channel cross sections of the coarse filtration modules are also larger than those of the first crossflow filtration device 2.
  • tube modules with a tube diameter of at least 6 mm are used.
  • the permeate separated off on the membrane surface 7 of the crossflow filtration device 6 is returned via a line 8 to the retentate side of the first crossflow filtration device 2.
  • From the retentate side of the two- A cross-flow filtration device 6 branches off a line 9 through which the residual retentate is discharged.
  • a circuit is created in which the turbidity, which is continuously removed via line 9, is considerably reduced.
  • continuous supply of raw juice via the supply line 1 continuous operation with a constant turbidity content is achieved when the cross-flow filtration device 2 is rented.
  • the trub content in the retentate of the crossflow filtration device 6 only increases drastically towards the end of the process cycle, so that this production phase can be monitored with little effort.
  • the retentate can be treated with fining agents before the membrane filtration system 6.
  • fining agents preferably by means of a mixing nozzle 10, for example an injection nozzle or by static mixing, into the retentate line 5.
  • the resulting agglomerates between macromolecules and beauty agents can be used by means of the second membrane filter disconnect trations worn 6.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Food Science & Technology (AREA)
  • Genetics & Genomics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Biochemistry (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Nutrition Science (AREA)
  • Polymers & Plastics (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

In a process for clarifying raw juice, the residue from a first cross-flow filtration device (2) is introduced into the residue side of a second cross-flow filtration device (6), the membrane surface (7) of the latter (6) having a greater pore size than the membrane surface (3) of the former (2). The permeate from the second cross-flow filtration device (6) is recycled to the residue side of the first cross-flow filtration device (2), thereby creating a circuit (2, 5, 6, 8) in which the turbidity is substantially reduced due to continuous discharge of the remaining residue through the pipe (9). The result is improved filtration efficiency and yield for a relatively low investment.

Description

Verfahren zur Klärung von Flüssigkeiten, insbesondere Rohsaft, sowie Anlage zur Durchführung des VerfahrensProcess for clarifying liquids, in particular raw juice, and system for carrying out the process
Die Erfindung betrifft ein Verfahren und eine Anlage zur Klärung von Flüssigkeiten, insbesondere Rohsaft aus Obst, Trauben, Beeren oder anderen Früchten, Gemü¬ sen und Saaten oder Wein mittels Querstromfiltration und einer Einrichtung zur Reduzierung des Trübes im Re- tentat.The invention relates to a method and a system for clarifying liquids, in particular raw juice from fruit, grapes, berries or other fruits, vegetables and seeds or wine by means of cross-flow filtration and a device for reducing the cloudiness in the pension.
Durch die Aufkonzentrierung im Retentatkreiεlauf einer im Batch- oder semikontinuierlichen Verfahren betriebe¬ nen Querstromfiltrationsanlage steigt der Trubanteil im Retentat mit zunehmender Filtrationszeit an. Die Fol¬ ge davon ist eine sinkende Filtrationsleistung und ver¬ ringerte Ausbeute. Ausserdem ist die Standzeit der Quer¬ stromfiltration bis zur Reinigung der Membran relativ kurz. Die Anzahl der Reinigungs-Zyklen, die für die Mem¬ bran die Hauptbelastung darstellen, wirkt sich auf die Lebensdauer der Membran nachteilig aus.As a result of the concentration in the retentate circuit of a cross-flow filtration system operated in a batch or semi-continuous process, the proportion of trub in the retentate increases with increasing filtration time. The consequence of this is a decrease in filtration performance and a reduced yield. In addition, the lifetime of the cross-flow filtration until the membrane is cleaned is relatively short. The number of cleaning cycles, which represent the main stress for the membrane, has a disadvantageous effect on the service life of the membrane.
