CA2132682C - Method for the removal of components causing turbidity, from a fluid, by means of microfiltration - Google Patents
Method for the removal of components causing turbidity, from a fluid, by means of microfiltration Download PDFInfo
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- CA2132682C CA2132682C CA002132682A CA2132682A CA2132682C CA 2132682 C CA2132682 C CA 2132682C CA 002132682 A CA002132682 A CA 002132682A CA 2132682 A CA2132682 A CA 2132682A CA 2132682 C CA2132682 C CA 2132682C
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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
- B01D61/147—Microfiltration
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
- A23C9/00—Milk preparations; Milk powder or milk powder preparations
- A23C9/14—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment
- A23C9/142—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration
- A23C9/1422—Milk preparations; Milk powder or milk powder preparations in which the chemical composition of the milk is modified by non-chemical treatment by dialysis, reverse osmosis or ultrafiltration by ultrafiltration, microfiltration or diafiltration of milk, e.g. for separating protein and lactose; Treatment of the UF permeate
-
- 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
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- 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
- C12H1/00—Pasteurisation, sterilisation, preservation, purification, clarification, or ageing of alcoholic beverages
- C12H1/02—Pasteurisation, sterilisation, preservation, purification, clarification, or ageing of alcoholic beverages combined with removal of precipitate or added materials, e.g. adsorption material
- C12H1/06—Precipitation by physical means, e.g. by irradiation, vibrations
- C12H1/063—Separation by filtration
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/04—Filters; Permeable or porous membranes or plates, e.g. dialysis
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M39/00—Means for cleaning the apparatus or avoiding unwanted deposits of microorganisms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/04—Backflushing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/20—By influencing the flow
- B01D2321/2066—Pulsated flow
Abstract
The invention relates to a process for the removal of components causing turbidity, from a fluid, by means of micro-filtration, whereby the fluid is beer, wine, fruit juice, bacterial suspension, blood, milk, enzyme suspension, etc.
According to the invention the fluid to be treated is fed across an asymmetric membrane having a pore structure such that the pores on the feed side of the membrane are larger than the nominal pore size and the pores of nominal pore size occur in the cross section toward the permeate side, the filtered off components are back-flushed from the membrane and are subsequently carried away with the fluid. The nominal pore size is usually 0.1-5.0 µm and preferably 0.2-1.0 µm. The membrane may be tubular, flat or capillary. Back-flushing takes place intermittently with a frequency of 1 second to 10 minutes for 0.1-1 second at a counter pressure of 0.5-5 bar.
The feed velocity is preferably below 2 m/s and the pressure difference over the membrane is less than 0.5 bar.
According to the invention the fluid to be treated is fed across an asymmetric membrane having a pore structure such that the pores on the feed side of the membrane are larger than the nominal pore size and the pores of nominal pore size occur in the cross section toward the permeate side, the filtered off components are back-flushed from the membrane and are subsequently carried away with the fluid. The nominal pore size is usually 0.1-5.0 µm and preferably 0.2-1.0 µm. The membrane may be tubular, flat or capillary. Back-flushing takes place intermittently with a frequency of 1 second to 10 minutes for 0.1-1 second at a counter pressure of 0.5-5 bar.
The feed velocity is preferably below 2 m/s and the pressure difference over the membrane is less than 0.5 bar.
Description
Method for the removal of components causing turbidity, from a fluid, by means of microfiltration The present invention relates to a method for the removal of components that cause turbidity, from a fluid, by means of microfiltration.
The application of microfiltration whereby by maintaining a flow along the membrane wall, it is attempted to prevent accumulation of dirt, is a known technique. This tech-nique is generally called crossflow microfiltration.
In practice this technique is applied in, for in-stance, ultrafiltration and microfiltration.
Effective velocities to prevent the build-up of a fouling layer often begin at 2 m/s while as a rule velocities from 4-6 m/s are used.
Dependent on the membrane configuration this is the range where turbulence in the flow occurs.
