EP4135882A1 - Vorrichtung und verfahren zum filtrieren von bier - Google Patents
Vorrichtung und verfahren zum filtrieren von bierInfo
- Publication number
- EP4135882A1 EP4135882A1 EP21712487.4A EP21712487A EP4135882A1 EP 4135882 A1 EP4135882 A1 EP 4135882A1 EP 21712487 A EP21712487 A EP 21712487A EP 4135882 A1 EP4135882 A1 EP 4135882A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- unfiltrate
- membrane filter
- buffer tank
- line
- sediment
- 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.)
- Withdrawn
Links
- 238000001914 filtration Methods 0.000 title claims abstract description 122
- 235000013405 beer Nutrition 0.000 title claims abstract description 77
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 172
- 239000013049 sediment Substances 0.000 claims abstract description 108
- 238000009295 crossflow filtration Methods 0.000 claims abstract description 6
- 239000012141 concentrate Substances 0.000 claims description 93
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 51
- 239000002245 particle Substances 0.000 claims description 44
- 239000000706 filtrate Substances 0.000 claims description 22
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 20
- 230000001105 regulatory effect Effects 0.000 claims description 19
- 238000007599 discharging Methods 0.000 claims description 2
- 239000012530 fluid Substances 0.000 abstract description 10
- 239000012071 phase Substances 0.000 description 20
- 210000005253 yeast cell Anatomy 0.000 description 16
- 239000007787 solid Substances 0.000 description 13
- 230000008569 process Effects 0.000 description 9
- 238000003860 storage Methods 0.000 description 9
- 238000004140 cleaning Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000011001 backwashing Methods 0.000 description 7
- 230000008901 benefit Effects 0.000 description 5
- 238000011049 filling Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- 238000009285 membrane fouling Methods 0.000 description 3
- 239000003381 stabilizer Substances 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 2
- 239000012459 cleaning agent Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000005374 membrane filtration Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000008092 positive effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000000654 additive Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 235000015110 jellies Nutrition 0.000 description 1
- 239000008274 jelly Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 235000015047 pilsener Nutrition 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 235000013809 polyvinylpolypyrrolidone Nutrition 0.000 description 1
- 229920000523 polyvinylpolypyrrolidone Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000012465 retentate Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000002699 waste material 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
- B01D61/147—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
- B01D61/18—Apparatus therefor
-
- 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
- B01D61/22—Controlling or regulating
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12C—BEER; PREPARATION OF BEER BY FERMENTATION; PREPARATION OF MALT FOR MAKING BEER; PREPARATION OF HOPS FOR MAKING BEER
- C12C11/00—Fermentation processes for beer
- C12C11/11—Post fermentation treatments, e.g. carbonation, or concentration
-
- 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
-
- 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
- B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
Definitions
- the invention relates to a device for filtering beer and a method according to the preambles of claims 1 and 9.
- the beer is filtered after fermentation / maturation in order to remove yeast and cloud particles from the beer. If the beer has stabilized (e.g. with xerogel or PVPP) before filtration, these substances must also be removed.
- Membrane filtration of beer has been an increasingly accepted technology for several years.
- Various materials are used as the membrane, for example hollow plastic fibers or ceramic filter candles with microfiltration pores.
- the crossflow method is used, in which the unfiltered beer, i.e. the unfiltrate (UF), is circulated through the membrane filter and the filtrate is withdrawn from the membrane filter. The unfiltrate is guided along the membrane, the filtrate exiting perpendicular to it.
- the unfiltrate side inevitably concentrates on.
- a membrane filter e.g. comprises several modules, i.e. filter modules.
- a module is understood to be a housing in which the membrane (s) are arranged and which has an unfiltrate inlet, a filtrate outlet and a concentrate outlet.
- modules are grouped together to form membrane filter units (ME) that can be operated in parallel.
- Each membrane filter unit has a return line via which the concentrate from the modules is returned as unfiltrate to the modules for filtration and can be returned to a concentrate collecting line to return the concentrate to the unfiltrate buffer tank.
- an unfiltrate buffer tank is provided through which the unfiltrate is fed to the membrane filter.
- the unfiltrate sediments in the unfiltrate buffer tank.
- the membrane filter concentrates the unfiltrate (and thus the contained particle load), via a concentrate collecting line leading to the unfiltrate buffer tank, part of the unfiltrate can be returned as concentrate to the unfiltrate buffer tank.
- An unfiltrate buffer tank can have a lateral and a lower outlet opening. From the side outlet of the unfiltrate buffer tank, the unfiltrate has a low particle load / concentration at the beginning of the filtration (which corresponds to the concentration of the beer that is conveyed from the storage cellar).
- the particles for example yeast, can sediment from the start of the process (the start of the process also includes the filling of the unfiltrate buffer tank) on and in the course of the filtration (duration) in the unfiltrate buffer tank and are deposited in the lower area of the unfiltrate buffer tank.
- the lower area of the tank thus has an increased particle load / concentration, in particular if the particle load / concentration is increased over time through the membrane filter, because unfiltrate, i.e. concentrate from the membrane filter, is fed back into the unfiltrate buffer tank.
- the filter either receives a continuously increasing particle load, which means that later filtration cycles start with a higher concentration, or the filter suddenly receives a large particle load when switching from the side to the lower outlet. It is particularly critical if the membrane filter is loaded abruptly via the lower drain. This is also disadvantageous because the trans membrane pressure then increases very sharply.
- TMD transmembrane pressure
- a filtration cycle begins when the unfiltrate is fed into the filtration unit and ends, for example, when a maximum transmembrane pressure is reached or after a certain time.
- a filtration cycle is understood to mean the period of approximately 1 hour to 6 hours.
- a cycle series is understood to mean several, approximately four to eight filtration cycles.
- the pure filtration time of a cycle series is about 20 to 30 hours.