Um diesen Schwierigkeiten entgegenzutreten, ist es be¬ kannt, im Retentatkreislauf der Querstromfiltrationsan¬ lage eine Seitenstrom-Zentrifuge anzuordnen, durch die ein grosser Teil des Trübes vom Retentat abgetrennt wird. Nachteilig hierbei ist jedoch, dass der abgetrennte Trub- schlamm noch relativ feucht ist und dadurch noch keine optimale Verbesserung der Ausbeute erzielt wird. Hinzu kommen Entsorgungsprobleme bei der Beseitigung des Trub- schlamms und die relativ hohen Anschaffungskosten für die Seitenstrom-Zentrifuge, die ausserdem sehr lärmin¬ tensiv ist. Ferner ist es bekannt, Querstromfiltrationseinrichtun- gen in mehreren Stufen hintereinander anzuordnen, um gegenüber den Batch- oder semikontinuierlichen Anlagen mit nur einer Filtrationsstufe einen kontinuierlichen Betrieb zu erreichen. Dabei wird jeweils das Retentat der vorhergehenden Stufe in die Retentatseite der nächs¬ ten Stufe eingeleitet. Voraussetzung für die Herstellung eines einheitlich klaren Produktes ist, dass alle Mem¬ branen dieselbe Trenngrenze aufweisen. Dadurch nimmt aber die mittlere Filtrationsleistung bzw. der mittlere Flux ab, was gegenüber semikontinuierlichen Anlagen zu Anlagen mit viel Membranflächen führt und sehr teuer ist. Ausserdem sind für einen optimalen Betrieb mindes¬ tens drei Stufen nötig. Dies bedeutet besonders bei klei¬ nen und mittleren Anlagegrössen höhere Anschaffungskoε- ten und komplizierteres Betreiben der Anlage. Hinzu kommt, dass die letzte Stufe ständig mit höchstem Konzentrations¬ faktor fährt und dadurch einen problemlosen Betrieb der Anlage, hinsichtlich Verstopfung der Module, gefährdet.In order to counteract these difficulties, it is known to arrange a side-stream centrifuge in the retentate circuit of the cross-flow filtration system, through which a large part of the sludge is separated from the retentate. The disadvantage here, however, is that the separated sludge is still relatively moist and therefore no optimal improvement in the yield is achieved. In addition, there are disposal problems in the removal of the sludge and the relatively high purchase costs for the side-stream centrifuge, which is also very noisy. Furthermore, it is known to arrange cross-flow filtration devices in several stages one after the other in order to achieve continuous operation compared to batch or semi-continuous systems with only one filtration stage. The retentate of the previous stage is introduced into the retentate page of the next stage. A prerequisite for the production of a uniformly clear product is that all membranes have the same separation limit. As a result, however, the average filtration capacity or the average flux decreases, which, compared to semi-continuous systems, leads to systems with a large membrane area and is very expensive. In addition, at least three stages are necessary for optimal operation. This means, especially in the case of small and medium-sized plant sizes, higher acquisition costs and more complicated operation of the plant. In addition, the last stage runs continuously with the highest concentration factor and thereby jeopardizes problem-free operation of the system with regard to blockage of the modules.
Der Erfindung liegt die Aufgabe zugrunde, die genannten Nachteile zu vermeiden und ein Verfahren der eingangs erwähnten Art zu schaffen, das auf einfache und kosten¬ günstige Art und Weise eine Reduzierung des Trubgehalts im Retentat und dadurch eine Verbesserung der Filtrations¬ leistung und der Ausbeute ermöglicht.The invention is based on the object of avoiding the disadvantages mentioned and of creating a method of the type mentioned at the outset which, in a simple and inexpensive manner, enables a reduction in the turbidity content in the retentate and thereby an improvement in the filtration performance and the yield .
Gemäss der Erfindung wird diese Aufgabe dadurch gelöst, dass Retentat der Querstromfiltration mindestens einer zweiten gröberen Querstromfiltration unterzogen wird und das Permeat aus der zweiten oder weiteren Querεtrom- filtrationen zur Retentatseite der ersten Querstromfil¬ tration zurückgeführt wird.According to the invention, this object is achieved in that retentate is subjected to the cross-flow filtration at least one second coarser cross-flow filtration and the permeate from the second or further cross-flow filtration is returned to the retentate side of the first cross-flow filtration.