It should be noted that the technique of back-flush-ing membranes was introduced by Klein and Schneider for self-supporting capillary membranes (Desalination 41 (1982 263-275) whereby microfiltration membranes were applied with a pore size of above 0.01 Vim. For further prior art reference is made to "Microfiltration mit Membranes" by S. Ripperger (ISBN 3-527-28457-5, 1992).
In the above-mentioned known techniques the back-flush is performed once every few minutes, giving a loss of production because part of the permeate is pushed back to the concentrate side of the membrane. A special technique is used by Memtec, who back-flush the membrane with gas (AU-B-34.400/-84). The fastest back-flush intervals are recorded in DK-A-476/90 (APV Pasilac).
Here back-flush frequencies are recorded of 1-10 back-flushes per minute at a back-flush duration of 1-5 seconds. One thing and another results in the fact, that due to these relative long back-flushing times the installation is not in use for filtration for 10-20% of the time.
A disadvantage of the known membrane is that it suf-fers a productivity drop due to the formation of a so-called secondary membrane, consisting of a packing of particles to be filtered off, which partly plug the pores and as layer shows only a limited "own" permeability.
The object of the invention is to provide a method with practically no productivity drop because the thickness of the layer of particles to be filtered off is limited and the secondary membrane is disturbed.
To this end, the present invention provides a process for the removal of components causing turbidity, from a fluid, by means of cross-flow microfiltration, characterized in that the fluid is fed across an asymmetric membrane having a pore structure such that the pores on the feed side of the membrane are larger than the nominal pore size and the pores of nominal pore size occur in the cross section toward the permeate side, the filtered off components are back-flushed from the membrane and are subsequently carried away with the fluid.
The method according to the invention is especially suitable for the removal of components causing turbidity from beer, wine, fruit juice, bacterial suspension, blood, milk, enzyme suspension, etc.
As fruit juice are considered: cherry juice, apple juice, etc.
The present invention has been shown to be especially suitable for the treatment of beer, yielding a particularly clear beer, which beer in addition remains stable during a long storage time.
The asymmetric membrane used is preferably a membrane having a nominal pore size of 0.1-5.0 ,um.
A membrane having a nominal pore size of 0.2-1.0 ,um has proved to be especially suitable. Membranes which according to the invention meet the requirements very well are tubular, flat or capillary.
In the method according to the invention membranes are used that reject certain components, while in many cases it is of great importance that some other components will permeate through the membrane. This is especially important, for instance, for the clarification of beer. As already known, in the production of beer yeast is used, making the beer turbid 21 ~23ss2 which is the reason why after the process the yeast must be removed from the beer. Apart from yeast the beer also contains precipitated proteins, which are also components responsible for poor beer quality. On the other hand beer also contains components that must not be removed during filtration, which components are high molecular weight components attributing to the beer's taste, colour, foam stability, etc. Of course, the same also goes for wine and other fruit juices.
It is especially very important that the high molecu-lar weight colloidal components permeate through during fil-tration of the fluid.
Surprisingly it was found, that the use of hydrophi-lic membranes of the type described in the US patents RE 34296 and 5,076,925 give excellent results. Naturally, the invention is not limited to the above-mentioned membranes.
It has been shown that when using the method accord-ing to the invention particularly good results are obtained when the asymmetric membrane is intermittently back-flushed with a frequency of 1 second to 10 minutes for 0.1-1 second at a counter pressure of 0.5-5 bar.
Intermittent back-flushing of the membrane can, for instance be realized by means of an electronic three-way valve, entirely controlled by computer. The back-flush medium used here is compressed air. Apart from compressed air other suitable back-flush mediums may be used.
Good results are obtained when the fluid to be treated is brought in with a flow velocity below 2 m/s.
Surprisingly it was found, that the method according to the invention can be applied successfully if the pressure difference over the membrane is less than 0.5 bar.
The invention will now be further elucidated by means of the following, non-limitative examples.
In Example I and II standard technology asymmetric ceramic membranes are used, whereby there is no back-flushing in Example I. In Example II back-flushing does take place.
Examples III to IX relate to beer filtration using an asymmetric membrane according to the invention, while Examples X and XI relate to cherry juice filtration, also using an asymmetric membrane according to the invention.