- the membrane can be cleared with a short ("simple", which takes one to two hours, for example), mostly only alkaline treatment (a so-called “regeneration") like that, since a large part of the "membrane fouling" can be removed and it follows the next filtration cycle. If the filtration cycles are too small because the regeneration is no longer sufficient, a long (“intensive”, which takes four to eight hours, for example) cleaning usually takes place with various cleaning agents and cleaning agent additives to eliminate the “membrane fouling”. With this long cleaning, the series of filtration cycles is completed.
- the present invention is based on the object of providing a device and a method for filtering beer which enable filtration with an adjustable, in particular as constant as possible, particle load of the unfiltrate over several filtration cycles.
- the device according to the invention has at least one membrane filter, in particular at least one membrane filter unit with several modules for crossflow filtration.
- a membrane filter can also comprise only one module.
- the device has an unfiltrate buffer tank, wherein unfiltrate can be circulated through the unfiltrate buffer tank and the at least one membrane filter.
- the concentrate collecting line is understood to be the line through which the concentrate from the at least one membrane filter is returned to the unfiltrate buffer tank.
- the unfiltrate buffer tank has a drain at its lower end and an upper, in particular lateral, drain above it.
- the lower outlet can be arranged, for example, at the lowest point of the unfiltrate buffer tank.
- the invention is not limited to a lower drain and can also have a further drain (for example a tank outlet, as will be explained in more detail below), the two drains then being able to open into a common line.
- the term upper flow is to be understood in the sense of at least one upper flow.
- the overlying drain is arranged in an upper area of the unfiltrate buffer tank and preferably extends from the side wall, ie the frame. It is alternatively also possible that the upper drain is located in a cover or cone and, for example, comprises a pipeline that protrudes into the upper area of the unfiltrate buffer tank in order to draw off unfiltrate with its opening at the corresponding height in the upper area. Such a pipeline can also extend from the frame of the tank into the upper region of the tank in order to draw off unfiltrate there.
- the upper area is understood here to mean, for example, the upper half of an unfiltrate buffer tank.
- the upper, in particular, lateral outlet of the unfiltrate buffer tank is connected to at least one membrane filter via an unfiltrate line. Unfiltrate can be conducted to the at least one membrane filter via the unfiltrate line.
- the unfiltrate buffer tank is, for example, connected to the unfiltrate line with a valve, for example a double seat valve, when open.
- Sediment can be added to the unfiltrate via the lower outlet of the unfiltrate buffer tank via a metering device. Because the sediment from the lower area of the unfiltrate buffer tank can be added to the unfiltrate withdrawn from an upper area, the particle load, that is, the solids per volume of liquid, can be set in a desired area. If there are several membrane filters, i.e. membrane filter units, they can be started at different times. It is then possible for the membrane filters to have a particle load in the same range regardless of the starting time of the filtration. This particle load can therefore in particular be kept essentially constant, which has a very positive effect on the course of the filtration.
- the arrangement according to the invention also offers the possibility that degassed water can be added to the sediment at the end of the filtration cycle, i.e. before cleaning, which has the advantage that the highly concentrated content in the lower area of the Unfiltrate buffer tanks can filter even more beer and thus increase system efficiency, or when the sediment is expelled into the gully, beer losses are significantly reduced.
- water is added to the sediment, it is possible that the wort previously produced in the process in the brewhouse is brewed with a higher original wort (extract content).
- sediment is understood to mean concentrated unfiltrate which is removed from the lower area of the unfiltrate buffer tank and which in particular has a higher particle load than unfiltrate which is removed via the upper outlet.
- the lower outlet of the unfiltrate buffer tank is advantageously connected to the unfiltrate line via a first metering line at a metering point D, the metering device being arranged in the metering line.
- This arrangement is particularly suitable for metering in the sediment during the filtration.
- the at least one membrane filter unit each has an unfiltrate inlet, a filtrate outlet and a concentrate outlet which opens into a concentrate collecting line.
- the lower outlet of the unfiltrate buffer tank is connected to the concentrate outlet of the at least one membrane filter unit via a line. Then the sediment in the membrane filter unit can be fed to the unfiltrate or, when pushed out, to the water and filtered.
- This arrangement is particularly suitable for adding the sediment at the end of a filtration cycle, i.e. shortly before the intermediate cleaning, when the unfiltrate in the membrane filter is expelled with water, for example.
- the metering device advantageously comprises a pump, in particular a metering pump, which can be controlled and convey a specific volume flow of sediment in the direction of the unfiltered fluid. It is also possible, for example, to provide a pump with a flow meter and / or an additional control valve as the metering device.
- the device comprises a control via which the amount / time of sediment that is metered into the unfiltrate can be metered in in a regulated manner.
- a measured value acts as an actual value for the control and is compared with a set target value or, for example, a previously empirically determined amount / time of sediment can be added.
- the dosed amount / time of sediment can be dosed depending on the following measured values:
- Transmembrane pressure on at least one of the modules of the membrane filter unit can be carried out in a simple manner by adding a certain percentage of its volume of sediment to the unfiltrate.
- the device can also have a device for measuring the turbidity or a value proportional thereto.
- the turbidity can, for example, be measured optically, for example with a transmitted light sensor or scattered light sensor; a 25 ° or 90 ° turbidity measurement is common, and the turbidity can be specified as an EBC unit.
- the turbidity is proportional to the particle load.
- other values can also be measured which are proportional to the particle load or turbidity, such as, for example, viscosity, viscoelasticity, conductivity or density.
- the turbidity can be measured simply and inexpensively.
- a desired particle load can thus be set and maintained in a simple manner.
- the device for measuring the turbidity or a proportional value is preferably located between the dosing point D, at which the dosing line opens into the unfiltrate line, and the at least one membrane filter.
- the particle load can thus be measured in front of the at least one membrane filter.
- the lower area of the unfiltrate buffer tank is preferably designed in such a way that it tapers conically downwards, for example the opening angle of the cone is between 60 and 70 °.
- the conical bottom allows the sediment to be drawn off particularly easily.