Nach einem weiteren Merkmal der Erfindung erfolgt die erste Querstromfiltration durch Ultra- oder Mikrofiltra- tion und die zweite Querstromfiltration durch Mikro- oder Grobfiltration.According to a further feature of the invention, the first crossflow filtration is carried out by ultra or microfiltration tion and the second cross-flow filtration by micro or coarse filtration.
Dem Retentat können vor oder während der Filtration, in der zweiten Querstromfiltration Schönungs ittel zu¬ geführt werden, um die Verstopfungstendenz der Membra¬ nen zu mindern.Finishing agents can be added to the retentate before or during the filtration in the second cross-flow filtration in order to reduce the tendency of the membranes to clog.
Die Anlage zur Durchführung des Verfahrens besteht aus einer ersten Querstromfiltrationseinrichtung, deren Re¬ tentatseite über eine Leitung mit der Retentatseite ei¬ ner zweiten Querstromfiltrationseinrichtung verbunden ist, wobei von der Permeatseite der zweiten Querstrom- filtrationseinrichtung eine Leitung zur Retentatseite der ersten Querstromfiltrationseinrichtung führt. Dabei ist gemäss der Erfindung die Porengrösse der Membran der zweiten Querstromfiltrationseinrichtung grösser als .. die Porengrösse der Membran der zweiten Querstromfiltra¬ tionseinrichtung.The system for carrying out the method consists of a first crossflow filtration device, the retentate side of which is connected via a line to the retentate side of a second crossflow filtration device, a line leading from the permeate side of the second crossflow filtration device to the retentate side of the first crossflow filtration device. According to the invention, the pore size of the membrane of the second crossflow filtration device is larger than .. the pore size of the membrane of the second crossflow filtration device.
Vorteilhafterweise ist die zweite Querstromfiltrations¬ einrichtung mit Mikro- oder Grobfiltrations-Membranen ausgerüstet. Dabei beträgt die Porengrösse ca. 0,1 bis 20 μm.The second cross-flow filtration device is advantageously equipped with micro- or coarse filtration membranes. The pore size is approximately 0.1 to 20 μm.
Um bei der Mikro- oder Grobfiltration der zweiten Quer¬ stromfiltrationseinrichtung mit möglichst hohen Drücken arbeiten zu können, ist diese mit Metall- oder Keramik- Modulen ausgerüstet, deren zulässiger Transmembrandruck grösser ist als bei den Filtrations-Modulen der ersten Querstromfiltrationseinrichtung.In order to be able to work with the highest possible pressures in the micro or coarse filtration of the second cross-flow filtration device, the latter is equipped with metal or ceramic modules, the permissible transmembrane pressure of which is greater than with the filtration modules of the first cross-flow filtration device.
Vorzugsweise beträgt der maximale Transmembrandruck der Metall- oder Keramik-Module mindestens 6 bar. Zur Vermeidung von Verstopfungen ist der Kanalguerschnitt der Filtrations-Module der zweiten Querstromfiltrations¬ einrichtung grösser als bei den Filtrations-Modulen der ersten Querstromfiltrationseinrichtung.The maximum transmembrane pressure of the metal or ceramic modules is preferably at least 6 bar. In order to avoid blockages, the channel cross section of the filtration modules of the second crossflow filtration device is larger than that of the filtration modules of the first crossflow filtration device.
Vorteilhafterweise ist die zweite Querstromfiltrations¬ einrichtung mit Rohr-Modulen ausgerüstet, die einen Rohr¬ durchmesser von mindestens 6 mm aufweisen.The second crossflow filtration device is advantageously equipped with tube modules which have a tube diameter of at least 6 mm.
