WO2016114283A1 - 高分子凝集剤混合溶解システム及び高分子凝集剤の混合溶解方法 - Google Patents
高分子凝集剤混合溶解システム及び高分子凝集剤の混合溶解方法 Download PDFInfo
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- WO2016114283A1 WO2016114283A1 PCT/JP2016/050773 JP2016050773W WO2016114283A1 WO 2016114283 A1 WO2016114283 A1 WO 2016114283A1 JP 2016050773 W JP2016050773 W JP 2016050773W WO 2016114283 A1 WO2016114283 A1 WO 2016114283A1
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- 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
- B01F23/50—Mixing liquids with solids
- B01F23/53—Mixing liquids with solids using driven stirrers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/30—Control equipment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F21/00—Dissolving
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- 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
- B01F23/50—Mixing liquids with solids
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- 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
- B01F23/50—Mixing liquids with solids
- B01F23/54—Mixing liquids with solids wetting solids
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- 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
- B01F23/50—Mixing liquids with solids
- B01F23/59—Mixing systems, i.e. flow charts or diagrams
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- 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
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- 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
- B01F25/60—Pump mixers, i.e. mixing within a pump
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/115—Stirrers characterised by the configuration of the stirrers comprising discs or disc-like elements essentially perpendicular to the stirrer shaft axis
- B01F27/1152—Stirrers characterised by the configuration of the stirrers comprising discs or disc-like elements essentially perpendicular to the stirrer shaft axis with separate elements other than discs fixed on the discs, e.g. vanes fixed on the discs
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/80—Mixing plants; Combinations of mixers
- B01F33/81—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles
- B01F33/811—Combinations of similar mixers, e.g. with rotary stirring devices in two or more receptacles in two or more consecutive, i.e. successive, mixing receptacles or being consecutively arranged
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/80—Mixing plants; Combinations of mixers
- B01F33/82—Combinations of dissimilar mixers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/21—Measuring
- B01F35/211—Measuring of the operational parameters
- B01F35/2113—Pressure
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/21—Measuring
- B01F35/212—Measuring of the driving system data, e.g. torque, speed or power data
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/22—Control or regulation
- B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
- B01F35/2213—Pressure
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/22—Control or regulation
- B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
- B01F35/2214—Speed during the operation
- B01F35/22142—Speed of the mixing device during the operation
- B01F35/221422—Speed of rotation of the mixing axis, stirrer or receptacle during the operation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/71—Feed mechanisms
- B01F35/717—Feed mechanisms characterised by the means for feeding the components to the mixer
- B01F35/7173—Feed mechanisms characterised by the means for feeding the components to the mixer using gravity, e.g. from a hopper
- B01F35/71731—Feed mechanisms characterised by the means for feeding the components to the mixer using gravity, e.g. from a hopper using a hopper
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5227—Processes for facilitating the dissolution of solid flocculants in water
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/127—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
- B01F2101/305—Treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
Definitions
- the present invention relates to a polymer flocculant mixed dissolution system and a polymer flocculant mixed dissolution method capable of generating a polymer flocculant solution in a short time with low power, and in particular, solid polymer flocculence.
- the present invention relates to a technique for dissolving an agent in water as a solvent.
- sludge In the sludge treatment field, sludge is concentrated and dehydrated. At that time, in order to improve the sludge concentration efficiency and dewatering efficiency, a flocculant is added to agglomerate the sludge. Further, in the field of water treatment, the suspension is coagulated and precipitated. At this time, in order to improve the coagulation sedimentation efficiency, a treatment for coagulating the suspension by adding a coagulant to the water to be treated is performed.
- various flocculants such as inorganic flocculants and cationic or anionic polymer flocculants are selectively used.
- the solid polymer flocculant has a disadvantage that it is difficult to dissolve in a liquid while high aggregation effect by cross-linking aggregation is obtained. For this reason, the solid polymer flocculant is not directly added to sludge, but is dissolved in water in advance to form an aqueous solution, and then added to sludge or the like so as to achieve a predetermined chemical injection rate.