- the upper or side drain can preferably be arranged in the upper half of the unfiltrate buffer tank. This upper half ensures that there is no sediment. In any case, the upper drain should be above the conical area.
- the lower drain can comprise a tank outlet nozzle, in the form of a drain pipe, which protrudes into the unfiltrate buffer tank from below, in such a way that sediment can drain through the drain pipe and / or through an area between the drain pipe and the tank wall of the unfiltrate buffer tank, preferably via valves , in particular control valves, it is possible to set whether sediment is to be diverted from the unfiltrate buffer tank through the drain pipe and / or the area between the drain pipe and the tank wall.
- the area between the drain pipe and the tank wall can be diverted from the unfiltrate buffer tank separately in a separate line to the membrane filter.
- two lower outlets can be present, the tank outlet nozzle which protrudes into the unfiltrate buffer tank for the (preferably continuous) dosing into the unfiltrate line during the filtration and the lower outlet for direct feeding into the concentrate outlet of the corresponding Membrane filter.
- the membrane can block more quickly, so it is advantageous if the sediment can settle in the unfiltrate buffer tank.
- the tank outlet nozzle can guarantee that sediment with a lower particle load (via the dosing device) is dosed during the filtration (continuously) via the tank outlet nozzle and that sediment with the highest particle load can be dosed at the end of a filter cycle and so can the membrane blocked less quickly during the filtration cycle.
- unfiltrate in the form of beer is filtered from an unfiltrate buffer tank with at least one membrane filter and unfiltrate is recycled to the unfiltrate buffer tank as concentrate.
- membrane filters can be operated in parallel, for example, with the concentrate from each membrane filter being fed into a common concentrate collecting line, for example, and then being returned to the unfiltrate buffer tank.
- Unfiltrate is removed from the unfiltrate buffer tank from an upper, in particular lateral outlet and sediment is removed via an un direct outlet at the lower end of the unfiltrate buffer tank and added to the unfiltrate at least temporarily.
- the particle load can be set in a defined manner during the entire filtration and can also be kept constant in a certain range.
- the sediment can in particular be metered in in a regulated manner, with the metered amount / time (i.e., for example, the volume flow) of sediment being able to be regulated as a function of a measured value, in particular as a function of the turbidity or a proportional value of the unfiltrate and / or the sediment and / or as a function of the flow rate, in particular of the unfiltrate and / or the sediment and / or as a function of a transmembrane pressure on at least one of the modules of a membrane filter unit.
- the metered amount / time i.e., for example, the volume flow
- turbidity or flow of the unfiltrate or sediment means that the corresponding value of the unfiltrate or sediment is measured in line sections before the dosing and a desired mixing ratio can be determined and set or regulated on this basis, for example the volume flow of the unfiltrate can be determined before the dosing point and the volume flow of the sediment before the dosing point can then be regulated to a desired value - or vice versa.
- turbidity or flow of the unfiltrate and sediment means that the corresponding value is measured before the dosing point for both sediment and unfiltrate or is also measured in a line section after the dosing point, i.e. at a point where the Sediment has already been added to the unfiltrate. Then, e.g. when measuring the turbidity, the volume flow of the sediment can be adjusted in such a way that an actual value can be regulated to a target value.
- the setpoint is not constant in the control during a filtration cycle and is selected, for example, so that the particle load is initially moderate at the beginning of a filtration cycle, then increases slightly in the middle of the filtration cycle and towards the end of the Filtration cycle decreases and increases again when the sediment is pushed out of the unfiltrate buffer tank with water.
- the unfiltrate is concentrated in the unfiltrate buffer tank and can be reduced by adding sediment to the unfiltrate from the unfiltrate buffer tank, which has the function of a sedimentation tank, as already explained, either into the unfiltrate line in front of the at least one membrane filter and / or into the at least one membrane filter, in particular in the concentrate drain of the at least one membrane filter.
- the sediment is introduced from the lower outlet of the unfiltrate buffer tank into a concentrate outlet of the at least one membrane filter, ie introduced backwards and then introduced into the unfiltrate stream and filtered.
- the valves in the membrane filter unit are switched in such a way that the concentrate that leaves the individual modules is fed back to the modules as unfiltrate in a return line and is not diverted into the concentrate collecting line and then the sediment and water also as unfilt council can be fed to the individual modules.
- At least one of several membrane filter units is in a filtration cycle and is filtering unfiltrate from the unfiltrate buffer tank
- at least one other membrane filter unit can be operated in such a way that water, in particular degassed water, is continuously passed through this membrane filter unit and sediment from the lower drain of the unfiltrate buffer tank and / or yeast beer or gelager beer is introduced into a concentrate drain of the corresponding membrane filter unit and is thus introduced into the water flow and filtered.
- This alternative operating mode can therefore not only be carried out at the end of a filtration cycle, but also as a continuous filtration process for several hours (for example 1 to 6 hours, i.e. the duration of a filtration cycle) for at least one selected membrane filter unit.
- the device is operated during a filtration cycle series over a time interval t before the tank is emptied, for example, and the device is cleaned, for example, wherein there are several successive filtration cycles during the time interval t and the particle load (solids per Volume of liquid), in particular the yeast concentration, is set or regulated in filtration cycles in such a way that the maximum particle load does not exceed a limit value and is essentially constant, which means that large fluctuations can be avoided. In other words, if there are several successive filtration cycles, essentially the same particle loads can always be assumed.
- an additional connection can be provided in the line that leads from the lower outlet of the unfiltrate buffer tank to the concentrate outlet of the respective at least one membrane filter, which is connected in particular to a tank or other system for yeast beer or gelager beer for recovery, wherein the concentrate control valve takes over the dosing function.
- a connection for water can be provided in such a way that water can be passed through the respective membrane filter in addition to the unfiltrate or as an alternative to the unfiltrate.
- the unfiltrate can be introduced into the unfiltrate buffer tank via a tangential inlet.