Die mit der Erfindung erzielten Vorteile bestehen ins¬ besondere darin, dass durch die Grobfiltration in der zweiten Querstromfiltrationseinrichtung ein hoher Flux bei wenig Membranfläche erreicht wird, wobei weniger Membranϊlache eine Verringerung der Investitionskosten bedeutet. Ausserdem können die für die höheren Drücke und gröbere Trenngrenze der zweiten Querstromfiltrations¬ einrichtung verwendeten Metall-Membranen, die für kleine Trenngrenzen nicht oder nur aufwendig herstellbar sind, mit relativ billigen Kunststoff-Membranen für die erste QuerStromfiltrationseinrichtung kombiniert werden. Hin¬ zu kommt, dass mit dem Einsatz von Membranen anstelle der bekannten Seitenstrom-Zentrifuge zur Reduzierung des Trubgehalts eine bessere Trennschärfe erreicht wird. Durch die Rückführung des Permeats der zweiten Querstrom- filtrationseinrichtung zur Retentatseite der ersten Quer¬ stromfiltrationseinrichtung wird der Trubgehalt im Reten¬ tat stark reduziert und die Ausbeute verbessert. Die Standzeit der ersten Querstromfiltrationseinrichtung bis zur Reinigung wird bei relativ bescheidenen Mehrin¬ vestitionen verlängert und die Lebensdauer der Membran erhöht. Ein hoher Konzentrationsfaktor tritt erst gegen Ende des Verfahrenszyklus auf.The advantages achieved by the invention are, in particular, that a high flux with a small membrane area is achieved by the coarse filtration in the second crossflow filtration device, with less membrane surface means a reduction in the investment costs. In addition, the metal membranes used for the higher pressures and coarser separation limit of the second crossflow filtration device, which are not or only costly to manufacture for small separation limits, can be combined with relatively inexpensive plastic membranes for the first crossflow filtration device. In addition, the use of membranes instead of the known side-stream centrifuge to reduce the sludge content results in better selectivity. By recycling the permeate of the second cross-flow filtration device to the retentate side of the first cross-flow filtration device, the trub content in the retentate is greatly reduced and the yield is improved. The service life of the first cross-flow filtration device until cleaning is extended in the case of relatively modest additional investments and the service life of the membrane is increased. A high concentration factor only occurs towards the end of the process cycle.
Die Erfindung ist in der folgenden Beschreibung und der Zeichnung, die ein Ausführungsbeispiel darstellt, näher erläutert. Die einzige Figur der Zeichnung zeigt in sche- matischer Darstellung den Aufbau der erfindungsgemässen Anlage.The invention is closer in the following description and the drawing, which represents an embodiment explained. The only figure in the drawing shows a schematic representation of the structure of the system according to the invention.
Der zu klärende Rohsaft wird über eine Zuführleitung 1 einer ersten Querstromfiltrationseinrichtung 2, die aus einer Ultra- oder einer Mikrofiltrationseinrichtung besteht, zugeführt. An einer Membranfläche 3 der Quer¬ stromfiltrationseinrichtung 2 wird der Klarsaft vom Re¬ tentat abgetrennt und durch eine Permeatabflussleitung 4 zu einer Sammelstelle abgeführt. Für die Membranflä¬ che 3 werden billige Kunststoff-Module für niedrige Drük- ke verwendet. Von der Retentatseite der Querstromfiltra¬ tionseinrichtung 2 führt eine Leitung 5 für Retentat zu einer zweiten Querstromfiltrationseinrichtung 6, die aus einer Mikro- oder Grobfiltrationseinrichtung besteht. Die Membranfläche 7 der Querstromfiltrationseinrichtung 6 wird vorzugsweise durch Metall- oder Keramik-Module gebildet, die gegenüber den Kunststoff-Modulen der ers¬ ten Querstromfiltrationseinrichtung 2 eine grössere Po¬ rengrösse von ca. 0,1 bis 20 μm aufweisen. Da bei der Grobfiltration mit höheren Drücken gearbeitet wird als bei der Ultrafiltration in der Querstromfiltrationsein¬ richtung 2, sind die Metall- oder Keramik-Module für einen maximalen Transmembrandruck von mehr als 6 bar ausgelegt. Auch die Kanalquerschnitte der Grobfiltra- tions-Module sind grösser gewählt als bei der ersten Querstromfiltrationseinrichtung 2. Vorzugsweise werden Rohr-Module mit einem Rohrdurchmesser von mindestens 6 mm verwendet.The raw juice to be clarified is fed via a feed line 1 to a first crossflow filtration device 2, which consists of an ultra or a microfiltration device. The clear juice is separated from the residue on a membrane surface 3 of the crossflow filtration device 2 and discharged through a permeate discharge line 4 to a collection point. Cheap plastic modules for low pressures are used for the membrane surface 3. From the retentate side of the crossflow filtration device 2, a line 5 for retentate leads to a second crossflow filtration device 6, which consists of a micro or coarse filtration device. The membrane surface 7 of the cross-flow filtration device 6 is preferably formed by metal or ceramic modules which have a larger pore size of approximately 0.1 to 20 μm compared to the plastic modules of the first cross-flow filtration device 2. Since higher pressures are used in coarse filtration than in ultrafiltration in cross-flow filtration device 2, the metal or ceramic modules are designed for a maximum transmembrane pressure of more than 6 bar. The channel cross sections of the coarse filtration modules are also larger than those of the first crossflow filtration device 2. Preferably, tube modules with a tube diameter of at least 6 mm are used.
