Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
  • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
  • B03D1/00—Flotation
  • B03D1/14—Flotation machines
  • B03D1/24—Pneumatic
  • B03D1/247—Mixing gas and slurry in a device separate from the flotation tank, i.e. reactor-separator type
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
  • B01F23/20—Mixing gases with liquids
  • B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
  • B01F23/232—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles
  • B01F23/2323—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using flow-mixing means for introducing the gases, e.g. baffles by circulating the flow in guiding constructions or conduits
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
  • B01F25/30—Injector mixers
  • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
  • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
  • B01F25/3123—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof with two or more Venturi elements
  • B01F25/31232—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof with two or more Venturi elements used simultaneously
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
  • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
  • B01F25/30—Injector mixers
  • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
  • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
  • B01F25/3124—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof characterised by the place of introduction of the main flow
  • B01F25/31243—Eductor or eductor-type venturi, i.e. the main flow being injected through the venturi with high speed in the form of a jet
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
  • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
  • B03D1/00—Flotation
  • B03D1/14—Flotation machines
  • B03D1/24—Pneumatic
  • B03D1/242—Nozzles for injecting gas into the flotation tank
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
  • D21B1/00—Fibrous raw materials or their mechanical treatment
  • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
  • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
  • D21B1/30—Defibrating by other means
  • D21B1/32—Defibrating by other means of waste paper
  • D21B1/325—Defibrating by other means of waste paper de-inking devices
  • D21B1/327—Defibrating by other means of waste paper de-inking devices using flotation devices
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
  • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
  • B03D1/00—Flotation
  • B03D1/14—Flotation machines
  • B03D1/1443—Feed or discharge mechanisms for flotation tanks
  • B03D1/1456—Feed mechanisms for the slurry
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W30/00—Technologies for solid waste management
  • Y02W30/50—Reuse, recycling or recovery technologies
  • Y02W30/64—Paper recycling

Definitions

• the invention relates to a method and a device for the purification of contaminated solid-liquid mixtures and the use of the method and the device.
• the invention relates to a method and a device for removing contaminants and impurities from an aqueous paper fiber suspension by flotation.
• Flotation processes are known for the preparation of a suspension obtained from printed wastepaper in which the ink particles are already detached from the fibers.
• the fact is used that the pulp remains in the fiber suspension due to its rather hydrophilic character, whereas the unwanted Störstoffteilchen are hydrophobic and therefore enter together with the air bubbles in the foam.
• This is referred to as selective flotation.
• the impurities discharged by the selective flotation are, in addition to the printing ink, in particular adhesives, fine plastic particles and, possibly, also resins.
• waste paper processing waste paper in a pulper will be added and mixed with return water to such a pumpable suspension to preserver ⁇ th.
• first sorting step large, non whippable and not pumpable impurities and impurities, such as cords and solid films removed.
• the resulting pulp slurry then undergoes a series of mechanical sorting steps, including baskets, where other smaller contaminants and Ver ⁇ impurities are removed.
• the pulp suspension undergoes a re-sorting, often a Deinkingstrom or even finer baskets.
• deinking is generally used not only for the removal of ink particles (ink), but also in general for the selective flotation of impurities from pulp suspensions In a deinking plant, the pulp suspension is enriched with air.
• water is first enriched with air.
• This enrichment of the water with air requires a considerable, usually electrical energy.
• a pump brings a volume of water to about 8 bar water pressure and conveys it into a pressure vessel. In this is introduced with about 10 bar of compressed air, wherein the volume of air corresponds to about 20% of the volume of water (the ratio of air to water here is about 1 to 5).
• mixing elements operating according to the Venturi principle are also known.
• DE 693 29 061 T2 discloses an apparatus for efficiently dispersing mixing gas bubbles with a liquid and effectively dissolving a gas in a liquid.
• the apparatus comprises a venturi-type mixing element having a throttled portion formed by a portion of a fluid flow passage whose cross-sectional area is reduced, one contiguous with the throttled portion, by gradually widening a portion of the fluid flow passage to the downstream side Section, ei ⁇ nem gas inlet, which is arranged in a region of the widened portion slightly downstream of the throttled portion and a downstream of the extended portion arranged mixing section with a downstream end.
• the apparatus further comprises a fluid tube with egg ⁇ nem proximal end which is connected to the downstream end of the mixing section of the mixing element, and a distal end which is connected to a nozzle portion having a plurality of nozzle holes, where ⁇ at immediately before A second throttled section is attached to the nozzle section. is arranged, which is formed by a reduced area in the cross-sectional area of the fluid idströmungskanales.
