WO2000012199A1 - Method and device for separating a mixture into solid and liquid parts by cross-flow filtration - Google Patents
Method and device for separating a mixture into solid and liquid parts by cross-flow filtration Download PDFInfo
- Publication number
- WO2000012199A1 WO2000012199A1 PCT/CH1999/000381 CH9900381W WO0012199A1 WO 2000012199 A1 WO2000012199 A1 WO 2000012199A1 CH 9900381 W CH9900381 W CH 9900381W WO 0012199 A1 WO0012199 A1 WO 0012199A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- mixture
- separated
- flow
- retentate
- filtration
- Prior art date
Links
- 239000000203 mixture Substances 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 title claims abstract description 22
- 238000009295 crossflow filtration Methods 0.000 title claims description 10
- 239000007787 solid Substances 0.000 title claims description 9
- 238000001914 filtration Methods 0.000 claims abstract description 64
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims abstract description 21
- 239000012466 permeate Substances 0.000 claims abstract description 15
- 235000013399 edible fruits Nutrition 0.000 claims abstract description 11
- 210000004102 animal cell Anatomy 0.000 claims abstract description 7
- 230000029087 digestion Effects 0.000 claims abstract description 5
- 239000012465 retentate Substances 0.000 claims description 37
- 239000012528 membrane Substances 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 14
- 238000011026 diafiltration Methods 0.000 claims description 6
- 230000000903 blocking effect Effects 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 230000001276 controlling effect Effects 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 230000003134 recirculating effect Effects 0.000 claims description 3
- 102000005575 Cellulases Human genes 0.000 claims description 2
- 108010084185 Cellulases Proteins 0.000 claims description 2
- 230000002255 enzymatic effect Effects 0.000 claims description 2
- 239000011368 organic material Substances 0.000 claims description 2
- 238000004804 winding Methods 0.000 claims description 2
- 102000004190 Enzymes Human genes 0.000 claims 1
- 108090000790 Enzymes Proteins 0.000 claims 1
- 125000003118 aryl group Chemical group 0.000 claims 1
- 238000010790 dilution Methods 0.000 claims 1
- 239000012895 dilution Substances 0.000 claims 1
- 238000009434 installation Methods 0.000 abstract 1
- 235000013311 vegetables Nutrition 0.000 abstract 1
- 239000000047 product Substances 0.000 description 23
- 238000010586 diagram Methods 0.000 description 6
- 238000000108 ultra-filtration Methods 0.000 description 5
- 235000015203 fruit juice Nutrition 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000001953 sensory effect Effects 0.000 description 2
- 230000008719 thickening Effects 0.000 description 2
- RUPQKSPPLBBBED-QMMMGPOBSA-N CCN(C)CCC[C@H](C)N Chemical compound CCN(C)CCC[C@H](C)N RUPQKSPPLBBBED-QMMMGPOBSA-N 0.000 description 1
- ZZZCUOFIHGPKAK-UHFFFAOYSA-N D-erythro-ascorbic acid Natural products OCC1OC(=O)C(O)=C1O ZZZCUOFIHGPKAK-UHFFFAOYSA-N 0.000 description 1
- 108010059820 Polygalacturonase Proteins 0.000 description 1
- 229930003268 Vitamin C Natural products 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 108010093305 exopolygalacturonase Proteins 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 235000019154 vitamin C Nutrition 0.000 description 1
- 239000011718 vitamin C Substances 0.000 description 1
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
-
- 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
-
- 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
- A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation containing fruit or vegetable juices
- A23L2/04—Extraction of juices
-
- 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
- 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
-
- 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
- B01D61/147—Microfiltration
-
- 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
- B01D61/16—Feed pretreatment
-
- 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
- B01D61/20—Accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/16—Flow or flux control
Definitions
- the invention relates to a method for separating a pumpable mixture of plant or animal cell groups into solid and liquid components by crossflow filtration, and an apparatus for carrying out the method.
- a method of making fruit juices is known from U.S. Patent 4,716,044 (Thomas et al.).
- the fruit is used to create a pumpable liquid puree consisting of fruit and juice.
- This puree is pumped under a pressure between 7 bar and 70 bar in a single pass through a rigid porous tubular housing with a diameter between 1.6 cm and 15 cm.
- a food-grade ultrafiltration membrane with a certain initial permeability is attached to the inside of the housing.
- the outlet pressure at the housing is kept between 3 bar and 7 bar.
- the invention has for its object to avoid the disadvantages of the known method by a new separation method and to provide a device for carrying it out.