- the polymer flocculant has another problem that it degrades over a long time after making it into an aqueous solution and the agglomeration effect decreases, it is not possible to prepare a large amount of aqueous solution in advance and store it in a tank or the like. It is not preferable. In order to sufficiently obtain the original flocculating effect of the polymer flocculant, it is preferable to add a fresh aqueous solution having a short elapsed time after being dissolved in water.
- Patent Document 1 discloses a technique in which an undissolved polymer flocculant is crushed and dissolved in water using a cylindrical mesh filter and a roller that rotates in the filter.
- Patent Documents 2 and 3 are also techniques for crushing undissolved polymer flocculants and dissolving them in water.
- Patent Document 4 discloses a technique in which an undissolved polymer flocculant is crushed and dissolved in water using a colloid mill.
- Patent Documents 5 and 6 are also techniques for crushing an undissolved polymer flocculant and dissolving it in water. As a technique for crushing undissolved polymer flocculant, use of a fixed disk and a rotating disk has also been studied.
- the polymer flocculant can be dissolved in a short time by using the technique disclosed in Patent Documents 1-6, but the power required for mechanically crushing the undissolved polymer flocculant is never small. Absent. Furthermore, there is a concern that the action of mechanically crushing the polymer flocculant destroys the molecular structure of the polymer flocculant and causes deterioration of the agglomeration action.
- the present invention has been made in order to solve the above-mentioned problems mentioned as an example, and an object of the present invention is to provide a polymer flocculant capable of generating a polymer flocculant solution in a short time with low power.
- An object of the present invention is to provide a mixed dissolution system and a method for mixing and dissolving a polymer flocculant.
- Another object of the present invention is to provide a polymer flocculant mixing and dissolving system capable of quickly dissolving an undissolved polymer flocculant without adding mechanical action such as crushing and crushing. It is to provide a method for mixing and dissolving a molecular flocculant.
- the polymer flocculant mixing and dissolving system of the present invention comprises a mixing tank for mixing a solid polymer flocculant with water as a solvent, and an aqueous solution containing the mixed polymer flocculant, A liquid feeding means for feeding liquid from the mixing tank, a casing disposed in the middle of the flow path of the aqueous solution discharged from the liquid feeding means, and an impeller having a radial groove formed on the entire circumference.
- a vortex mixer for mixing and dissolving the polymer flocculant by rotating the impeller within the casing and applying pressure while forming a vortex flow of the aqueous solution along the inner peripheral wall of the casing;
- Pressure adjusting means arranged in the middle of the flow path of the aqueous solution that has passed through the mixer and controlling the pressure on the discharge side of the vortex mixer, the pressure adjusting means corresponding to the type of polymer flocculant Has information on the set pressure value Based on the information, the pressure in the discharge side of the vortex mixer so that the pressure corresponding to the kind of polymer flocculant, characterized by pressure control.
- the vortex pump is sometimes referred to as a cascade pump.
- the flow path of the aqueous solution from the liquid feeding means to the pressure adjusting means may be configured such that at least two or more vortex mixers that sequentially pressurize the aqueous solution at each stage are arranged in series.
- Power detection means for detecting the power of the vortex mixer at each stage, and rotation of the impeller of each stage vortex mixer so that the power of the vortex mixer at each stage detected by the power detection means becomes equal
- a power adjustment means for controlling the number may be further provided.
- Power adjustment means for controlling the power of the vortex mixer of each stage based on the flow rate of the aqueous solution fed by the liquid delivery means and the information, further comprising power setting value information of the vortex mixer of each stage It can also be configured.
- “so that the power of the vortex mixers at each stage is equal” means that the power is equalized in the direction in which the unequal state is eliminated, so that the power is completely equal. It doesn't mean that. Therefore, even if there is a difference in power (for example, about ⁇ 10%), if equalization is included, it is included in “so that the power of the vortex mixers in each stage is equal”.
- the method for mixing and dissolving the polymer flocculant of the present invention includes a step of mixing a solid polymer flocculant with water as a solvent, and feeding an aqueous solution containing the mixed polymer flocculant into a vortex mixer. A step of applying pressure while forming a vortex flow of the aqueous solution along the inner peripheral wall of the casing of the vortex mixer to mix and dissolve the polymer flocculant in the vortex mixer, and the aqueous solution that has passed through the vortex mixer.