- upper drain is to be understood in the sense of at least one upper drain through which the unfiltrate can be withdrawn from the upper area of the unfiltrate buffer tank.
- the present invention also relates to a device for filtering beer with at least one membrane filter, in particular at least one membrane filter unit with several modules, for crossflow filtration.
- the membrane filter has an unfiltrate line for supplying unfiltrate.
- the membrane filter is also connected to a filtrate line for discharging the filtrate produced and a return line for the concentrate via which the unfiltrate leaves the crossflow filter and can be recycled.
- the device has a collecting tank which is connected to the membrane filter via the return line for the concentrate and the unfiltrate line and preferably additionally via the filtrate line. It is advantageous if the collecting tank is also connected to the filtrate line, since then, for example, corresponding mixed phases can be passed from the filter into the collecting tank.
- this interconnection enables greater process freedom and increases efficiency. It is irrelevant from which point the filtrate line, the return line and the unfiltrate line open into the collection tank.
- a valve device is also provided which can be switched in such a way that a medium can at least partially or completely be conducted into the collecting tank via the filtrate line and / or the return line for concentrate and / or can be conducted from the collecting tank back to the membrane filter, in particular in the Unfiltratlei device and / or return line for concentrate. It is thus possible to route mixed phases, for example beer and water or backwashing liquid such as a mixture of beer and water, beer or water from the filter into the collection tank, or else concentrate with a high solids content I.
- the collection tank is advantageously provided in addition to an unfiltrate buffer tank, with unfiltrate preferably being able to circulate through the unfiltrate buffer and the at least one membrane filter, and with the collection tank being connected in particular to the lower outlet of the unfiltrate buffer tank.
- An additional collection tank in addition to the unfiltrate buffer tank is advantageous because, for example, the unfiltrate or concentrate can circulate via the unfiltrate buffer tank during the filtration and the separate collection tank does not affect the ongoing filtration. Inserts and mixed phases from the collection tank can be fed back into the filtration process at any point in time or added to the unfiltrate that is fed to the membrane filter.
- the contents of the collection tank can also be returned to the unfiltrate buffer tank.
- the main advantage of this additional collection tank is that, for example, mixed phases that had to be discarded can now be reused at a later point in time without affecting the ongoing filtration, which would be the case if the corresponding mixed phases were returned to the unfiltrate buffer tank would.
- the use of two tanks thus enables process optimization.
- the present invention is explained in more detail with reference to the following figures.
- FIG. 1 shows, roughly schematically, an embodiment according to the present invention.
- FIG. 1a schematically shows a section of FIG. 1 during production.
- Figure 1b shows schematically a section of Figure 1 at the end of the filtration cycle.
- FIG. 2 shows schematically a diagram which shows the yeast concentration as a function of the filtration time.
- FIG. 3 shows schematically an unfiltrate buffer tank with a tank outlet nozzle.
- FIG. 4 schematically shows an embodiment in which discharges, mixed phases and concentrates are fed to a collecting tank and reused.
- FIG. 1 shows, roughly schematically, an embodiment according to the present invention.
- the device 1 comprises an unfiltrate buffer tank 3 which, for example, has a filling volume in a range from 5 hl to 500 hl.
- the unfiltrate buffer tank 3 is designed in such a way that its lower end tapers conically, in particular at an opening angle ⁇ of 60 to 70 °.
- a lower outlet 4 At the lower end of the conical area there is a lower outlet 4, which leads into a metering line 12, 16, in particular via a valve, in particular a double seat valve 80.
- a tank outlet nozzle to be provided, as shown in FIG. 3 and explained in more detail below.
- the unfiltrate buffer tank 3 has an upper outlet 5, which is arranged above the lower outlet 4.
- the upper drain 5 is a lateral drain which is arranged, for example, in the frame of the unfiltrate buffer tank 3.
- the upper outlet 5 is located above the conical area, preferably in the upper half of the unfiltrate buffer tank 3. In this area, a strong concentration of the unfiltrate due to sedimentation is not to be expected.
- the upper drain 5 can also be designed in such a way that it does not draw off the unfiltrate via the side wall, but rather via a cover or cone the upper half of the tank opens.
- the unfiltrate buffer tank 3 also has an inlet 20, in particular a lateral inlet, which is also arranged above the lower outlet 4, preferably above the conical area and preferably below the upper outlet 5.
- the inlet 20 is preferably essentially as a tangential inlet pronounced so that the introduction is tangential or with a tangential directional component.
- UF unfiltrate
- QIT measuring instruments
- the lateral outlet 5 opens via a discharge line 6a into the unfiltrate line 6, which is connected to at least one membrane filter 2a, 2b, 2c, as will be explained in more detail below.
- a corresponding valve in particular a special double seat valve 22, can be arranged between the discharge line 6a and the unfiltrate line 6.
- a line 23 also opens out via the valve, for example via valve 22, into the unfiltrate line 6, the line 23 being connectable to the supply line 19 via the line 35 and via a valve 35a and valve 24.
- the unfiltrate tank 3 can be connected to the lines 35 and 23.
- the unfiltrate line 6 there can be a pump 24a, via which the unfiltrate can be pumped in the direction of the membrane filter 2a, 2b, 2c.
- a device for measuring the turbidity 18 or a proportional value, such as, for example, the viscosity or viscoelasticity, conductivity or density, can be arranged in the unfiltrate line 6. The measured values are proportional to the turbidity and particle load.
- a cooler 26 can optionally also be provided in the unfiltrate line 6.
- the unfiltrate line 6 opens here via a valve, for example a double seat valve, into the unfiltrate inlet 8a, 8b, 8c of the respective membrane filter unit 2a, 2b, 2c.
- a valve for example a double seat valve
- three membrane filters 2a, 2b, 2c are shown, each in the form of a membrane filter unit which comprises several individual filter modules 40, as shown in FIGS. 1a, 1b.
- the membrane filter units 2a, 2b, 2c are, for example, connected in parallel.