- this object is achieved in a method of the type mentioned at the outset by preparing a mash from plant or animal cell groups, in particular from whole fruits, by comminution and digestion, that a filtration system with at least one flow path (pass) for the Flow of the mixture to be separated and an outlet for separated liquid components (permeate) is provided and that at least a part of the prepared mash as a pumpable mixture to be separated is circulated several times through the flow paths
- the method is preferably carried out in such a way that the flow and / or pressure of the mixture to be separated is detected at the outlet of each flow path (passport) and regulated in such a way that the pressure by means of a variable throttle at the outlet and the flow through at least one circulation pump in the circuit to set values are controlled, and that if these setpoints are not reached, the outflow of the separated liquid fractions (permeate) is alternatively reduced or interrupted.
- a device according to the invention for separating a pumpable mixture of plant or animal cell groups, in particular a mash prepared from whole fruits by comminution and digestion into solid and liquid fractions by crossflow filtration comprises at least two filtration modules which are connected in series in a retentate circuit for the mixture to be separated , wherein the filtration modules comprise individual tubular membranes with an inner diameter of more than 10 mm.
- FIG. 1 shows a diagram of a direct filtration system for carrying out the separation process of a mixture according to the invention
- FIG. 2 shows a variant of the direct filtration system according to FIG. 1, 3 is a diagram of control loops for a direct filtration system ge ass Fig. 1,
- FIG. 4 shows a diagram of a partial removal of retentate from the product cycle of a system according to FIG. 1,
- FIG. 5 shows a diagram of a partial or total removal of retentate from the product cycle of a system according to FIG. 1,
- FIG. 6 shows a diagram of a direct filtration system for carrying out the separation process according to the invention of a mixture in a compact design for minimizing residual product quantities in the event of a product displacement and
- FIG. 7 shows a variant of the direct filtration system according to FIG. 1.
- the direct filtration system shown schematically in FIG. 1 is particularly suitable for separating a fruit mash into a raw juice and a residue (pomace).
- a mill which is not shown and is known per se, is used for comminuting and disintegrating whole fruits, with a pumpable mash being prepared.
- This mash passes through a line 1 with a shut-off valve 2 into a batch tank 3, which is provided with a stirring device 4 in a manner known per se.
- a product circuit with a cross-flow filtration system is connected to the batch tank 3, the structure of which is described below.
- a circulation pump 5 for the contents of the batch anchor 3, which is to be separated as a pumpable mixture.
- the circulation pump 5 conveys this mixture via a connecting line ⁇ , a mixer 7 and a symmetrical distributor 8 into four parallel flow paths (passe), which each have two cross-flow filtration modules 9, 9 ', 10, 10 ', 11, 11', 12, 12 'in series.
- a control valve 13, 14, 15, 16 for controlling the pressure and flow of the mixture is provided at the outputs of the four yokes.
- Each control valve 13, 14, 15, 16 is supplied with the output signal of a sensor 13 ', 14', 15 ', 16' connected upstream for flow and / or pressure of the mixture.
- the outputs of the control valves 13, 14, 15, 16 are connected to a via a second symmetrical distributor 17
- the return line 18 leads a part (retentate) of the mixture after separation of a liquid portion in the filtration modules 9, 9 ', 10, 10', 11, 11 ', 12, 12' via a reverse pump 19 for setting the mixture pressure and a shut-off valve 20 back into batch tank 3.
- a line 22 for removing retentate from the circuit is also arranged via a shut-off valve 21.
- a flow sensor 23 is provided between the circulation pump 5 and the mixer 7, a pressure sensor 24 between the mixer 7 and the distributor 8 and a further pressure sensor 25 at the output of the second symmetrical distributor 17.
- the output signals of the sensors 23, 24 and 25 are supplied to the circulation pump 5 and the reverse pump 19 for controlling the flow and pressure of the mixture in the product circuit.
- a vessel 26 with a shut-off valve 27 is provided between the mixer 7 and the distributor 8 to compensate for pressure surges from the circulation pump 5.
- a line 28 with a shut-off valve 29 for supplying water to the batch tank 3 is also provided if the residue of the mash (retentate) is to be displaced from the filtration system or diafiltered after the juice separation has ended.
- the separated juice is removed from the filtration modules 9, 9 ', 10, 10', 11, 11 ', 12, 12' as a permeate by means of lines 30.
- a gas or a gaseous substance can be added to the mixture at a suitable point in the circuit. If the viscosity and thus the pressure drop in the residue (retentate) reaches a maximum permissible value or the yield of juice reaches a predetermined value, then diafiltration with the addition of a washing-out agent into the mixture to be separated may prove advantageous to further increase the yield. This diafiltration is terminated if the soluble fractions in the juice fall below a predetermined value or if a desired overall yield is reached.