- a solid polymer flocculant is mixed with water as a solvent, and an aqueous solution obtained by mixing is fed into a vortex mixer, and in this vortex mixer, a vortex flow of an aqueous solution along the inner peripheral wall of a casing is formed.
- the polymer flocculant is mixed and dissolved by pressurization.
- the present invention since mechanical action such as crushing and crushing is not used, anxiety that the molecular structure of the polymer flocculant is destroyed and deteriorated, and further, in the sludge treatment process and the water treatment process. There is also an advantage that the anxiety that is affected can be reduced compared to the conventional case.
- FIG. 1 is a schematic diagram showing the overall configuration of a polymer flocculant mixing and dissolving system (hereinafter referred to as “mixing and dissolving system”) according to the present embodiment.
- the mixing and dissolving system 1 includes a mixing tank 2 for mixing a solid polymer flocculant with water as a solvent.
- the mixing tank 2 is a closed or open tank capable of storing water as a solvent. Water as a solvent is supplied into the tank through a flow path such as a pipe connected to the upper part of the tank.
- the mixing tank 2 can further include stirring means for stirring the water in the tank and dispersing the polymer flocculant.
- a stirrer 21 that rotates a stirring blade disposed in a tank by a drive motor can be used. You may employ
- the volume of the mixing tank 2 can be appropriately designed according to the amount of the aqueous solution to be prepared.
- the volume can be designed to be suitable for operation by setting the mixing time (that is, the residence time) in the tank to 5 to 15 minutes, preferably 10 minutes.
- the reason for setting this mixing time is to ensure the time necessary for swelling the polymer flocculant to such an extent that it can be dissolved in the subsequent step. If the mixing time is too short, the polymer flocculant may not swell sufficiently, and may not be sufficiently dissolved even in the subsequent steps. On the other hand, if it is too long, it is against the purpose of obtaining a fresh aqueous solution. In addition, there is a disadvantage that the mixing tank 2 is enlarged.
- Water as a solvent can be continuously supplied into the tank. If the continuous supply method is adopted, there is an advantage that the mixing tank 2 can be miniaturized. Instead of the continuous supply method, a batch method may be employed in which a fixed amount of water is poured into the tank, the polymer flocculant is added, and then the inserted amount of water (aqueous solution) is extracted.
- the powdery or granular solid polymer flocculant is quantitatively added to the mixing tank 2 using, for example, a hopper 22 disposed at the top of the mixing tank 2.
- the hopper 22 has a main body formed in a conical body such as an inverted cone or an inverted pyramid, stores the polymer flocculant therein, and quantitatively cuts out the polymer flocculant from the bottom to mix the tank 2. It is the composition added to.
- the hopper 22 may be a closed system so that the polymer flocculant does not absorb moisture during storage, and may further take moisture-proof measures such as blowing dry gas.
- a discharging means 22a for cutting out the polymer flocculant from the hopper in a fixed amount is disposed.
- a screw conveyor type quantitative feeder can be used as an example of the discharging means 22a.
- the hopper 22 is a preferable example of means for quantitatively adding the polymer flocculant to the mixing tank 2, and other addition means may be adopted, or an operator may add it manually. Also good.
- the mixing tank 2 is connected to a liquid feed pump 3 which is an example of a liquid feed means for continuously extracting the aqueous solution in the tank and feeding it to a downstream process.
- the aqueous solution withdrawn from the mixing tank 2 contains already dissolved polymer flocculant and swollen undissolved polymer flocculant. Further, it may contain a polymer flocculant powder. Since the aqueous solution has a high viscosity in the amount of the polymer flocculant dissolved, the aqueous solution is sent to the downstream process using the liquid feed pump 3.
- a single screw pump suitable for feeding a highly viscous liquid in a fixed amount can be used.