- each membrane filter unit 2a, 2b, 2c has a filtrate outlet 9a, 9b, 9c which open into a common filtrate line 90 via corresponding valves, for example double seat valves.
- the respective concentrate outlets 10a, 10b, 10c of the respective membrane filter unit 2a, 2b, 2c are connected to a concentrate collecting line 11 via corresponding valves 25a, 25b, 25c, here double seat valves.
- the concentrate outlets 10a, 10b, 10c of the respective membrane filter 2a, 2b, 2c are connected in series, for example, with the lines from the respective concentrate outlets 10a, 10b, 10c to the common concentrate collecting line 11 via the corresponding valves 25a, 25b, 25c from each other can be separated.
- the concentrate drain to be selected from certain membrane filter units 2a, 2b, 2c, for example a membrane filter unit can also be bridged.
- the membrane filter units 2a, 2b, 2c can be interconnected in such a way that their filtration cycles can begin and end independently of one another. Concentrate can be circulated back to the unfiltrate buffer tank 3 via the concentrate collecting line 11.
- Each membrane filter unit 2a, 2b, 2c has a return line 89 via which the concentrate from the modules 40 is returned as unfiltrate to the modules for filtration and can also be returned via a concentrate drain 10 of a concentrate collecting line 11 to transfer the concentrate to the unfiltrate buffer tank 3 to lead back as can be seen in Fig. 1a and 1b.
- a control valve 70 and a flow meter 71 are provided for regulating the derived volume flow of the concentrate or, as will be explained below, for dosing sediment that is backwards into the return line via the concentrate outlet 10 89 is added in order to be filtered, as will be explained in more detail below.
- the lower outlet 4 of the unfiltrate buffer tank 3 is connected to the unfiltrate line 6 via a metering line 12, 16.
- the dosing device 7 can be located, which here has a dosing pump 7a with a flow meter 7b, for example, in such a way that the volume flow of the unfiltrate or sediment from the lower outlet 4 of the unfiltrate buffer tank 3 can be regulated.
- it is only essential that the volume flow of the sediment that is withdrawn via the lower outlet 4 can be adjusted or regulated via the metering device 7, in particular via a control device (not shown) as a function of a measured value.
- the metered amount / time can be regulated as a function of the measured value of the device 18, that is to say, for example, the turbidity.
- the metering line 12, 16 opens at the metering point D into the unfiltrate line 6, here via the valve 27, in particular the double seat valve.
- the valve 27, for example, sediment can also be discharged into a gully via a gully valve or, for example, via the valve 29 into a line 13 which, via a valve, in particular a double seat valve 30, via the line 14 to the concentrate outlet 10 of the respective membrane filter unit 2a , 2b, 2c leads.
- the line 13 is also connected to the line 12, that is to say the metering line, via a valve 31.
- sediment can also be fed to the concentrate collecting line 11.
- sediment can alternatively or in addition to the dosing at dosing point D also be introduced into the concentrate drain 10a, 10b, 10c of the membrane filter units 2a, 2b, 2c into the membrane filter and added there, in particular via the concentrate control valve 70, which is shown here takes over the function of the metering device, as shown in Figure 1 and 1a.
- a CIP return is designated by 32.
- FIG. 3 shows a further embodiment according to the present invention wherein the lower drain 4 has a tank outlet nozzle, ie drain pipe 4b, which protrudes into the unfiltrate tank 3 from below, so that sediment can drain through the drain pipe 4b and / or through an area 4c between the Drain pipe 4b and the tank wall of the unfiltrate buffer tank 3, whereby it is preferably possible to set via valves 60a, 60b in the line sections 12a and 12b, in particular control valves, whether sediment flows through the drain pipe 4b and / or the area 4c between the drain pipe 4b and the tank wall of the unfilt ratbuffertank 3 is to be diverted.
- the line sections 12a and 12b open into the common line 12.
- the valve arrangement 80 in particular the double seat valve 80, is connected to the area 4c and to the line 23 and line 35.
- the sediment is preferably withdrawn via the drain pipe 4b when the sediment is added via the dosing point D (because it has a lower particle load than the sediment which is withdrawn in area 4c), while the sediment is preferably withdrawn via area 4c when the sediment is fed directly to the filter module, that is to say via the concentrate drain 10.
- the area 4c between the drain pipe 4b and the tank wall of the unfiltrate buffer tank 3 can also be diverted separately, for example via the line 13 up to the concentrate drain 10, to the membrane filter units 2a, 2b, 2c, although not shown.
- Beer is introduced as unfiltrate from a storage cellar 21 via the feed line 19 for filling the unfiltrate buffer tank 3, preferably first via the outlet 4, the valves 35a and 80 being switched in such a way that the beer flows into the line 35 into the unfiltrate buffer tank 3.
- the valve arrangement 24 and 35a is switched in such a way that the beer does not flow into the line 35, which is connected to the line 23.
- the unfiltrate buffer tank 3 is only filled via the inlet 20.
- the unfiltrate can be fed to the Unfiltratlei device 6 via the upper, here lateral drain 5 via the line 6a when the valve arrangement 22 is opened accordingly, and for example via the pump 24a in the direction of the membrane filter 2a, 2b, 2c. be pumped.
- the turbidity or a correspondingly proportional value can be measured via the optional device 18 and passed on to a controller, not shown.
- the unfiltrate can also be cooled via the cooler 26.
- the unfiltrate enters the membrane filter or membrane filter unit 2a, 2b, 2c via the respective unfiltrate inlet 8a, 8b, 8c, which is currently in a filtration cycle, with filtrate being passed through the corresponding filtrate outlet 9 into a common Filtratlei device 90.
- Concentrate can be fed into the common concentrate collecting line 11 via the concentrate drain 10 with the appropriate switching of the valve 25 of the respective membrane filter unit 2a, 2b, 2c and in the circuit K, for example, via the line 19 when the valve arrangement 92 and 24, in particular the double seat valves, is opened accordingly 92 and 24 and the closed valve arrangement 35a can be returned to the unfiltrate buffer tank 3 via the inlet 20.