• the air-enriched water i. the air suspension is then combined with the fibrogen suspension.
• Chemical auxiliaries are known in order to dissolve or mask the contaminants and impurities from the paper fibers.
• the known chemical adjuvants are not sufficiently efficient and not economical.
• Another problem of known flotation methods and devices is that not only impurities and impurities are floated, but also undesirably a paper fiber content of more than 2% is discharged with.
• a deinking system consists of several deinking cells connected in series.
• the deposited contaminants and impurities are typically fed into a secondary cell to recover lost paper fibers. Nevertheless, the fiber loss in a deinking plant is greater than 2%.
• the contaminants and contaminants that are removed in a deinking plant are for the most part only ink particles.
• Other undesirable particles, such as stickies, metals, plastics, resins and organic substances, are usually not discharged in a deinking plant.
• the fabric density range in a deinking plant is normally between 1% and 1, 5%.
• the pH is about 7. The state of the art regarding flotation processes for pulp suspensions is already very advanced.
• So 10 2008 056 040 A1 discloses the DE to a process for the removal of sturgeon ⁇ materials with the aid of gas bubbles from an aqueous pulp suspension, wherein the flow of the fiber suspension fed in at least one mixing device, at least one stream of gas and gas bubbles are formed, thereby interfering ⁇ materials be collected from the pulp suspension in a flotation foam and removed with this.
• at least one internal flow of gas alternatively also to the outside of the stream of the fiber suspension, an external flow of gas is fed into the interior of the stream of fiber suspension.
• the DE 10 2008 064 271 A1 discloses a process for removing Feststof ⁇ fen with the aid of gas bubbles from an aqueous pulp suspension, in particular waste paper suspension, in which the fiber suspension fed in at least one mixing device gas and gas bubbles are formed. Thereafter, the fumigated suspension from the mixing device via an adjustable flow resistance, in particular by a throttle, passed into a flotation tank by the deposition of solids by flotation. The method allows the adjustment of the air content of the gassed suspension.
• DE 10 201 1 009 792 A1 discloses a process for the purification of contaminated fibers in which, in a first process step, the fibers to be cleaned are mixed with liquid and in a second process step as solid-liquid mixture flowing with an air-liquid mixture be merged, wherein the confluence of the air-liquid mixture with the solid-liquid mixture with greatly different flow rates and this process is performed so that at the same time a significant dilution of the solid-liquid mixture takes place and the dissolved impurity particles settle on the air bubbles from the air-liquid mixture, and in a third process step for the separation of fiber content, polluted foam from the bubbles and liquid the resulting mixture in the second step is subjected to a fractionation in which the a Foam arising on the surface, contaminated with impurities, is separated from the cleaned fibers.
• the object of the invention is therefore to provide an apparatus and a method for sheep ⁇ fen, which overcome the aforementioned disadvantages of the prior art.
• a first aspect of the invention relates to a device for purifying impure solid-liquid mixtures, comprising at least a first pipeline for the supply of a liquid, preferably water, at least a second pipeline for the supply of a solid-liquid mixture, preferably one Pulp suspension, particularly preferably a paper fiber suspension, at least a third pipeline which connects the first and the second pipeline and comprises at least one mixing element which operates according to the Venturi principle, hereinafter referred to as Venturi mixing element, wherein the Venturi mixing element element has two oppositely directed cones, each with its small passage opening in a cavity forming a chamber, wherein the region of the junction in the cavity forming chamber is formed such that the respective small passage opening of the cones ent in a non-conical line section speaking the cross-sectional area of the small passage openings is continued, these non-conical line sections open into the chamber between the cones, the large passage ⁇ opening of the first cone via the third pipe is connected to the first pipe and the large passage opening of the second cone on the dr
• the venturi mixing element By supplying the liquid to the venturi mixing element and conducting the gas, preferably air to the venturi mixing element, in the venturi mixing element an enrichment of the liquid takes place with gas bubbles of different diameters, at the same time increasing the flow velocity of the liquid.
• the liquid enriched with gas bubbles of different diameter is subsequently introduced into the contaminated solid-liquid mixture, the gas-bubble-enriched liquid having a higher flow velocity than the solid-liquid mixture.
• Cavity between the cones opens. This cavity forms a significant Enlargement of the passage cross-section for the liquid.