Unfiltered Carlsberg pilsner beer was subjected to filtration using an asymmetric ceramic membrane, whereby no back-flushing was carried out.
This ceramic membrane has a nominal pore size of 1.0 ~cm. The beer was supplied with a crossflow velocity of 0.5 m/s. The pressure difference over the membrane was 0.15 bar.
Within 2 hours the flux of the membrane appeared to decline from 150 to 3 1/m2/h. This rapid flux decline renders such a filtration system without back-flush unsuitable for beer fil-tration.
EXAMPLE II
Again unfiltered Carlsberg pilsner beer was filtered using an asymmetric ceramic membrane, whereby back-flushing did take place.
The nominal pore size, crossflow velocity and pres-sure difference over the membrane are the same as in Example I. Back-flushing was carried out with an interval of 3 seconds, whereby each back-flush lasted 0.05 seconds. By using the same membrane as in Example I, but with back-flushing, the flux was shown to decline in 2 hours from 150 to 70 1/mz/h.
This demonstrates clearly the favourable effect of back-flush-ing on the flux.
EXAMPLE III
Unfiltered Carlsberg pilsner beer was filtered using an asymmetric (X-Flow) membrane, however, without back-flush-ing.
The nominal pore size of the used asymmetric membrane was 0.66 ,um, while the beer was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 1.0 bar. After 6 hours the flux was shown to have declined from 180 to 18 1/m2/h. 750 of proteins of high molecular weight were seen to have permeated.
EXAMPLE IV
Unfiltered Carlsberg pilsner beer was filtered using an asymmetric (X-Flow) membrane.
..~.,.
The nominal pore size of the membrane was 0.66 ~,m, while the beer was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.05 bar.
5 Back-flushing was carried out at an interval of 1 minute, while each back-flush lasted 5 seconds.
After 3 hours the flux was shown to have declined from 120 to 108 1/m2/h.
EXAMPLE V
Unfiltered Carlsberg pilsner beer was filtered using an asymmetric (X-Flow) membrane, with back-flushing.
The pore size was 0.66 ~,m, while the beer was sup-plied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.05 bar.
Back-flushing was carried out every 3 seconds, while each back-flush lasted 0.05 seconds. Surprisingly it was shown that the flux remained constant for 3 days, at 230 1/mz/h.
100% of the proteins of high molecular weight had permeated.
EXAMPLE VI
400 liters beer containing yeast rests (unfiltered Carlsberg pilsner) were filtered. It took 124 minutes to ob-taro 300 liters permeate. The membrane surface measured 1 mz and the transmembrane pressure, the feed pressure was 0.04 tot 0.08 bar, productivity was maintained around 150 1/m2/h. The crossflow velocity was 0.5 m/s.
Every 5 seconds a back-flush pulse was given with a pressure of about 1.5 bar lasting less than 0.1 second. The temperature of the beer was 0°C. The nominal pore size of the membrane was 0.6 ~Cm.
The data show that high velocity back-flushing has a tremendously good effect on the constancy of the membrane pro-ductivity. In standardized figures this is 1875 1/mZ/h/bar.
EXAMPLE VII
The membrane of Example VI was applied with a nominal pore size of 0.6 Vim.
2132x82 In a similar experiment using a crossflow velocity of 2.3 m/s and a pressure of 2 bar an average flux of 80 1/m2/h was achieved without back-flushing, but under otherwise the same conditions. Standardized this means a productivity of 40.
EXAMPLE VIII
In this Example the same membrane was used as in Ex-amples VI and VII.
In the same situation as above a flux was obtained of 30 1/mz/h/bar.
EXAMPLE IX
In this Example the same membrane was used as in Ex-ample VI and VII.
By back-flushing in the conventional manner every 5 minutes for 5 seconds a flux was obtained of 80 1/m2/h/bar.
EXAMPLE X
This Example relates to the filtration of cherry juice using an asymmetric (X-Flow) membrane without back flushing.
The nominal pore size of the membrane was 0.51 ~,m, while the cheery juice was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.5.