- sediment settles in the lower area of the unfiltrate buffer tank 3.
- a metering device 7 or here 7a, 7b sets the volume flow of the withdrawn sediment as a function of the turbidity 18 measured by the device 18 or a proportional value.
- the volume flow is preferably regulated as a function of the corresponding measured value. This means that if the turbidity measured after the dosing point D is still relatively low, a higher amount of sediment can be added than if the turbidity has a correspondingly higher value.
- the turbidity is measured according to the dose point D. It can thus be effectively prevented that there is a high concentration in the lower region of the unfiltrate buffer tank 3.
- the particle load in the unfiltrate to be filtered can be kept constant over many filtration cycles.
- Regulating the volume flow of the sediment as a function of the turbidity 18 is only one possible exemplary embodiment.
- the metered amount / time of the metered sediment can be regulated as a function of the flow, in particular the unfiltrate (before or after the metering point D) and / or the sediment (in the metering line).
- transmembrane pressure is measured on at least one module 40 and sent to the controller.
- the particle load i.e. the solids per volume of the liquid
- the membrane filters can have a defined particle load regardless of the start of the filtration, which can be kept essentially constant, which has a very positive effect on the filter process.
- An abruptly large particle load can be prevented, since the particle load in the lower area can be kept low. In this way, a sudden, strong increase in diaphragm pressure (transmembrane pressure) can be prevented.
- unfiltrate i.e. beer from the storage tank 21
- unfiltrate i.e. beer from the storage tank 21
- the unfiltrate is preferably fed in via metering point D.
- unfiltrate is via the return line 89 the z. B. in series or parallel scarf ended modules 40 for filtration.
- no sediment is metered in via the concentrate outlet 10.
- the unfiltrate is pushed out of the membrane filter unit with water, in particular degassed water, as shown for example in FIG. 1b.
- water, in particular ent gassed water for example via the connection 82, with appropriately opened valves in the membrane filter or membrane filter unit, which z. B requires intermediate cleaning due to reaching the transmembrane pressure limit value.
- water in particular degassed water
- the valve arrangement 22 is in particular switched in such a way that no unfiltrate is supplied via the line 6a and the upper outlet 5. Sediment is drawn off via the lower outlet 4 and, as also described above, can be metered into the line 6 via the metering point D.
- the volume flow of the sediment can also be regulated via the regulation described above as a function of the measured turbidity or the correspondingly proportional value.
- the setpoint can be set accordingly here.
- the added amount / time of sediment in particular the volume flow, can be regulated independently of the control parameters previously described in connection with the regulation via the metering point D. It is regulated, for example, according to the measured transmembrane pressure on at least one module 40 of the corresponding membrane filter unit 2a, 2b, 2c. However, it is also possible for the metered amount / time to be empirically determined and set in advance.
- a connection 81 can also be provided in the line 13, which leads from the lower run 4 to the concentrate run 10 of the respective at least one membrane filter 2a, 2b, 2c, which in particular is connected to a tank or other system for yeast beer or jelly beer connected to recovery.
- yeast beer can be metered in via the concentrate outlet 10, with the concentrate control valve 70 taking over the metering function.
- the operating mode shown in FIG. 1b takes place not only at the end of a filtration cycle. While at least one of several membrane filter units 2a, 2b, 2c is in a filtration cycle and is filtering unfiltrate from the unfiltrate tank 3, at least one other membrane filter unit 2a, 2b, 2c can be operated in such a way that water, in particular degassed water, e.g.
- Connection 82 is passed through this membrane filter unit 2a, 2b, 2c and sediment is introduced via, for example, line 13 from the lower outlet 4 of the unfiltrate buffer tank 3 and / or yeast beer or gelager beer via a connection 81 into a concentrate outlet 10 of the corresponding membrane filter unit 2a, 2b, 2c and is introduced into the water stream and filtered.
- This alternative operating mode can therefore not only be carried out at the end of a filtration cycle, but can also be carried out as a continuous filtration process for several hours (e.g. 1 to 6 hours, i.e. the duration of a filtration cycle) for at least one selected membrane filter unit.
- the membrane filter unit 2a can be operated in accordance with the alternative operating mode, while, for example, in the case of the membrane filter units 2b and 2c, the filtration process runs as shown in FIG. 1a.
- Figure 2 shows the yeast cell count (10 6 yeast cells / ml) of the unfiltrate that is fed to the at least one membrane filter 2a, 2b, 2c, depending on the filtration time (hours), ie operating time of the membrane filter without cleaning time.
- the hatched values show the yeast cell number as a function of time according to the present invention.
- the yeast cell count can be kept essentially constant over time, i.e. during several successive filtration cycles, since the yeast load can be controlled in that sediment from the lower area of the unfiltered buffer tank 3 can be metered into the unfiltrate in a targeted manner.
- a filtration cycle takes about 6 hours, for example.
- the filtration cycle begins either with the expulsion of water with beer or, if the filter is under a gas atmosphere, with the filling with beer and usually ends when the maximum or a certain transmembrane pressure is reached or when no more beer is filtered who should and the pushing out of the beer.
- the dotted values show, for example, the course of the yeast cell number according to the prior art.
- the unfiltrate slowly concentrates here.
- the bare values also show a method according to the state of the art in which the unfiltrate buffer tank 3 is emptied from below after a first filtration cycle, which likewise leads to a significant increase in the number of yeast cells.
- the first low value of, for example, 2 to 5x10 6 yeast cells per ml at the beginning of the filtration cycle results from the fact that unfiltrate is first removed from the upper outlet and there is a control delay until the yeast cell count, ie solid load, by metering in sediment, here for example to 15x10 6 yeast cells per ml.