• Liquid supplied to the Venturi mixing element via the third pipeline is accelerated in its flow velocity by the first cone and, after it has flowed through the non-conical line section adjoining the small passage opening of the cone, enters the cavity as a liquid jet with increased flow velocity. In this case, a negative pressure is generated, as a result, gas is sucked through the fourth pipe into the chamber.
• the liquid which flows into the cavity at an increased rate absorbs or tears this gas sucked into the cavity.
• the liquid jet After the cavity, i. after the sudden increase in the passage cross section for the liquid, which passes this cavity as a quasi liquid jet, the liquid jet enters the non-conical line section of the small passage opening of the second cone.
• This non-conical line section has a larger diameter than the liquid jet. It is adjoined by the second cone, with a further enlargement of the passage cross section for the liquid.
• this non-conical line section and subsequently the second cone of the Venturi mixing element there is a very intensive mixing of the liquid with the gas taken up or entrained, the gas being distributed as small bubbles in the liquid.
• the liquid When exiting the Venturi mixing element in the third pipeline, the liquid is strongly enriched with different sized gas bubbles.
• This mixture of different sized gas bubbles in the liquid is important to effect attachment to a wide range of different sized contaminants and contaminants to be separated.
• the amount and the size distribution of the gas bubbles in the liquid depends in addition to the flow rate of the liquid and the amount of gas sucked in a high degree on the structural design of the Venturi mixing element described in detail below.
• the diameter of the large passage opening of the first cone is between 10 and 20 mm and the diameter of the small passage opening of the first cone is between 14 and 16 mm, whereby of course the diameter of the small passage opening is always smaller than the diameter of the large one Through hole is.
• the diameter of the small passage opening of the second cone is between 12 and 20 mm and the diameter of the large passage opening of the second cone between 16 and 24 mm, wherein, of course, the diameter of the small passage opening is always smaller than the diameter of the large passage opening.
• the condition is that the diameter of the small through hole of the first cone is at least 2 mm smaller than that
• Diameter of the small passage opening of the second cone Diameter of the small passage opening of the second cone.
• the length of the non-conical line sections is between 20 and 80 mm.
• the distance between the two opposite junctions of the non-conical line sections in the cavity, so the width of the cavity is between 6 and 20 mm.
• the enriched gas bubbles under ⁇ different sizes and size distribution of liquid, a ratio of gas to liquid of Figure 1.
• the Ventun mixing element on a plurality of mutually oppositely directed cones, each with its small passage opening in a cavity forming chamber, wherein the region of the mouth is formed in the cavity such that the respective small Through hole of the cones is continued in a non-conical line section corresponding to the cross-sectional area of the small passage openings and this non-conical line section opens into said cavity between the cones.
• all the cones open into a common cavity, wherein, as already described, two oppositely directed cones are aligned axially to each other.
• the number of cones is between 2 and 25, preferably between 4 and 20.
• the amount of gas can vary widely in different systems, it is advantageous application-specific to adjust the amount of gas absorbed and bubble size by the number of arranged cones in the Venturi mixing element.
• a Venturi mixing element with up to 4 cone pairs can be used.
• a Venturi mixing element for a DN 80 line for example, up to 7 cone pairs are possible.
• a Venturi mixing element for a DN 120 line up to 9 cone pairs can be arranged.
• the Venturi mixing element is designed such that the gas bubble size can be adjusted application-specific. In this case, for example, the cross sections of the third and fourth pipeline can be changed in the Venturi mixing element.
• the cross sections of the small through holes of the cones and the lengths of the non-conical line sections, through which the small passage openings of the cones open into the cavity between the cones in the Venturi mixing element can be adapted to the application and affect the size and size distribution of the gas bubbles in the liquid ,
• the third pipe opens at an angle of 90 ° ⁇ 45 ° in the second pipe.
• the third pipeline opens into the second pipeline at an angle of 90 °.
• the second pipeline has a larger diameter than the third pipeline.
• the third pipe opens at an angle of 45 ° in the flow direction of the second pipe into the second pipe.
• the liquid in the first pipeline to a pressure of 2 to 4 bar. In a further embodiment of the invention, the liquid in the first pipeline has a flow velocity of 1 m / s to 5 m / s.
• the solid-liquid mixture in the second pipeline has a flow velocity of ⁇ 4 m / s.
• the liquid enriched with gas bubbles in the third pipeline after the Venturi mixing element has a flow rate of 5 to 40 m / s, preferably 5 to 25 m / s, preferably 9 to 25 m / s.