After 2 hours the flux was shown to decline from 120 to 5 1/m2/h.
EXAMPLE XI
Cherry juice was filtered by means of an asymmetric (X-Flow) membrane as in Example X, but with back-flushing.
The nominal pore size of the membrane was 0.51 ~,m, while the cherry juice was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.5.
Back-flushing took place every 3 seconds, every time flushing for 0.05 seconds.
After 2 hours the flux was shown to have declined from 120 to 80 1/mz/h.
The application of microfiltration whereby by maintaining a flow along the membrane wall, it is attempted to prevent accumulation of dirt, is a known technique. This tech-nique is generally called crossflow microfiltration.
In practice this technique is applied in, for in-stance, ultrafiltration and microfiltration.
Effective velocities to prevent the build-up of a fouling layer often begin at 2 m/s while as a rule velocities from 4-6 m/s are used.
Dependent on the membrane configuration this is the range where turbulence in the flow occurs.
It should be noted that the technique of back-flush-ing membranes was introduced by Klein and Schneider for self-supporting capillary membranes (Desalination 41 (1982 263-275) whereby microfiltration membranes were applied with a pore size of above 0.01 Vim. For further prior art reference is made to "Microfiltration mit Membranes" by S. Ripperger (ISBN 3-527-28457-5, 1992).
In the above-mentioned known techniques the back-flush is performed once every few minutes, giving a loss of production because part of the permeate is pushed back to the concentrate side of the membrane. A special technique is used by Memtec, who back-flush the membrane with gas (AU-B-34.400/-84). The fastest back-flush intervals are recorded in DK-A-476/90 (APV Pasilac).
Here back-flush frequencies are recorded of 1-10 back-flushes per minute at a back-flush duration of 1-5 seconds. One thing and another results in the fact, that due to these relative long back-flushing times the installation is not in use for filtration for 10-20% of the time.
A disadvantage of the known membrane is that it suf-fers a productivity drop due to the formation of a so-called secondary membrane, consisting of a packing of particles to be filtered off, which partly plug the pores and as layer shows only a limited "own" permeability.
The object of the invention is to provide a method with practically no productivity drop because the thickness of the layer of particles to be filtered off is limited and the secondary membrane is disturbed.
To this end, the present invention provides a process for the removal of components causing turbidity, from a fluid, by means of cross-flow microfiltration, characterized in that the fluid is fed across an asymmetric membrane having a pore structure such that the pores on the feed side of the membrane are larger than the nominal pore size and the pores of nominal pore size occur in the cross section toward the permeate side, the filtered off components are back-flushed from the membrane and are subsequently carried away with the fluid.
The method according to the invention is especially suitable for the removal of components causing turbidity from beer, wine, fruit juice, bacterial suspension, blood, milk, enzyme suspension, etc.
As fruit juice are considered: cherry juice, apple juice, etc.
The present invention has been shown to be especially suitable for the treatment of beer, yielding a particularly clear beer, which beer in addition remains stable during a long storage time.
The asymmetric membrane used is preferably a membrane having a nominal pore size of 0.1-5.0 ,um.
A membrane having a nominal pore size of 0.2-1.0 ,um has proved to be especially suitable. Membranes which according to the invention meet the requirements very well are tubular, flat or capillary.
In the method according to the invention membranes are used that reject certain components, while in many cases it is of great importance that some other components will permeate through the membrane. This is especially important, for instance, for the clarification of beer. As already known, in the production of beer yeast is used, making the beer turbid 21 ~23ss2 which is the reason why after the process the yeast must be removed from the beer. Apart from yeast the beer also contains precipitated proteins, which are also components responsible for poor beer quality. On the other hand beer also contains components that must not be removed during filtration, which components are high molecular weight components attributing to the beer's taste, colour, foam stability, etc. Of course, the same also goes for wine and other fruit juices.
It is especially very important that the high molecu-lar weight colloidal components permeate through during fil-tration of the fluid.
Surprisingly it was found, that the use of hydrophi-lic membranes of the type described in the US patents RE 34296 and 5,076,925 give excellent results. Naturally, the invention is not limited to the above-mentioned membranes.