- other types of metering pumps may be used, and a configuration may be adopted in which metering is performed by a combination of a flow rate adjusting valve and a pump. You may employ
- the first vortex mixer 4A is connected to a flow path such as a pipe connected to the discharge side of the liquid feed pump 3, and then the second vortex mixer 4B is connected. That is, the first vortex mixer 4A and the second vortex mixer 4B for mixing and dissolving the polymer flocculant are arranged in series in two stages.
- a valve V (V1, V2, V3) or a pressure gauge is provided in the middle of the flow path from the liquid feed pump 3 to the first vortex mixer 4A and in the middle of the flow path from the first vortex mixer 4A to the second vortex mixer 4B.
- P (P1, P2, P3) or the like may be provided.
- a coupled meter can be used as an example of the pressure gauge P1. Furthermore, in order to enable the operation of the first vortex mixer 4A alone, a bypass flow path for sending downstream without passing through the second vortex mixer 4B may be provided.
- the first vortex mixer 4A and the second vortex mixer 4B may be arranged with vortex mixers with different processing capabilities, but it is preferable to use the same structure and the same processing capability. In this way, the convenience in terms of maintenance is enhanced, for example, the number of spare parts can be reduced.
- the structure of the vortex mixers 4A and 4B will be described in more detail.
- a casing 41 having an aqueous solution suction port 41a and a discharge port 41b, an impeller 42 corresponding to an impeller in terms of a pump,
- a drive motor 43 as a drive mechanism for rotating the vehicle 42 is provided.
- the drive motor 43 is shown in a block diagram.
- the casing 41 communicates with each of the suction port 41a and the discharge port 41b of the aqueous solution and has an internal region 41c that rotatably accommodates the impeller 42.
- the inner region 41c has an inner peripheral surface 41d that faces the outer peripheral edge of the impeller 42 through a gap in a non-contact manner.
- the aqueous solution sucked into the casing 41 from the suction port 41a is transferred while being pressurized in the casing inner region 41c by the rotating impeller 42, and is discharged from the discharge port 41b.
- the suction port 41a and the discharge port 41b are preferably arranged closer to the upper portion of the casing 41, thereby ensuring a long pressurization distance in the casing 41.
- a buffer region 44 having an enlarged volume is formed at the discharge port 41b. Since the aqueous solution discharged from the casing 41 forms a vortex flow, the vortex flow can be eliminated by the buffer region 44.
- the inlet 41 a is provided with an inlet 41 e for injecting so-called “priming water” into the casing 41 at startup.
- the impeller 42 is formed in a generally disc shape, and is arranged in the inner region 41c of the casing 41 so as to be rotatable about a line extending in a direction perpendicular to the center of the circle (perpendicular to the paper surface) as a rotation axis.
- a large number of grooves 45 for forming a fine vortex flow along the inner peripheral surface 41 d of the casing 41 are formed radially on the outer peripheral edge of the impeller 42.
- the plurality of radial grooves 45 are formed on the outer peripheral edge of the impeller 42 over the entire circumference. For details of the shape of the groove 45, as shown in a partially enlarged perspective view of FIG.
- a first blade portion 45a having a plane formed in the rotational direction and a direction perpendicular to the rotational direction. It is comprised by the part 45b of the 2nd blade
- the first blade portion 45a is formed such that the upper end protrudes outward from the second blade portion 45b.
- the second blade portion 45b is formed in a triangular cross section whose thickness increases from the upper end toward the lower end. Therefore, the size of the groove can be changed by changing the size of the first blade portion 45a and the second blade portion 45b.
- the size of the groove 45 can be changed as appropriate, by making the shape as shown in FIG.
- a fine vortex flow is repeatedly formed along the casing inner peripheral wall 41d by the groove 45 of the rotating impeller 42, thereby The aqueous solution inside can be pressurized.
- the provision of the second blade portion 45b makes it possible to form a uniform vortex flow on both sides (left and right direction) of the impeller 42, and to promote mixing and dissolution of the polymer flocculant. .
- the second blade portion 45b is not necessarily provided.
- a rotating shaft 46 is connected to the impeller 42 along the rotating shaft.
- the rotation shaft 46 penetrates the casing 41 and is connected to a drive motor 43 disposed outside.