• the liquid is water, preferably clear water or white water.
• the device comprises one or more further pipelines, each with a Venturi mixing element, which are arranged in cascade and are connected downstream of the junction of the third pipeline into the second pipeline.
• the multiple introduction of an enriched with gas bubbles of different size liquid in the solid-liquid mixture better mixing of the gas bubbles in the solid-liquid mixture.
• this increases the cleaning effect, so that the use of multiple Venturi mixing elements and the multiple introduction of the gas bubbles enriched liquid in a solid-liquid mixture is advantageous.
• the confluence of the third pipeline into the second pipeline is fan-shaped.
• the solid-liquid mixture after introduction of the gas bubbles enriched liquid has a solids content of ⁇ 2% by weight.
• the device comprises control options.
• adjustable slides are arranged before and after the Venturi mixing element.
• a controllable slide is arranged in the fourth pipe. These gate valves can be operated electrically or manually. The aforementioned control options influence the number, size and size distribution of the gas bubbles in the fluid.
• a significant advantage of the device according to the invention, in particular the Venturi mixing element, is that the liquid is enriched with a mixture of gas bubbles of different sizes, without the need for energy-intensive compression of the gas.
• the gas bubbles in the liquid have a high kinetic energy, whereby the impact of the gas bubbles on fibers, which adhere contaminants or impurities, a detachment of the impurities or impurities from the fibers is effected.
• Another aspect of the invention relates to a process for purifying contaminated solid-liquid mixtures comprising the steps of:
• the solid-liquid mixture is a fiber suspension, preferably a paper fiber suspension.
• the liquid is enriched with gas bubbles of different size and size distribution such that the liquid enriched with gas bubbles has a ratio of gas to liquid of 1 to 4: 1, preferably 1: 1.
• the liquid in the first pipeline to a pressure of 2 to 4 bar.
• the liquid flows in the first pipeline at a flow rate of 1 m / s to 5 m / s.
• the solid-liquid mixture flows in the second pipeline at a flow rate of ⁇ 4 m / s.
• the liquid enriched with gas bubbles flows in the third pipeline after the Venturi mixing element at a flow rate of 5 to 40 m / s, preferably 5 to 25 m / s, preferably 9 to 25 m / s ,
• the supply of the gas bubbles enriched liquid in the solid-liquid mixture at an angle of 90 ° ⁇ 45 °.
• the supply of the gas bubbles enriched liquid in the solid-liquid mixture takes place at an angle of 90 °.
• the supply of the liquid enriched with gas bubbles in the solid-liquid mixture takes place in egg ⁇ nem angle of 45 ° in the flow direction of the solid-liquid mixture.
• the supply of gas-enriched liquid in the solid-liquid mixture takes place at an angle of 45 ° counter to the flow direction of the solid-liquid mixture.
• the liquid is water, preferably clear water or white water.
• a further aspect of the invention relates to the use of a device according to the invention and a method according to the invention for purifying contaminated solid-liquid mixtures, preferably contaminated fiber suspensions, particularly preferably contaminated paper fiber suspensions.
• the inflowing amount of the liquid before the Venturi mixing element is equal to the amount flowing out of the Venturi mixing element, the pressure after the Venturi mixing element being lower.
• the flow velocity is higher after the Venturi mixing element, since the liquid is enriched with gas bubbles.
• the amount of liquid and its flow rate may vary depending on the application. They have to be adapted to the respective application in order to achieve an optimal cleaning effect.
• Important for achieving a good cleaning effect is a higher flow velocity of the gas bubbles enriched liquid than the flow velocity of the solid-liquid mixture.
• Figure 1 a schematic representation of an apparatus for the purification of contaminated solid-liquid mixtures, in
• Figure 2 a schematic sectional view of a Venturi mixing element
• Figure 3a a schematic representation of the arrangement of the small through holes of the cones in a side wall of the cavity between the cones for a Venturi mixing element with 4 Konenschreiben, in
• FIG. 3b shows a schematic representation of the arrangement of the small passage openings of the cones in a side wall of the cavity between the cones for a venturi mixing element with 7 cone pairs, in FIG. 3b
• Figure 3c is a schematic representation of the arrangement of the small passage openings of the cones in a side wall of the cavity between the cones for a Venturi mixing element with 19 pairs of cones
• Figure 4a a schematic representation of an embodiment of the device for
• FIG. 4b shows a schematic illustration of a further embodiment of the device for cleaning contaminated solid-liquid mixtures
• FIG. 4c shows a schematic representation of a further embodiment of the device for purifying contaminated solid-liquid mixtures
• 5a shows a schematic cross-sectional view perpendicular to the flow direction of the junction of the third pipeline in the second pipeline, in
• Figure 5b a schematic cross-sectional view of the junction of the third
• FIG. 5 c another schematic cross-sectional view of an alternative
• an apparatus 1 is shown schematically in FIG. 1 with a first pipeline 2 for supplying a liquid, this being clarified or white water, hereinafter referred to simply as water.