It has been shown that when using the method accord-ing to the invention particularly good results are obtained when the asymmetric membrane is intermittently back-flushed with a frequency of 1 second to 10 minutes for 0.1-1 second at a counter pressure of 0.5-5 bar.
Intermittent back-flushing of the membrane can, for instance be realized by means of an electronic three-way valve, entirely controlled by computer. The back-flush medium used here is compressed air. Apart from compressed air other suitable back-flush mediums may be used.
Good results are obtained when the fluid to be treated is brought in with a flow velocity below 2 m/s.
Surprisingly it was found, that the method according to the invention can be applied successfully if the pressure difference over the membrane is less than 0.5 bar.
The invention will now be further elucidated by means of the following, non-limitative examples.
In Example I and II standard technology asymmetric ceramic membranes are used, whereby there is no back-flushing in Example I. In Example II back-flushing does take place.
Examples III to IX relate to beer filtration using an asymmetric membrane according to the invention, while Examples X and XI relate to cherry juice filtration, also using an asymmetric membrane according to the invention.
Unfiltered Carlsberg pilsner beer was subjected to filtration using an asymmetric ceramic membrane, whereby no back-flushing was carried out.
This ceramic membrane has a nominal pore size of 1.0 ~cm. The beer was supplied with a crossflow velocity of 0.5 m/s. The pressure difference over the membrane was 0.15 bar.
Within 2 hours the flux of the membrane appeared to decline from 150 to 3 1/m2/h. This rapid flux decline renders such a filtration system without back-flush unsuitable for beer fil-tration.
EXAMPLE II
Again unfiltered Carlsberg pilsner beer was filtered using an asymmetric ceramic membrane, whereby back-flushing did take place.
The nominal pore size, crossflow velocity and pres-sure difference over the membrane are the same as in Example I. Back-flushing was carried out with an interval of 3 seconds, whereby each back-flush lasted 0.05 seconds. By using the same membrane as in Example I, but with back-flushing, the flux was shown to decline in 2 hours from 150 to 70 1/mz/h.
This demonstrates clearly the favourable effect of back-flush-ing on the flux.
EXAMPLE III
Unfiltered Carlsberg pilsner beer was filtered using an asymmetric (X-Flow) membrane, however, without back-flush-ing.
The nominal pore size of the used asymmetric membrane was 0.66 ,um, while the beer was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 1.0 bar. After 6 hours the flux was shown to have declined from 180 to 18 1/m2/h. 750 of proteins of high molecular weight were seen to have permeated.
EXAMPLE IV
Unfiltered Carlsberg pilsner beer was filtered using an asymmetric (X-Flow) membrane.
..~.,.
The nominal pore size of the membrane was 0.66 ~,m, while the beer was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.05 bar.
5 Back-flushing was carried out at an interval of 1 minute, while each back-flush lasted 5 seconds.
After 3 hours the flux was shown to have declined from 120 to 108 1/m2/h.
EXAMPLE V
Unfiltered Carlsberg pilsner beer was filtered using an asymmetric (X-Flow) membrane, with back-flushing.
The pore size was 0.66 ~,m, while the beer was sup-plied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.05 bar.
Back-flushing was carried out every 3 seconds, while each back-flush lasted 0.05 seconds. Surprisingly it was shown that the flux remained constant for 3 days, at 230 1/mz/h.
100% of the proteins of high molecular weight had permeated.
EXAMPLE VI
400 liters beer containing yeast rests (unfiltered Carlsberg pilsner) were filtered. It took 124 minutes to ob-taro 300 liters permeate. The membrane surface measured 1 mz and the transmembrane pressure, the feed pressure was 0.04 tot 0.08 bar, productivity was maintained around 150 1/m2/h. The crossflow velocity was 0.5 m/s.
Every 5 seconds a back-flush pulse was given with a pressure of about 1.5 bar lasting less than 0.1 second. The temperature of the beer was 0°C. The nominal pore size of the membrane was 0.6 ~Cm.
