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WO1989003240A1 - Procede de decantation des liquides, en particulier les jus bruts, et installation pour la mise en oeuvre du procede - Google Patents

Procede de decantation des liquides, en particulier les jus bruts, et installation pour la mise en oeuvre du procede 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
Authority
WO
WIPO (PCT)
Prior art keywords
cross
flow filtration
filtration device
retentate
plant according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CH1988/000191
Other languages
German (de)
English (en)
Inventor
Walter Gresch
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bucher Guyer AG
Original Assignee
Bucher Guyer AG
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 Bucher Guyer AG filed Critical Bucher Guyer AG
Publication of WO1989003240A1 publication Critical patent/WO1989003240A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Preparation or treatment thereof
    • 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
    • B01D61/149—Multistep processes comprising different kinds of membrane processes selected from ultrafiltration or microfiltration
    • 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.

Landscapes

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

Abstract

Dans le procédé de décantation des jus bruts, objet de l'invention, le rétentat d'une première installation de filtrage à flux transversal (2) est introduit dans le côté rétentat d'une deuxième installation de filtrage à flux transversal (6), dont la surface de la membrane (7) présente des pores de plus grandes dimensions que la surface de la membrane (3) de la première installation de filtrage à flux transversal (2). Le perméat de la deuxième installation de filtrage à flux transversal (6) est alors renvoyé vers le côté rétentat de la première installation de filtrage à flux transversal (2). Il se crée ainsi un circuit (2, 5, 6, 8) dans lequel le dépôt est réduit dans des proportions considérables en raison d'une évacuation continue du rétentat résiduel par la conduite (9). Il en résulte une amélioration du pouvoir de filtrage et du rendement pour un investissement relativement modeste.
PCT/CH1988/000191 1987-10-16 1988-10-14 Procede de decantation des liquides, en particulier les jus bruts, et installation pour la mise en oeuvre du procede Ceased WO1989003240A1 (fr)

Applications Claiming Priority (2)

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

Publications (1)

Publication Number Publication Date
WO1989003240A1 true WO1989003240A1 (fr) 1989-04-20

Family

ID=4269258

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CH1988/000191 Ceased WO1989003240A1 (fr) 1987-10-16 1988-10-14 Procede de decantation des liquides, en particulier les jus bruts, et installation pour la mise en oeuvre du procede

Country Status (3)

Country Link
EP (1) EP0338043A1 (fr)
CH (1) CH673957A5 (fr)
WO (1) WO1989003240A1 (fr)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1990014018A1 (fr) * 1989-05-18 1990-11-29 Bucher-Guyer Ag Maschinenfabrik Procede et dispositif pour purifier des liquides, en particulier du jus brut
WO1991005847A1 (fr) * 1989-10-20 1991-05-02 Bucher-Guyer Ag Maschinenfabrik Dispositif pour la clarification de jus brut ainsi qu'installation pour la realisation de ce procede
EP0388628A3 (fr) * 1989-03-18 1991-11-27 OTTO TUCHENHAGEN GmbH & Co. KG Procédé pour la séparation de particules de suspensions fermentescibles ou fermentées de la préparation de boissons
EP0464506A1 (fr) * 1990-07-04 1992-01-08 BUCHER-GUYER AG Maschinenfabrik Procédé et appareil pour clarifier des liquides
WO1993014650A1 (fr) * 1992-01-29 1993-08-05 Bucher-Guyer Ag Maschinenfabrik Procede de preparation d'une boisson sans alcool a teneur en sucre reduite
EP0562100A4 (fr) * 1991-10-15 1994-02-09 The Nutrasweet Company
WO1995033045A1 (fr) * 1994-05-30 1995-12-07 BÄCHLI, Emil Procede de preparation d'un liquide trouble contenant des substances volatiles ou parfumees
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 (fr) * 1999-10-27 2001-05-04 Brunet Procede de filtration tangentielle du mout de raisin et dispositif pour la mise en oeuvre dudit procede
IT201800007405A1 (it) * 2018-07-20 2020-01-20 Metodo ed impianto di fermentazione

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2389284C (fr) * 1999-10-27 2008-03-25 Rwe Nukem Corporation Systeme de traitement d'eaux usees
DE10255064A1 (de) * 2002-11-25 2004-06-17 Rwe Nukem Gmbh Verfahren zum Behandeln von radioaktivem Abwasser

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2046055A1 (de) * 1969-04-04 1971-04-22 Hydronautics Israel Ltd Rehovot (Israel) Verfahren und Vorrichtung zum Einengen von Losungen
DE3517886A1 (de) * 1984-08-17 1986-02-20 Bucher-Guyer Ag Maschinenfabrik, Niederweningen Verfahren zur gewinnung von fluessigkeit aus einer restsubstanz und vorrichtung zur durchfuehrung derselben

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2046055A1 (de) * 1969-04-04 1971-04-22 Hydronautics Israel Ltd Rehovot (Israel) Verfahren und Vorrichtung zum Einengen von Losungen
DE3517886A1 (de) * 1984-08-17 1986-02-20 Bucher-Guyer Ag Maschinenfabrik, Niederweningen Verfahren zur gewinnung von fluessigkeit aus einer restsubstanz und vorrichtung zur durchfuehrung derselben

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0388628A3 (fr) * 1989-03-18 1991-11-27 OTTO TUCHENHAGEN GmbH & Co. KG Procédé pour la séparation de particules de suspensions fermentescibles ou fermentées de la préparation de boissons
WO1990014018A1 (fr) * 1989-05-18 1990-11-29 Bucher-Guyer Ag Maschinenfabrik Procede et dispositif pour purifier des liquides, en particulier du jus brut
WO1991005847A1 (fr) * 1989-10-20 1991-05-02 Bucher-Guyer Ag Maschinenfabrik Dispositif pour la clarification de jus brut ainsi qu'installation pour la realisation de ce procede
EP0464506A1 (fr) * 1990-07-04 1992-01-08 BUCHER-GUYER AG Maschinenfabrik Procédé et appareil pour clarifier des liquides
CH680976A5 (fr) * 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
EP0562100A4 (fr) * 1991-10-15 1994-02-09 The Nutrasweet Company
WO1993014650A1 (fr) * 1992-01-29 1993-08-05 Bucher-Guyer Ag Maschinenfabrik Procede de preparation d'une boisson sans alcool a teneur en sucre reduite
WO1995033045A1 (fr) * 1994-05-30 1995-12-07 BÄCHLI, Emil Procede de preparation d'un liquide trouble contenant des substances volatiles ou parfumees
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 (fr) * 1999-10-27 2001-05-04 Brunet Procede de filtration tangentielle du mout de raisin et dispositif pour la mise en oeuvre dudit procede
IT201800007405A1 (it) * 2018-07-20 2020-01-20 Metodo ed impianto di fermentazione
WO2020016695A1 (fr) * 2018-07-20 2020-01-23 Della Toffola Spa Procédé et appareil de fermentation

Also Published As

Publication number Publication date
EP0338043A1 (fr) 1989-10-25
CH673957A5 (fr) 1990-04-30

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