• the water in the first pipeline 2 has a flow velocity of 1 m / s to 5 m / s and a pressure of 2 to 4 bar.
• the device 1 comprises a second pipe 3 for supplying a solid-liquid mixture with a flow velocity of ⁇ 4 m / s, which is a paper fiber suspension.
• the second pipe 3 is followed by an unillustrated fractionator.
• the pulp suspension contains contaminants in the form of impurities and impurities (ink particles, stickies, tiny plastic particles, etc.).
• a third pipeline 4 which comprises a venturi mixing element 5.
• a fourth pipe 6 leads to the passage of a gas, in the example ⁇ described example of air.
• the water is with gas bubbles of different size angerei ⁇ chert, thereby greatly accelerated.
• the water enriched with gas bubbles at a flow rate of about 9 m / s to 25 m / s.
• the gas bubbles enriched water contains a large number of gas bubbles of different sizes. This different size of the gas bubbles is important in order to achieve an attachment to a wide range of differently sized to be separated impurities and impurities. An effective separation of different impurities and impurities requires an adjustment of the number and size distribution of the gas bubbles.
• the number and size distribution of the gas bubbles in the water, in addition to the flow rate of the liquid and the amount of gas sucked in, depends to a great extent on the structural design of the Venturi mixing element 5.
• FIG. 2 schematically shows a sectional view of the Venturi mixing element 5.
• the Venturi mixing element 5 has a first cone 7, which leads to a tapering of the cross section.
• the third pipe 4 is connected, with that part which is connected to the first pipe 2.
• the venturi mixing element has a first non-tapered line section 8 which adjoins the small through hole 12 of the first cone 7 and Wesentli ⁇ chen the same cross-sectional area, namely that of the small through hole 12 of the first cone 7, comprising.
• the first non-conical line section 8 opens into a cavity 9 forming a chamber to this chamber 9, the fourth pipe 6 is connected.
• a second non-conical line section 10 is arranged, to which a second cone 1 1 with its small passage opening 13 connects.
• the third pipe 4 is connected sen, with that part which is connected to the second pipe 3.
• the chamber 9 forms a significant increase in the cross-sectional area.
• the Venturi mixing element 5 water is supplied.
• the water is accelerated by the first cone 7 in its flow velocity and enters as a liquid jet with increased flow velocity into the cavity of the chamber 9 a.
• a negative pressure is generated, as a result of which the gas flowing in at increased speed into the cavity of the chamber 9 absorbs gas or travels with it, which is sucked into the cavity via the fourth pipeline.
• the water jet with the absorbed or entrained gas enters the second non-conical line section 10 of the small passage opening 13 of the second Cone 1 1 on.
• This line section 10 is continued in the second cone 1 1, wherein a further enlargement of the cross-sectional area for the water takes place.
• this line section 10 and in the subsequent second cone 1 1 of the Venturi mixing element 5 is a very intensive mixing of the water with the absorbed or entrained gas, wherein the gas is distributed as bubbles of different sizes in the water.
• the water is strongly enriched with gas in the form of different sized bubbles. These gas bubbles of different sizes are important in order to achieve an attachment to a wide range of different sized impurities and impurities to be separated.
• the third pipe 4 is formed as a DN 80 pipe.
• the first conical region 7 has a reduction in cross-sectional area from a cross-sectional diameter of the large through-hole of 1 6 mm to a cross-sectional diameter of the small through hole of 1 2 mm.
• the first non-conical line section 8 thus has a cross-sectional diameter of 12 mm and has a length of about 50 mm. Longer configurations of the non-conical line section 8 are possible.
• the chamber 9 has a width of 10 mm, ie the junction of the first non-conical line section 8 in the chamber 9 is 10 mm apart from the opposite confluence of the second non-conical line section 10, to which the second cone 1 1 followed.