Das an der Membranfläche 7 der Querstromfiltrationsein¬ richtung 6 abgetrennte Permeat wird über eine Leitung 8 zur Retentatseite der ersten Querstromfiltrationsein¬ richtung 2 zurückgeführt. Von der Retentatseite der zwei- ten Querstromfiltrationseinrichtung 6 zweigt eine Lei¬ tung 9 ab, durch die das Restretentat abgeführt wird. Durch die Rückführung des Permeats zur ersten Querstrom- filtrationseinrichtung 2 entsteht ein Kreislauf, in dem der Trüb, der über die Leitung 9 ständig abgeführt wird, erheblich reduziert wird. Bei kontinuierlicher Zuführung von Rohsaft über die Zuführleitung 1 wird ein kontinuier¬ licher Betrieb mit einem konstanten Trubgehalt beim Re¬ tentat der Querstromfiltrationseinrichtung 2 erreicht. Bei Batch- oder semikontinuierlichem Betrieb erhöht sich der Trubgehalt beim Retentat der Querstromfiltrations¬ einrichtung 6 erst gegen Ende des Verfahrenszyklus dras¬ tisch, sodass sich diese Produktionsphase mit wenig Auf¬ wand überwachen lässt.The permeate separated off on the membrane surface 7 of the crossflow filtration device 6 is returned via a line 8 to the retentate side of the first crossflow filtration device 2. From the retentate side of the two- A cross-flow filtration device 6 branches off a line 9 through which the residual retentate is discharged. By returning the permeate to the first cross-flow filtration device 2, a circuit is created in which the turbidity, which is continuously removed via line 9, is considerably reduced. With continuous supply of raw juice via the supply line 1, continuous operation with a constant turbidity content is achieved when the cross-flow filtration device 2 is rented. In batch or semi-continuous operation, the trub content in the retentate of the crossflow filtration device 6 only increases drastically towards the end of the process cycle, so that this production phase can be monitored with little effort.
Um den Gehalt an makromolekularen Stoffen, z.B. Polyphe- nole, welche die Membranen der Membranfiltrationseinrich¬ tung 2 mit zunehmender Konzentration stärker verstopfen, im Retentat zu reduzieren und damit die Standzeit bis zur nächsten Reinigung der Filtrationsanlage weiter zu verlängern, kann vor der Membranfiltrationsanlage 6 das Retentat mit Schönungsmitteln behandelt werden. Zu die¬ sem Zwecke genügt eine Zudosierung von relativ geringen Mengen an Schönungsmitteln, vorzugsweise mittels einer Mischdüse 10, beispielsweise einer Injektionsdüse oder durch statisches Mischen, in die Retentatleitung 5. Die entstehenden Aglomerate zwischen Makromolekülen und Schö¬ nungsmitteln lassen sich mittels der zweiten Membranfil¬ trationseinrichtung 6 abtrennen. In order to determine the content of macromolecular substances, e.g. To reduce polyphenols in the retentate, which clog the membranes of the membrane filtration device 2 with increasing concentration, and thus further extend the service life until the next cleaning of the filtration system, the retentate can be treated with fining agents before the membrane filtration system 6. For this purpose, it is sufficient to add relatively small amounts of fining agents, preferably by means of a mixing nozzle 10, for example an injection nozzle or by static mixing, into the retentate line 5. The resulting agglomerates between macromolecules and beauty agents can be used by means of the second membrane filter disconnect trationseinrichtung 6.