- the viscosity of the mash can also be measured Reduce enzymatic treatment with pectinases or cellulases. An additional reduction in the viscosity of the mash is also achieved by heating to more than 30 ° C or 60 ° C.
- the sensory quality of the juice can be improved by using the solid / liquid
- Fig. 2 shows schematically a variant of the
- Direct filtration system of the type described in relation to FIG. 1, reference numerals from FIG. 1 denoting corresponding components in FIG. 2.
- a separate backward-running pump 19 ', 19' ', 19' '', 19 '' '' is provided for setting the mixture pressure for each of the four flow paths .
- Two sensors are arranged in front of each of these pumps, namely four flow sensors 33, 34, 35, 36 and four pressure sensors 33 ', 34', 35 ', 36'.
- the output signals of the sensors 24, 33-36 and 33 '-36' control the reverse pumps 19 '-19' '''and the circulation pump 5, by which Output signals of the sensor 23, on the other hand, only the circulation pump 5.
- the pressure and flow controls for the individual flow paths also serve to avoid blockages of the product during the filtration and subsequent flushing of the filtration modules 9-12, 9 with that according to FIG. 2 '- 12'.
- the filtration modules 9-12, 9 '-12' can be connected in series for a final discharge of the largely juiced residue (retentates). This measure prevents blockage of individual filtration modules lying in parallel, but it is only useful if the required discharge pressure does not exceed the permissible operating pressure of the filtration modules.
- Fig. 1 and Fig. 2 are the control loops for controlling the pressure and flow of the pumpable to be separated
- FIG. 3 now shows a diagram of control loops for a direct filtration system according to FIG. 1 in detail. Only one filtration module 9 ′′ is provided, which has an inlet 38 for the mixture, as well as an outlet 37 for the residue and an outlet 42 for the separated permeate. To detect pressure and flow, a pressure sensor 24 and a flow sensor 23 are arranged at the inlet 38, a pressure sensor 25 and a flow sensor 13 ′′ at the outlet 37 and a pressure sensor 30 ′ at the outlet 42 for the permeate. 3, the output signals are all fed to a regulator and control unit 40.
- a control valve 41 is switched on in the return line 18 at the outlet 37 for the residue and a control valve 43 in the line 30 for discharging the permeate from the outlet 42.
- the control valves 41, 43 are operated by the regulator and control unit 40 ago set via control lines. These settings are made so that the setpoints of pressure and flow are reached. If this is not possible due to blocking in the filtration module 9 ′′, the control valve 43 is first closed. As a further measure, pressurized water is then applied to the filtration membranes on the permeate side via an adjusting valve 44 arranged at the outlet 42 for the separated permeate, and thus backwashing is initiated in a manner known per se.
- Direct filtration system for a separation process in which a product batch introduced into the batch tank 3 is juiced by recirculation, the shut-off valve 21 remaining closed and being opened only for expelling the largely juiced residue (retentate). According to the amount of juice separated from the cycle, the
- FIG. 1 shows FIG. 4.
- a circuit for the recirculation of the mixture to be separated which comprises a filtration module 9 ′′, as well as a recirculation pump 5 at its input and one at its output, is shown schematically here backward-running pressure maintenance pump 19.
- the batch tank 3 according to FIG. 1 is omitted when it is returned directly to the pump 5 according to FIG. 4.
- the product circuit is closed by a return line 18 'from the outlet of the pressure-maintaining pump 19 to the inlet of the recirculation pump 5.
- a discharge pump 21 ′ which also runs backwards, is arranged at the outlet of the pressure-maintaining pump 19.
- the retentate is discharged via a line 22, and fresh product is continuously fed accordingly via a line 1 '. Further details of the direct filtration system measured Fig. 1 are not shown in the schematic representation of Fig. 4.
- FIG. 5 shows a variant of the circuit according to FIG. 4, in which the discharge pump 21 'is connected between the pressure-maintaining pump 19 and the outlet of the filtration module 9' '.
- FIG. 6 shows a schematic of a variant of a direct filtration system according to FIG. 1 for carrying out the separation process according to the invention of a mixture in a compact design for minimizing residual product quantities in the event of product displacement.
- the reverse-running pressure-maintaining pump 19 is directly connected to the batch tank 3 on the output side and is arranged spatially directly thereon.
- the length of the connecting lines between the feed pump 5 and the filtration module 9 ′′ and between the filtration module 9 ′′ and the pressure-maintaining pump 19 is kept as small as possible.