- the device 1 can be operated over a time interval t before the tank, for example, is emptied and the device is, for example, cleaned, for example the membrane filter unit (s) is or are backwashed, during which Time interval the particle load, in particular yeast concentration, is set.
- the present invention thus enables a filtration with a regulated addition of the sediment from the unfiltrate buffer tank depending on the membrane filter status of a respective membrane filter (e.g. filtration, end of the filtration cycle, filtration of yeast beer and yeast beer).
- a respective membrane filter e.g. filtration, end of the filtration cycle, filtration of yeast beer and yeast beer.
- the pumps used can be frequency-controlled.
- This unfiltrate buffer tank which functions as a sedimentation tank with a dosing device for sediment, can also be used, for example, for precoat filtration for beer. It can also be useful for precoat filtration if the filter inlet has a defined particle load. With precoat filtration, no concentrate is returned, but sedimentation takes place here as a result of the continuous feeding of unfiltrate from the storage cellar with different particle loads (e.g. by changing the storage tank) into the unfiltrate buffer tank, especially if filter aids or stabilizers have been used beforehand.
- FIG. 4 Another possibility of increasing the yield in the production of beer is shown in FIG. 4.
- a mixed phase consisting of water and beer results.
- Any mixed phases produced can be collected in a collecting tank 55 (a so-called reworktank), especially when it comes to beers which have been produced using the high gravity method (a wort with a high original wort (extract content) is brewed in the brewhouse).
- a collecting tank 55 a so-called reworktank
- beer can also be used for backwashing.
- Concentrate that, for example, should no longer be circulated at the end of the filtration can also be fed to the collecting tank 55. This can also be necessary in particular if the concentrate collecting line 11 is not used or not available and the concentrate is merely returned to the membrane filter 2 as unfiltrate to the modules 40 for filtration via a return line 89.
- these discharges are either thrown away in the sewage system (gully) or they are collected in pre / post tanks or in residual beer tanks and recycled in some other way. For the filtration process, this represents a loss of unfiltrate every time. This is particularly true when it comes to beers that have a high solids load and therefore require frequent expulsions.
- the beer losses can be reduced to a minimum.
- Mixed phases can, for example, be conducted from the filtrate line 90 to the line 42 and thus to the collecting tank 55 via a connecting line 41a. Even if not shown in FIG. 4, the line 41a can also connect the filtrate outlet 90 to the line 42. Via a connecting line 41b, concentrate can, for example, be conducted from the return line 89 to the line 42 and thus to the collecting tank 55. Via a connecting line 41c, concentrate can, for example, be led from the concentrate collecting line 11 to the line 42 and thus to the collecting tank 55.
- the mixed phase that occurs during the backwashing of the membrane filter 2a, 2b, 2c can be fed into the tank via the line 89 and line 41b 55 are directed.
- a mixed phase and / or concentrate from another production step of the beer production can be conducted through the line 42 and thus to the collecting tank 55 via a connecting line 41 d or connection 41 d.
- mixed phases and / or concentrate can also be fed via appropriate lines into the unfiltrate buffer tank, which then serves as a collection tank.
- the collecting tank 55 is preferably a separate collecting tank which is present in addition to the unfiltrate buffer tank 3. The advantage of a separate collection tank is that the ongoing filtration is initially not influenced, and the collected amount can then be returned in a targeted manner. This is particularly advantageous if, as already mentioned above, a targeted dosage of the mixed phase resulting from the backwashing (i.e.
- the collection tank 55 into the unfiltrate flow, i.e., for example, into the unfiltrate line 6, 8, 10 or the return line 89 is to take place.
- This enables, for example, a certain amount, for example only 510% proportional dosage of the collected amount.
- this collected amount has a high concentration of solids, the renewed stress on the membrane can be controlled in a targeted manner. Ie with the help of the collected amount, the time, amount, concentration and duration of the return can be influenced in a targeted manner.
- the solids load of the contents of the unfiltrate buffer tank 3 can be controlled in a targeted manner at any point in time.
- the lower region of the collecting tank 55 is preferably designed in such a way that it tapers conically downwards, for example the opening angle of the cone is between 60 and 70 °, so that the collecting tank 55 also serves as a sedimentation tank.
- the conical bottom allows the sediment to be drawn off particularly easily. In this case, the removal of the sediment is primarily used to separate the no longer usable solids which, for example, are passed into the gully.
- the collecting tank 55 can have a lower inlet 44 and an inlet 43 located above it, preferably above the conical section of the collecting tank 55. Even if not shown, the collecting tank 55 can also have only one inlet, or several inlets arranged differently in height. The inlet or the inlets can also be used as drain (s).
- the inlet 44 close to the bottom can also be used as an outlet. Via the outlets 44, 45, 46, 47, the medium is fed to the line 48 and thus to a further use.
- the collecting tank 55 can also have only one drain or only two drains or more than four drains at different heights.
- the feed line 42 to the collecting tank 55 there can be a separator (not shown) which separates the liquid from the solids contained therein.
- the concentrate is removed from the filtration process and fed to a gully or other recycling (e.g. used yeast recycling, animal feed).
- the liquid phase is fed back into the process via the collecting tank 55.
- the optional separator 51 can, however, also be located in the line 48 which leads away from the collecting tank 55; the separator is preferably located in the line 48 in such a way that that in a circulation line with which the contents of the collecting tank 55 can be circulated via the outlets / inlets 43, 44, 45, 46, 47. If the collecting tank 55 is the unfiltrate buffer tank 3, then an optional separator 51 can also be arranged in the concentrate collecting line 11.
- a separator another suitable separation device can also be present, such as, for example, a decanter or similar suitable systems.
- the contents of the collection tank 55 can be fed to the membrane filter 2a, 2b, 2c via appropriate lines at certain times of the filtration process, for example if a certain turbidity value or a proportional value in the unfiltrate that is sent to the membrane filter is fed to the membrane filter 2a , 2b, 2c can be dosed as long as the content from the collecting tank 55 until a certain / maximum turbidity value or a proportional value in the unfiltrate to the membrane filter 2a, 2b, 2c is reached. It is also possible to continuously supply the contents of the collection tank 55 to the filtration process.