Claims

P A T E N T A N S P R U E C H E PATENT CLAIMS
1. Verfahren zur Klärung von Flüssigkeiten, insbeson¬ dere Rohsaft aus Obst, Trauben, Beeren oder anderen Früchten, Gemüsen und Saaten oder Wein mittels Quer¬ stromfiltration und einer Einrichtung zur Reduzie¬ rung des Trübes im Retentat, dadurch gekennzeichnet, dass Retentat der Querstromfiltration mindestens einer zweiten, gröberen Querstromfiltration unter¬ zogen wird und das Permeat aus der zweiten oder weiteren Querstromfiltrationen zur Retentatseite der ersten Querstromfiltration zurückgeführt wird.1. Process for clarifying liquids, in particular raw juice from fruit, grapes, berries or other fruits, vegetables and seeds or wine by means of cross-flow filtration and a device for reducing the turbidity in the retentate, characterized in that retentate of the cross-flow filtration is subjected to at least one second, coarser cross-flow filtration and the permeate from the second or further cross-flow filtration is returned to the retentate side of the first cross-flow filtration.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die erste Querstromfiltration durch Ultra¬ oder Mikrofiltration und die zweite Querstromfil¬ tration durch Mikro- oder Grobfiltration erfolgt. 2. The method according to claim 1, characterized in that the first cross-flow filtration is carried out by ultra or microfiltration and the second cross-flow filtration is carried out by micro or coarse filtration.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass dem Retentat vor oder während der Filtration in der zweiten Querstromfiltration Schönungsmittel zugeführt werden.3. The method according to claim 1, characterized in that fining agents are added to the retentate before or during the filtration in the second cross-flow filtration.
4. Anlage zur Durchführung des Verfahrens nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass die Retentatseite einer ersten Querstromfiltrations¬ einrichtung (2) über eine Leitung (5) mit der Reten¬ tatseite einer zweiten Querstromfiltrationseinrich¬ tung (6) verbunden ist und von der Permeatseite der zweiten Querstromfiltrationseinrichtung (6) eine Leitung (8) zur Retentatseite der ersten Quer¬ stromfiltrationseinrichtung (2) zurückführt.4. System for carrying out the method according to one of claims 1 to 3, characterized in that the retentate side of a first cross-flow filtration device (2) is connected via a line (5) to the retentate side of a second cross-flow filtration device (6) and from the permeate side of the second crossflow filtration device (6) leads a line (8) back to the retentate side of the first crossflow filtration device (2).
5. Anlage nach Anspruch 4, dadurch gekennzeichnet, dass die Porengrösse der Membran (7) der zweiten Querstromfiltrationseinrichtung (6) grösser ist als die Porengrösse der Membran (3) der ersten Quer¬ stromfiltrationseinrichtung (2).5. Plant according to claim 4, characterized in that the pore size of the membrane (7) of the second cross-flow filtration device (6) is larger than the pore size of the membrane (3) of the first cross-flow filtration device (2).
6. Anlage nach einem der Ansprüche 4 und 5, dadurch gekennzeichnet, dass die erste Querstromfiltrations¬ einrichtung (2) mit Ultra- oder Mikrofiltrations- membranen und die zweite Querstromfiltrationsein¬ richtung (6) mit Mikro- oder Grobfiltrations-Mem- branen ausgerüstet ist. 6. Plant according to one of claims 4 and 5, characterized in that the first cross-flow filtration device (2) is equipped with ultra or microfiltration membranes and the second cross-flow filtration device (6) is equipped with micro or coarse filtration membranes .
7. Anlage nach einem der Ansprüche 4 bis 6, dadurch gekennzeichnet, dass die Porengrösse der Membran (7) der zweiten Querstromfiltrationseinrichtung (2) ca. 0,1 bis 20 μm beträgt.7. Plant according to one of claims 4 to 6, characterized in that the pore size of the membrane (7) of the second cross-flow filtration device (2) is approximately 0.1 to 20 microns.