• the second non-conical region 10 has a cross section with a diameter of 16 mm as well as the small through hole 13 of the second cone 1 first
• the large passage opening of the second cone 1 1 has a cross section with a diameter of 18 mm.
• the second non-conical region 10 to the chamber 9 and the second conical region 1 1 with a diameter increase from 16 mm to 18 mm are important for the formation of different sized gas bubbles in the water.
• the gas bubbles required for the subsequent flotation are formed.
• the Venturi mixing element has a total length of 300 mm.
• Figures 3a to c show the arrangement of the junctions of the non-conical line sections in a side wall of the chamber 9 between the cones 7, 1 1 for a venturi mixing element 5 with 4, 7 and 19 Konencoveren.
• FIG. 4a an embodiment of the device according to the figure 1 is shown in Figure 4a, wherein the third pipe 4 opens at an angle of 45 ° in the second pipe 3.
• the confluence takes place in the flow direction of the solid-liquid mixture, which is represented by the arrow.
• the second pipe 3 has a larger diameter than the third pipe 4.
• the third pipeline 4 opens into the second conduit 3 opposite to the flow Rich ⁇ processing of the solid-liquid mixture.
• the 45 ° should not be fallen below, otherwise the mixing of the solid-liquid mixture is less effective with the water bubbles introduced gas bubbles, whereby the efficiency of the flotation process suffers.
• FIG . 4c A further embodiment of the above-described embodiment is shown in FIG . 4c.
• the device 5 comprises a plurality of venturi Mischelemen- te which nachei ⁇ Nander discharge into the flow direction of the solid-liquid mixture in the second pipeline.
• Venturi mixing elements 5 By using a plurality of parallel acting Venturi mixing elements 5 results in a better mixing of the solid-liquid mixture with the introduced with the water in the second pipe 3 gas bubbles. In addition, the cleaning effect increases in several feed locations of the gas bubbles enriched water in the solid-liquid mixture.
• FIG. 5a schematically shows a fan-shaped junction 14 of the third pipeline 4 into the second pipeline 3.
• a fan-shaped design of the junction 14 results in a better thorough mixing of the solid-liquid mixture in the second pipeline 3 with the gas bubbles-enriched water from the third Pipe 4 reached.
• the cross-sectional area of the fan-shaped junction 4 is exactly the same size as the cross-sectional area of the second pipeline 3, so that the flow velocity of the gas bubbles enriched water is not changed and the cleaning effect is not adversely affected.
• FIG. 5 b likewise shows schematically an alternative embodiment of the fan-shaped junction 14 of the third pipeline 4 into the second pipeline 3, the fan-shaped spreading of the junction 14 being aligned parallel to the flow direction of the solid-liquid mixture in the second pipeline 3.
• FIG. 5c shows the confluence of three third pipes 4 into the second pipe 3, wherein the third pipes 4 are arranged in a star shape around the second pipe 3.
• This arrangement of the junctions of several parallel streams of gas bubbles enriched water in the solid-liquid mixture leading second pipe 3 causes a better mixing of the solid-liquid mixture with the introduced with the water in the second pipe 3 gas bubbles.
• the device 1 comprises means for controlling the flows of water and / or gas. These are For example, before and after the Venturi mixing element 5 in the third pipe 4 and in the fourth pipe 6 arranged slide for influencing the respec ⁇ gene water and / or gas flow.
• the slides can be electrically or manually operated. By means of them, the number, the size and the size distribution of the gas bubbles in the liquid can be influenced.

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• Engineering & Computer Science (AREA)
• Life Sciences & Earth Sciences (AREA)
• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Biotechnology (AREA)
• Wood Science & Technology (AREA)
• Mechanical Engineering (AREA)
• Paper (AREA)
• Manufacture, Treatment Of Glass Fibers (AREA)
• Physical Water Treatments (AREA)

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• 2014
  • 2014-08-22 DE DE102014012666.8A patent/DE102014012666B4/de not_active Expired - Fee Related
• 2015
  • 2015-08-14 HU HUE15784553A patent/HUE051667T2/hu unknown
  • 2015-08-14 HR HRP20201255TT patent/HRP20201255T1/hr unknown
  • 2015-08-14 CA CA2958823A patent/CA2958823C/en active Active
  • 2015-08-14 WO PCT/DE2015/000408 patent/WO2016026477A1/de not_active Ceased
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  • 2015-08-14 JP JP2017529134A patent/JP6782697B2/ja active Active
  • 2015-08-14 PT PT157845538T patent/PT3183052T/pt unknown

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