The data show that high velocity back-flushing has a tremendously good effect on the constancy of the membrane pro-ductivity. In standardized figures this is 1875 1/mZ/h/bar.
EXAMPLE VII
The membrane of Example VI was applied with a nominal pore size of 0.6 Vim.
2132x82 In a similar experiment using a crossflow velocity of 2.3 m/s and a pressure of 2 bar an average flux of 80 1/m2/h was achieved without back-flushing, but under otherwise the same conditions. Standardized this means a productivity of 40.
EXAMPLE VIII
In this Example the same membrane was used as in Ex-amples VI and VII.
In the same situation as above a flux was obtained of 30 1/mz/h/bar.
EXAMPLE IX
In this Example the same membrane was used as in Ex-ample VI and VII.
By back-flushing in the conventional manner every 5 minutes for 5 seconds a flux was obtained of 80 1/m2/h/bar.
EXAMPLE X
This Example relates to the filtration of cherry juice using an asymmetric (X-Flow) membrane without back flushing.
The nominal pore size of the membrane was 0.51 ~,m, while the cheery juice was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.5.
After 2 hours the flux was shown to decline from 120 to 5 1/m2/h.
EXAMPLE XI
Cherry juice was filtered by means of an asymmetric (X-Flow) membrane as in Example X, but with back-flushing.
The nominal pore size of the membrane was 0.51 ~,m, while the cherry juice was supplied with a velocity of 0.5 m/s.
The pressure difference over the membrane was 0.5.
Back-flushing took place every 3 seconds, every time flushing for 0.05 seconds.
After 2 hours the flux was shown to have declined from 120 to 80 1/mz/h.
Claims (9)
1. A process for the removal of components causing turbidity, from a fluid, by means of cross-flow microfiltration, characterized in that the fluid is fed across an asymmetric membrane having a pore structure such that the pores on the feed side of the membrane are larger than the nominal pore size and the pores of nominal pore size occur in the cross section toward the permeate side, the filtered off components are back-flushed from the membrane and are subsequently carried away with the fluid.
2. A process according to claim 1, characterized in that the fluid is selected from the group including beer, wine, fruit juice, bacterial suspension, blood, milk and enzyme suspension.
3. A process according to claim 1 or 2, characterized in that the fluid is beer.
4. A process according to claims 1-3, characterized in that the asymmetric membrane used is a microporous membrane having a nominal pore size of 0.1-5.0 µm.
5. A process according to claim 4, characterized in that the nominal pore size is 0.2-1.0 µm.
6. A process according to claims 1-5, characterized in that the membrane is tubular, flat or capillary.
7. A process according to claims 1-6, characterized in that back-flushing of the membrane takes place intermittently with a frequency of 1 second to 10 minutes for 0.1-1 second at a counter pressure of 0.5-5 bar.
8. A process according to claim 7, characterized in that the feed velocity is below 2 m/s.
9. A process according to claims 1-8, characterized in that the pressure difference over the membrane is less than 0.5 bar.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL9301653A NL9301653A (en) | 1993-09-24 | 1993-09-24 | Method for removing turbidizing constituents from a liquid by microfiltration. |
| NL9301653 | 1993-09-24 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2132682A1 CA2132682A1 (en) | 1995-03-25 |
| CA2132682C true CA2132682C (en) | 2000-04-18 |
Family
ID=19862921