8. Anlage nach einem der Ansprüche 4 bis 7, dadurch gekennzeichnet, dass die zweite Querstromfiltra¬ tionseinrichtung (6) mit Metall- oder Keramik- Modulen ausgerüstet ist, deren zulässiger Trans¬ membrandruck grösser ist als bei den Filtrations- Modulen der ersten Querstromfiltrationseinrich¬ tung (2).8. Plant according to one of claims 4 to 7, characterized in that the second cross-flow filtration device (6) is equipped with metal or ceramic modules, the permissible Trans¬ membrane pressure is greater than in the filtration modules of the first cross-flow filtration device tion (2).
9. Anlage nach Anspruch 8, dadurch gekennzeichnet, dass der maximale Transmembrandruck der Metall¬ oder Keramik-Module mindestens 6 bar beträgt.9. Plant according to claim 8, characterized in that the maximum transmembrane pressure of the metal or ceramic modules is at least 6 bar.
10. Anlage nach einem der Ansprüche 4 bis 9, dadurch gekennzeichnet, dass der Kanalquerschnitt der Fil¬ trations-Module der zweiten Querstromfiltrations¬ einrichtung (6) grösser ist als bei den Filtra¬ tions-Modulen der ersten Querstromfiltrationsein¬ richtung (2 ) .10. Plant according to one of claims 4 to 9, characterized in that the channel cross section of the filtration modules of the second cross-flow filtration device (6) is larger than in the filtration modules of the first cross-flow filtration device (2).
11. Anlage nach einem der Ansprüche 4 bis 10, dadurch gekennzeichnet, dass die zweite Querstromfiltra- tionseinrichtung (6) mit Rohr-Modulen ausgerüstet ist, die einen Rohrdurchmesser von mindestens 6mm aufweisen.11. Plant according to one of claims 4 to 10, characterized in that the second cross-flow filter tion device (6) is equipped with tube modules that have a tube diameter of at least 6mm.
12. Anlage nach einem der Ansprüche 4 bis 11, dadurch gekennzeichnet, dass die Retentatleitung (5) mit einer Schönungsmittel führenden Leitung verbindbar ist.12. Plant according to one of claims 4 to 11, characterized in that the retentate line (5) can be connected to a line carrying fining agent.
13. Anlage nach Anspruch 12, dadurch gekennzeichnet, dass eine Mischdüse oder ein Statischmischer zur Schönungsmittelzufuhr vorgesehen ist. 13. Plant according to claim 12, characterized in that a mixing nozzle or a static mixer is provided for the fining agent supply.
PCT/CH1988/000191 1987-10-16 1988-10-14 Process and plant for clarifying liquids, in particular raw juice WO1989003240A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH4070/87A CH673957A5 (en) 1987-10-16 1987-10-16
CH4070/87-7 1987-10-16

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0388628A2 (en) * 1989-03-18 1990-09-26 OTTO TUCHENHAGEN GmbH & Co. KG Process for the separation of particles from fermentable or fermented suspensions of beverage production
WO1990014018A1 (en) * 1989-05-18 1990-11-29 Bucher-Guyer Ag Maschinenfabrik Process and device for clarifying liquids, in particular raw juice
WO1991005847A1 (en) * 1989-10-20 1991-05-02 Bucher-Guyer Ag Maschinenfabrik Process for clarifying raw juice and installation for implementing it
EP0464506A1 (en) * 1990-07-04 1992-01-08 BUCHER-GUYER AG Maschinenfabrik Process and apparatus to clarify liquids
WO1993014650A1 (en) * 1992-01-29 1993-08-05 Bucher-Guyer Ag Maschinenfabrik Method of manufacturing a non-alcoholic drink with a reduced sugar content
EP0562100A1 (en) * 1991-10-15 1993-09-29 Nutrasweet Co Sugar separation from juices.