- 5% to 10% content from the collecting tank 55 can be metered into the unfiltrate (5% means that 95 hl unfiltrate is added to 5 hl tank content from the collecting tank).
- the contents of the collection tank 55 are fed to the membrane filter 2 towards the end of the filtration process. It is also conceivable that the contents of the collecting tank 55 are fed to the wort kettle or some other utilization (for example a waste yeast tank, a leftover beer tank, a separator, sedicanter or decanter.
- the preferred use of the contents of the collecting tank 55 is the supply during or against End of the filtration process to the membrane filter 2a, 2b, 2c.
- the addition can take place in any line that leads to the membrane filter 2 or, if the collecting tank 55 is a separate tank, it can also be fed to the unfiltrate buffer tank 3.
- the medium Via the line 48 and 49 and the connecting line 50a, medium can be fed from the collecting tank 55 via the inlet 20 to the unfiltrate buffer tank 3. Even if not shown, the medium can also be fed to the unfiltered buffer tank 3 via the lower outlet 4.
- the lines 48 and 49 as well as the connecting line 50b medium from the collecting tank 55 of the metering line 12, or via the connecting line iteration 50c of the line 13 are fed.
- the medium can be fed from the collecting tank 55 via the lines 48 and 49 to the membrane filter 2a, 2b, 2c via one of the lines 14, 23, 35 or unfiltrate line 6 (before or after the dosing point D). Even if not shown in FIG. 4, the medium can be supplied with the metering device 7 or 70. Even if not shown in FIG.
- the sediment can be fed from the unfiltrate buffer tank 3, for example via the connecting line 50b and the lines 49 and 48 via the inlet 43, to the collection tank 55, so that the unfiltrate puff fertank 3 cleaned and / or with unfiltrate which differs from the unfiltrate in the unfiltrate buffer tank 3 (for example unfiltrate of a different type of beer can be filled).
- the unfiltrate buffer tank 3 has been refilled (for example before a filtration cycle or a change of beer type) with an unfiltrate from the storage cellar 21 with a low yeast cell count, the solids quantity / yeast cell count, i.e.
- the load on the membrane 40 is to be started later should be successively increased through increased solids load.
- the membranes 40 of the membrane filter 2a, 2b, 2c are not exposed to too high a particle load and are thereby protected. Since the discharges and concentrates are collected and reused, the membrane filters 2a, 2b, 2c can be rinsed at an earlier point in time, when the particle load is not that high, from an economic point of view. Thus, although the membrane filter 2a, 2b, 2c is backwashed more frequently, for example with water, the membranes 40 are protected by the lower particle load.
- the inlets and outlets can also be located inside the tank at different height levels of the collecting tank 55. It can be a concentrically arranged pipe inserted from below into the collecting tank 55, with a first central opening arranged at the lower end of the collecting tank 55. Furthermore, the second inflow or outflow can comprise a second pipe and the third inflow or outflow can comprise a third pipe, the second and third pipes preferably extending at least in sections within the collecting tank 55. The second and third tubes can be arranged one inside the other, preferably concentrically.
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- Chemical Kinetics & Catalysis (AREA)
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Abstract
Description
Claims
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DE102020110313 | 2020-04-15 | ||
DE102021103430.2A DE102021103430A1 (de) | 2020-04-15 | 2021-02-15 | Vorrichtung und Verfahren zum Filtrieren von Bier |
PCT/EP2021/056453 WO2021209203A1 (de) | 2020-04-15 | 2021-03-15 | Vorrichtung und verfahren zum filtrieren von bier |
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EP4135882A1 true EP4135882A1 (de) | 2023-02-22 |
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EP21712487.4A Withdrawn EP4135882A1 (de) | 2020-04-15 | 2021-03-15 | Vorrichtung und verfahren zum filtrieren von bier |
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EP (1) | EP4135882A1 (de) |
DE (1) | DE102021103430A1 (de) |
WO (1) | WO2021209203A1 (de) |
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DE3509892C2 (de) * | 1985-03-19 | 1994-04-21 | Westfalia Separator Ag | Verfahren zum Nachklären und Stabilisieren von Polyphenole und/oder Eiweißstoffe enthaltenden Flüssigkeiten und Getränken, insbesondere von Bier |
DE3533306A1 (de) * | 1985-09-18 | 1987-03-26 | Adolf Reiter | Verfahren zur auftrennung und klarfiltration von suspensionen und vorrichtung zu seiner durchfuehrung |
DE3813924A1 (de) * | 1988-04-25 | 1989-11-02 | Mylius Ulrich Von | Verfahren zur auftrennung und klarfiltration von bier mit hefe und trubstoffen |
ATE115181T1 (de) * | 1988-07-15 | 1994-12-15 | Filtrox Werk Ag | Filtrationsverfahren, verwendung von stabilisierungsmitteln, anlage für ein filtrationsverfahren und verfahren zum betreiben der anlage. |
AU2003209917A1 (en) * | 2002-04-03 | 2003-10-13 | Bucher-Guyer Ag | Cross-flow filtration system and operation method therefor |
EP1743689A1 (de) * | 2005-07-13 | 2007-01-17 | KRONES Aktiengesellschaft | Crossflow-Membranfilteranlage sowie Verfahren |
DE102016217500A1 (de) * | 2016-09-14 | 2018-03-15 | Gea Brewery Systems Gmbh | Vorrichtung und Verfahren zum Mischen eines Inhalts eines Tanks |
-
2021
- 2021-02-15 DE DE102021103430.2A patent/DE102021103430A1/de not_active Withdrawn
- 2021-03-15 WO PCT/EP2021/056453 patent/WO2021209203A1/de unknown
- 2021-03-15 EP EP21712487.4A patent/EP4135882A1/de not_active Withdrawn
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