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002132682A Expired - Fee Related CA2132682C (en) | 1993-09-24 | 1994-09-22 | Method for the removal of components causing turbidity, from a fluid, by means of microfiltration |
Country Status (9)
| Country | Link |
|---|---|
| US (1) | US5560828A (en) |
| EP (1) | EP0645174B1 (en) |
| JP (1) | JPH07155559A (en) |
| AT (1) | ATE213660T1 (en) |
| CA (1) | CA2132682C (en) |
| DE (1) | DE69419296T2 (en) |
| DK (1) | DK0645174T3 (en) |
| ES (1) | ES2135536T3 (en) |
| NL (1) | NL9301653A (en) |
Families Citing this family (26)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL1004210C2 (en) * | 1996-10-07 | 1998-04-10 | Prime Water Systems N V | Water filtration device. |
| GB2320256A (en) * | 1996-12-11 | 1998-06-17 | Brf International | Beer filtration |
| BR0012993A (en) * | 1999-08-05 | 2002-06-18 | Microfiltration Technology Aps | Cross-flow filtering method and a cross-flow filtering installation |
| EP1184070A3 (en) | 2000-09-01 | 2003-12-17 | Haldor Topsoe A/S | Method for the removal of particulate matter from aqueous suspension |
| AU2002357338A1 (en) * | 2002-01-09 | 2003-07-30 | Hydranautics | Methods for improving filtration performance of hollow fiber membranes |
| SI2298436T1 (en) * | 2002-06-19 | 2014-12-31 | Nortwest Biotherapeutics, Inc. | Use of a tangential flow filtration device and methods for leukocyte enrichment |
| DE10231835B4 (en) * | 2002-07-12 | 2004-05-19 | Sartorius Ag | Process for crossflow filtration of beverages |
| DE10354571B4 (en) * | 2003-11-21 | 2011-05-05 | Sartorius Stedim Biotech Gmbh | Process for the production of spirits |
| US7790039B2 (en) * | 2003-11-24 | 2010-09-07 | Northwest Biotherapeutics, Inc. | Tangential flow filtration devices and methods for stem cell enrichment |
| US7392811B2 (en) | 2004-02-23 | 2008-07-01 | Ecolab Inc. | Delivery head for multiple phase treatment composition, vessel including a delivery head, and method for treating a vessel interior surface |
| US7220358B2 (en) | 2004-02-23 | 2007-05-22 | Ecolab Inc. | Methods for treating membranes and separation facilities and membrane treatment composition |
| US7247210B2 (en) | 2004-02-23 | 2007-07-24 | Ecolab Inc. | Methods for treating CIP equipment and equipment for treating CIP equipment |
| US20080004205A1 (en) | 2006-06-30 | 2008-01-03 | Millipore Corporation | Ultrafiltration membranes and methods of making |
| JP4748655B2 (en) * | 2004-06-25 | 2011-08-17 | ミリポア・コーポレイション | Ultrafiltration membrane and manufacturing method |
| EP1642636A1 (en) * | 2004-09-30 | 2006-04-05 | HydroSep AG | Fluid treatment system and method |
| EP1721656A1 (en) * | 2005-05-04 | 2006-11-15 | Filtrox AG | Membrane, membrane module and process for cross-flow depth filtration |
| US20060254984A1 (en) * | 2005-05-16 | 2006-11-16 | Uspolyresearch | Hollow Fiber Membrane Adsorber and Process for the Use Thereof |
| DE102006026081B4 (en) * | 2006-06-03 | 2014-11-27 | Sartorius Stedim Biotech Gmbh | Process for the preparation of ready-to-drink spirits |
| US20080093277A1 (en) * | 2006-06-13 | 2008-04-24 | John Armour | Cadence detection in a sequence of video fields |
| US10632237B2 (en) * | 2006-10-09 | 2020-04-28 | Minnetronix, Inc. | Tangential flow filter system for the filtration of materials from biologic fluids |
| US10850235B2 (en) | 2006-10-09 | 2020-12-01 | Minnetronix, Inc. | Method for filtering cerebrospinal fluid (CSF) including monitoring CSF flow |
| EP2335814B1 (en) | 2008-09-26 | 2016-12-28 | Asahi Kasei Kabushiki Kaisha | Use of porous hollow-fiber membrane for producing clarified biomedical culture medium |
| US9055752B2 (en) * | 2008-11-06 | 2015-06-16 | Intercontinental Great Brands Llc | Shelf-stable concentrated dairy liquids and methods of forming thereof |