- the circulating pump 5 according to FIG. 1 is replaced by a circulating pump 5 'for the four individual flow paths (yoke).
- each pass comprises three filtration modules 9 '''in series.
- the product from the batch tank 3 reaches the four circulation pumps 5 'via a simple distribution line 50 and shut-off valves 51.
- the residues from the four flow paths (pass) return to the batch tank 3 via a simple manifold 52 and shut-off valves 53, a return line 18, a pressure maintenance pump 19 and a shut-off valve 20.
- a flow sensor 23 is arranged between the circulation pumps 5 'and the first filtration modules 9''' of the four passages, as is a flow sensor 23 'at the outputs of the last four filtration modules 9'''. As shown in FIG. 7, the output signals of the flow sensors 23 act on the pressure-maintaining pump 19 and the output signals of the flow sensors 23 'act on the four circulation pumps 5' for regulating the flows through the four passages on them
- the permeates separated in the filtration modules 9 ′′ ′′ pass via manifolds 30 ′′ and throttles 54 into an outlet line 55 for the separated fruit juice.
- filtration modules When using a filtration system with several separation stages in series, inexpensive low-pressure filtration modules can be used in the first stage if the transmembrane pressure is limited to a maximum of 8 bar or 10 bar.
- Such filtration modules include tubular membranes made of organic material, the support tubes of which are produced by winding a band. If several filtration modules with tube membranes are used in series, the inside diameter and tube length of the tube membranes in each filtration module are adapted to a different product viscosity, and such filtration modules can be shut down in the circuit by bridging, the dimensions of which are poorly adapted to the product viscosity just present.
- Suitable filtration modules are commercially available devices from the Supercore brand from Koch or the brand Super-Cor or A 19 from PCI. Eccentric screw pumps are suitable as feed pumps for products with higher viscosity.
- Macrofiltration can also be used to produce cloudy juices, as are known from conventional presses.
- vitamin C is added to reduce the oxidation.
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL99340343A PL340343A1 (en) | 1998-08-28 | 1999-08-18 | Method of breaking a mixture into solid and liquid fractions by means of transverse filtration |
CA002307673A CA2307673A1 (en) | 1998-08-28 | 1999-08-18 | Method and device for separating a mixture into solid and liquid parts by cross-flow filtration |
AU51460/99A AU5146099A (en) | 1998-08-28 | 1999-08-18 | Method and device for separating a mixture into solid and liquid parts by cross-flow filtration |
JP2000567294A JP2002523075A (en) | 1998-08-28 | 1999-08-18 | Method for separating a mixture into solid and liquid components by cross-flow filtration |
EP99936229A EP1027138A1 (en) | 1998-08-28 | 1999-08-18 | Method and device for separating a mixture into solid and liquid parts by cross-flow filtration |
HU0100341A HUP0100341A3 (en) | 1998-08-28 | 1999-08-18 | Method for separating a mixture of solid and liquid parts by cross-flow filtration |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CH176798 | 1998-08-28 | ||
CH1767/98 | 1998-08-28 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000012199A1 true WO2000012199A1 (en) | 2000-03-09 |
Family
ID=4218112
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CH1999/000381 WO2000012199A1 (en) | 1998-08-28 | 1999-08-18 | Method and device for separating a mixture into solid and liquid parts by cross-flow filtration |
Country Status (10)
Country | Link |
---|---|
EP (1) | EP1027138A1 (en) |
JP (1) | JP2002523075A (en) |
CN (1) | CN1277564A (en) |
AR (1) | AR020272A1 (en) |
AU (1) | AU5146099A (en) |
CA (1) | CA2307673A1 (en) |
HU (1) | HUP0100341A3 (en) |
PL (1) | PL340343A1 (en) |
WO (1) | WO2000012199A1 (en) |
ZA (1) | ZA200002102B (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9161560B2 (en) | 2002-08-19 | 2015-10-20 | Lycored Natural Products Industries, Ltd. | Industrial tomoato process and product obtained thereof |
WO2019048471A1 (en) * | 2017-09-08 | 2019-03-14 | Krones Ag | Device and method for mashing and filtration for beer production |