WO1995033045A1 (en) * 1994-05-30 1995-12-07 BÄCHLI, Emil Process for preparing a turbid liquid containing volatile substances or fragrances
GB2306898A (en) * 1995-11-09 1997-05-14 Weizmann Kiryat Membrane Prod Membrane recovery of chromatography solvent and solute
US6113791A (en) * 1990-07-06 2000-09-05 Bucher-Guyer Ag Process for flushing the filtration modules of a unit for clarifying liquids
FR2800386A1 (en) * 1999-10-27 2001-05-04 Brunet Clarifying raisin must, for use in wine making, involves tangential filtration
IT201800007405A1 (en) * 2018-07-20 2020-01-20 FERMENTATION METHOD AND PLANT

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CA2389284C (en) * 1999-10-27 2008-03-25 Rwe Nukem Corporation Waste water treatment system
DE10255064A1 (en) * 2002-11-25 2004-06-17 Rwe Nukem Gmbh Process for treating radioactive waste water

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2046055A1 (en) * 1969-04-04 1971-04-22 Hydronautics Israel Ltd Rehovot (Israel) Method and device for concentrating solutions
DE3517886A1 (en) * 1984-08-17 1986-02-20 Bucher-Guyer Ag Maschinenfabrik, Niederweningen METHOD FOR OBTAINING LIQUID FROM A REMAINING SUBSTANCE AND DEVICE FOR IMPLEMENTING THE SAME

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2046055A1 (en) * 1969-04-04 1971-04-22 Hydronautics Israel Ltd Rehovot (Israel) Method and device for concentrating solutions
DE3517886A1 (en) * 1984-08-17 1986-02-20 Bucher-Guyer Ag Maschinenfabrik, Niederweningen METHOD FOR OBTAINING LIQUID FROM A REMAINING SUBSTANCE AND DEVICE FOR IMPLEMENTING THE SAME

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0388628A2 (en) * 1989-03-18 1990-09-26 OTTO TUCHENHAGEN GmbH & Co. KG Process for the separation of particles from fermentable or fermented suspensions of beverage production
EP0388628A3 (en) * 1989-03-18 1991-11-27 OTTO TUCHENHAGEN GmbH & Co. KG Process for the separation of particles from fermentable or fermented suspensions of beverage production
WO1990014018A1 (en) * 1989-05-18 1990-11-29 Bucher-Guyer Ag Maschinenfabrik Process and device for clarifying liquids, in particular raw juice
WO1991005847A1 (en) * 1989-10-20 1991-05-02 Bucher-Guyer Ag Maschinenfabrik Process for clarifying raw juice and installation for implementing it
EP0464506A1 (en) * 1990-07-04 1992-01-08 BUCHER-GUYER AG Maschinenfabrik Process and apparatus to clarify liquids
CH680976A5 (en) * 1990-07-04 1992-12-31 Bucher Guyer Ag Masch
US6113791A (en) * 1990-07-06 2000-09-05 Bucher-Guyer Ag Process for flushing the filtration modules of a unit for clarifying liquids
EP0562100A1 (en) * 1991-10-15 1993-09-29 Nutrasweet Co Sugar separation from juices.
EP0562100A4 (en) * 1991-10-15 1994-02-09 The Nutrasweet Company
WO1993014650A1 (en) * 1992-01-29 1993-08-05 Bucher-Guyer Ag Maschinenfabrik Method of manufacturing a non-alcoholic drink with a reduced sugar content
WO1995033045A1 (en) * 1994-05-30 1995-12-07 BÄCHLI, Emil Process for preparing a turbid liquid containing volatile substances or fragrances
GB2306898A (en) * 1995-11-09 1997-05-14 Weizmann Kiryat Membrane Prod Membrane recovery of chromatography solvent and solute
GB2306898B (en) * 1995-11-09 1999-06-16 Weizmann Kiryat Membrane Prod A multi-stage membrane system and process
FR2800386A1 (en) * 1999-10-27 2001-05-04 Brunet Clarifying raisin must, for use in wine making, involves tangential filtration
IT201800007405A1 (en) * 2018-07-20 2020-01-20 FERMENTATION METHOD AND PLANT
WO2020016695A1 (en) * 2018-07-20 2020-01-23 Della Toffola Spa Method and apparatus for fermentation

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CH673957A5 (en) 1990-04-30

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