| UA112972C2 (en) | 2010-09-08 | 2016-11-25 | Інтерконтінентал Грейт Брендс ЛЛС | LIQUID DAIRY CONCENTRATE WITH A HIGH CONTENT OF DRY SUBSTANCES |
| ES2944452T3 (en) | 2015-12-04 | 2023-06-21 | Minnetronix Inc | Cerebrospinal fluid conditioning systems |
| EP3680319B1 (en) * | 2017-09-07 | 2024-01-24 | Asahi Kasei Kabushiki Kaisha | Method for manufacturing brewed alcoholic beverage using porous membrane |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NZ190436A (en) * | 1978-05-15 | 1981-12-15 | Pall Corp | Preparation of skinless hydrophilic alcohol insoluble polyamide membranes membranes casting resin solutions |
| US4629563B1 (en) * | 1980-03-14 | 1997-06-03 | Memtec North America | Asymmetric membranes |
| US4333972A (en) * | 1980-06-25 | 1982-06-08 | Puropore, Inc. | Highly anisotropic membranes |
| JPS6227006A (en) * | 1985-07-27 | 1987-02-05 | Fuji Photo Film Co Ltd | Microporous membrane |
| NL8602402A (en) * | 1986-09-23 | 1988-04-18 | X Flow Bv | METHOD FOR MANUFACTURING HYDROFILE MEMBRANES AND SIMILAR MEMBRANES |
| US5064580A (en) * | 1988-03-31 | 1991-11-12 | The Dow Chemical Company | Process for making microporous membranes from poly(etheretherketone)-type polymers |
| DE3818860A1 (en) * | 1988-06-03 | 1989-12-07 | Seitz Filter Werke | FILTER ELEMENT |
| US4897465A (en) * | 1988-10-12 | 1990-01-30 | Abbott Laboratories | Enrichment and concentration of proteins by ultrafiltration |
| NL8901090A (en) * | 1989-04-28 | 1990-11-16 | X Flow Bv | METHOD FOR MANUFACTURING A MICROPOROUS MEMBRANE AND SUCH MEMBRANE |
| DK166435B1 (en) * | 1990-02-22 | 1993-05-24 | Apv Pasilac As | Method for removal of microorganisms during microfiltration of a material of a primary membrane filter without significant formation of a secondary membrane, as well as apparatus for use during performance of the method |
| US5221479A (en) * | 1991-02-15 | 1993-06-22 | Fuji Photo Film Co., Ltd. | Filtration system |
| DE4105210C1 (en) * | 1991-02-20 | 1992-03-19 | Sempas Membrantechnik Gmbh, 7240 Horb, De | Cross-flow micro-filter for particle concn. in suspension - is cyclically backflushed to prevent passage of small particles through funnel-shaped pores |
| US5344565A (en) * | 1993-07-26 | 1994-09-06 | Pall Corporation | Method of treating a clogged porous medium |
-
1993
- 1993-09-24 NL NL9301653A patent/NL9301653A/en active Search and Examination
-
1994
- 1994-09-05 AT AT94202524T patent/ATE213660T1/en not_active IP Right Cessation
- 1994-09-05 DK DK94202524T patent/DK0645174T3/en active
- 1994-09-05 EP EP94202524A patent/EP0645174B1/en not_active Revoked
- 1994-09-05 ES ES94202524T patent/ES2135536T3/en not_active Expired - Lifetime
- 1994-09-05 DE DE69419296T patent/DE69419296T2/en not_active Expired - Fee Related
- 1994-09-21 JP JP6226912A patent/JPH07155559A/en active Pending
- 1994-09-22 CA CA002132682A patent/CA2132682C/en not_active Expired - Fee Related
- 1994-09-23 US US08/312,481 patent/US5560828A/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| DE69419296T2 (en) | 2003-02-13 |
| JPH07155559A (en) | 1995-06-20 |
| ATE213660T1 (en) | 2002-03-15 |
| EP0645174A1 (en) | 1995-03-29 |
| US5560828A (en) | 1996-10-01 |
| NL9301653A (en) | 1995-04-18 |
| DK0645174T3 (en) | 1999-11-22 |
| DE69419296D1 (en) | 2002-07-11 |
| ES2135536T3 (en) | 2002-10-01 |
| CA2132682A1 (en) | 1995-03-25 |
| EP0645174B1 (en) | 2002-02-27 |
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| Date | Code | Title | Description |
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| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20140923 |