US10830740B2 (en) | 2010-03-31 | 2020-11-10 | Cytiva Bioprocess R&D Ab | Parallel separation system |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10204414A1 (en) * | 2002-02-04 | 2003-09-04 | Siemens Ag | Microfluidic system |
ATE401009T1 (en) * | 2003-10-01 | 2008-08-15 | Campbell Soup Co | METHOD FOR THE ENZYMATIC TREATMENT AND FILTRATION OF A PLANT AND PRODUCTS OBTAINED THEREFROM |
WO2005094614A1 (en) * | 2004-04-01 | 2005-10-13 | Japan Science And Technology Agency | Method of squeezing juice from fruit and apparatus for squeezing juice from fruit |
JP4840973B2 (en) * | 2006-03-23 | 2011-12-21 | カゴメ株式会社 | Reverse osmosis concentrator |
CA2793723A1 (en) * | 2010-03-31 | 2011-10-06 | Ge Healthcare Bio-Sciences Ab | A parallel separation system |
JP2011115797A (en) * | 2011-03-22 | 2011-06-16 | Kagome Co Ltd | Reverse osmosis concentration apparatus |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4716044A (en) * | 1986-01-31 | 1987-12-29 | Clemson University | Process for obtaining juices from fruits containing same |
WO1988006005A1 (en) * | 1987-02-14 | 1988-08-25 | Bucher-Guyer Ag | Process for treating fruit and vegetables, in particular for juice extraction, and installation for carrying out the process |
US5112489A (en) * | 1990-07-04 | 1992-05-12 | Bucher-Guyer Ag Maschinenfabrik | Process and unit for clarification of liquids |
WO1996012553A1 (en) * | 1994-10-25 | 1996-05-02 | Bucher-Guyer Ag Maschinenfabrik | Process and device for concentrating solid/liquid mixtures by means of diaphragm technology |
WO1998024331A1 (en) * | 1996-12-02 | 1998-06-11 | Barth Fruit Ag | Method of processing, in particular concentrating, fruit and/or vegetable juice and arrangement for carrying out this method |
-
1999
- 1999-08-18 AU AU51460/99A patent/AU5146099A/en not_active Abandoned
- 1999-08-18 HU HU0100341A patent/HUP0100341A3/en unknown
- 1999-08-18 CA CA002307673A patent/CA2307673A1/en not_active Abandoned
- 1999-08-18 CN CN99801506A patent/CN1277564A/en active Pending
- 1999-08-18 EP EP99936229A patent/EP1027138A1/en not_active Withdrawn
- 1999-08-18 WO PCT/CH1999/000381 patent/WO2000012199A1/en not_active Application Discontinuation
- 1999-08-18 JP JP2000567294A patent/JP2002523075A/en not_active Withdrawn
- 1999-08-18 PL PL99340343A patent/PL340343A1/en unknown
- 1999-08-26 AR ARP990104271A patent/AR020272A1/en unknown
-
2000
- 2000-04-28 ZA ZA200002102A patent/ZA200002102B/en unknown
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4716044A (en) * | 1986-01-31 | 1987-12-29 | Clemson University | Process for obtaining juices from fruits containing same |
WO1988006005A1 (en) * | 1987-02-14 | 1988-08-25 | Bucher-Guyer Ag | Process for treating fruit and vegetables, in particular for juice extraction, and installation for carrying out the process |
US5112489A (en) * | 1990-07-04 | 1992-05-12 | Bucher-Guyer Ag Maschinenfabrik | Process and unit for clarification of liquids |
WO1996012553A1 (en) * | 1994-10-25 | 1996-05-02 | Bucher-Guyer Ag Maschinenfabrik | Process and device for concentrating solid/liquid mixtures by means of diaphragm technology |
WO1998024331A1 (en) * | 1996-12-02 | 1998-06-11 | Barth Fruit Ag | Method of processing, in particular concentrating, fruit and/or vegetable juice and arrangement for carrying out this method |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9161560B2 (en) | 2002-08-19 | 2015-10-20 | Lycored Natural Products Industries, Ltd. | Industrial tomoato process and product obtained thereof |
US10830740B2 (en) | 2010-03-31 | 2020-11-10 | Cytiva Bioprocess R&D Ab | Parallel separation system |
WO2019048471A1 (en) * | 2017-09-08 | 2019-03-14 | Krones Ag | Device and method for mashing and filtration for beer production |
DE102017215930A1 (en) * | 2017-09-08 | 2019-03-14 | Krones Aktiengesellschaft | Apparatus and method for mashing and filtering for beer production |
Also Published As
Publication number | Publication date |
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CA2307673A1 (en) | 2000-03-09 |
ZA200002102B (en) | 2000-11-15 |
HUP0100341A2 (en) | 2001-06-28 |
JP2002523075A (en) | 2002-07-30 |
EP1027138A1 (en) | 2000-08-16 |
AR020272A1 (en) | 2002-05-02 |
HUP0100341A3 (en) | 2002-01-28 |
PL340343A1 (en) | 2001-01-29 |
CN1277564A (en) | 2000-12-20 |
AU5146099A (en) | 2000-03-21 |
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