- the drive shaft 43 is configured to rotate when the drive motor 43 is driven.
- the portion that penetrates the casing 41 can be sealed by a sealing mechanism (not shown) such as a mechanical seal.
- the vortex mixers 4A and 4B are further provided with power adjusting means for making the rotational speed of the impeller 42 variable.
- an inverter 47 can be used as an example of the power adjusting means. Accordingly, the first vortex mixer 4A and the second vortex mixer 4B can operate the impeller 42 at the same rotation speed or at different rotation speeds, and by changing the rotation speed, the polymer flocculant can be operated.
- the initial setting value may be set to a frequency of 60 Hz (or 50 Hz), and the frequency may be variably adjusted so as to obtain an appropriate rotational speed.
- the power (load factor) of the inverter 47 can be used as an index for obtaining an appropriate rotational speed.
- the power [kW] of the drive motor 43 may be measured using a dynamometer or the like, and the measurement result may be used as an index.
- the power measured from the inverter 47 with a built-in dynamometer may be used as an index.
- other power detection means may be used.
- the first vortex mixer 4A and the second vortex mixer 4B work so as to work equally with each other, in other words, when a state where the work is biased to one side is improved.
- the time can be mentioned. That is, since pressurization is performed by the two-stage vortex mixers 4A and 4B, it is easier to pressurize to the target pressure when operating at as high a rotational speed as possible.
- an uneven state occurs in which work is biased on one side, an overload is likely to occur in the drive motor 43 that is biased. Therefore, the overload of the drive motor 43 is prevented by improving so as to work equally. If it can be improved to work evenly, the power consumption can be minimized, and a power saving effect can be obtained.
- Adjustment means are provided.
- the pressure adjusting valve 5 that adjusts the pressure by changing the valve opening, the pressure sensor 51, and the opening of the pressure adjusting valve 5 so that the detected value of the pressure sensor 51 becomes a predetermined pressure.
- a combination of pressure control units 52 to be controlled can be used.
- the predetermined pressure is, for example, a set pressure value determined in advance according to the type of the polymer flocculant.
- the present embodiment focuses on the property that the polymer flocculant dissolves easily when the pressure is high because penetration into the solvent is facilitated, and the degree of pressure varies depending on the type.
- a configuration in which pressurization is controlled to a pressure suitable for dissolution is employed. Therefore, it is preferable to have information on the pressure setting value determined in advance in association with the type of the polymer flocculant, or store it in the memory of the computer of the pressure control unit 52 or the like.
- the pressure set value may be determined based on, for example, the component and molecular weight of the polymer flocculant, or may be determined by actually performing a test. Then, depending on the type of polymer flocculant, the operator sets the pressure setting value of the pressure control unit 52, or the pressure control unit 52 reads information from the memory or the like and sets the pressure setting value.
- the aqueous solution (that is, the polymer flocculant solution) that has passed through the pressure regulating valve 5 may be added to the sludge in the sludge treatment process as it is, or may be added to the sludge once through a buffer tank or the like. Good. In the water treatment step, it can be similarly added to the water to be treated.
- the sludge to which the polymer flocculant solution has been added so as to achieve a predetermined chemical injection rate is supplied to, for example, a decanter type centrifugal concentrator or centrifugal dehydrator, and solid-liquid separation for concentration or dehydration do.
- the water to be treated to which the polymer flocculant solution is added so as to obtain a predetermined chemical injection rate, is supplied to a settling tank, a filter, and the like to perform solid-liquid separation.
- the polymer flocculant solution prepared by the mixed dissolution system 1 of the present embodiment is not limited to the type of solid-liquid separation device, and can be used for a known solid-liquid separation device.
- the vortex mixers 4A and 4B having the configuration shown in FIG. 2 are shown as a preferred form, but a general vortex pump may be used instead.
- the vortex pump may also be referred to as a cascade pump.
- the type of the polymer flocculant applied to the mixing and dissolving system 1 of the present embodiment is not particularly limited, and can be appropriately selected according to the type and composition of the treated sludge and treated water. .
- cationic polymer flocculants are the mainstream, but anionic and amphoteric polymer flocculants may also be used.
- methacrylic acid ester or acrylic acid ester can be used. More specifically, dimethylaminoethyl methacrylate or dimethylaminoethyl acrylate can be used.
- a crosslinkable or amidine polymer flocculant may be used.
- polymer flocculants have a molecular weight of 1.5 to 16 million. Generally, the larger the molecular weight, the higher the viscosity of the aqueous solution. Therefore, the viscosity can be grasped by using the molecular weight as a guide.
- the liquid feed pump 3, the first vortex mixer 4 ⁇ / b> A, and the second vortex mixer 4 ⁇ / b> B are each driven, and the set value of the control pressure by the pressure controller 52 is determined / changed.
- the pressure set value is set to 0.3 MPa.
- the polymer flocculant mixed with water dissolves in water in the mixing tank 2, but a part remains undissolved. However, the mixing tank 2 is in a swollen state by securing a mixing time with water of about 10 minutes.
- the water (aqueous solution) whose viscosity has been increased by dissolving the polymer flocculant is fed into the first vortex mixer 4A by the liquid feed pump 3 while containing the undissolved polymer flocculant.
- the flow rate of the liquid feed pump 3 can be set to 8 to 25 L / min, for example.
- the first vortex mixer 4A and the second vortex mixer 4B set the frequency to 60 Hz (or 50 Hz) by the inverter 47, for example, and drive the drive motor 43.
- the appropriate value of the frequency corresponding to the type of the polymer flocculant is known in advance, the appropriate value is set.
- the impeller 42 is rotated, for example, within a range of 800 to 3500 min ⁇ 1 .
- the aqueous solution sent to the first vortex mixer 4A by the liquid feed pump 3 repeatedly forms a fine vortex flow along the inner peripheral surface 41d of the casing 41 by the rotating impeller 42, and is pressurized by this.
- an aqueous solution that was ⁇ 0.05 MPa near the suction port is pressurized to 0.12 MPa near the discharge port.
- the impeller 42 rotates in a non-contact manner with respect to other portions, the action of mechanically crushing the polymer flocculant and the shear stress hardly occur.
- the mixing and dissolution of the polymer flocculant is promoted by the fine vortex flow repeatedly formed through the fine grooves 45 formed radially and the pressurizing action.
- the aqueous solution that has passed through the first vortex mixer 4A is repeatedly pressurized by the rotating impeller 42 along the inner peripheral surface 41d of the casing 41 in the subsequent second vortex mixer 4B. Go.
- an aqueous solution that was 0.12 MPa near the suction port is pressurized to a target pressure of 0.3 MPa near the discharge port. That is, the vortex mixers 4A and 4B having a two-stage configuration in series are sequentially pressurized to a pressure suitable for dissolving the polymer flocculant.
- the second vortex mixer 4B promotes the mixing and dissolution of the polymer flocculant by the fine vortex flow that is repeatedly formed through the fine grooves 45 formed radially and the pressurizing action.
- the polymer flocculant can be completely dissolved by pressurizing to a pressure suitable for dissolving the polymer flocculant.
- the increase in the viscosity of the second aqueous solution converges because the polymer flocculant is completely dissolved.
- rotational speed a of the liquid feed pump 3 [min -1] are determined rotational speed c [min -1] of the rotational speed of the first vortex mixer 4A b [min -1] and a second vortex mixer 4B .
- the indicated value of the pressure sensor 51 changes when the required flow rate becomes F1 [L / min], but is automatically controlled to an appropriate pressure (pressure set value) by the pressure adjustment valve 5.
- the rotation speed b [min ⁇ 1 ] of the first vortex mixer 4A and the rotation of the second vortex mixer 4B are maintained so as to keep the power (ie, power consumption) of the first vortex mixer 4A and the second vortex mixer 4B properly.
- a deviation is given to the number c [min ⁇ 1 ].
- FIG. 4A shows the result of the actual test. Since the inverter load factor% was biased to 46/62, the frequency of the second eddy current mixer 4B was lowered to 52 Hz. The inverter load factor% was substantially equal to 46/48. Alternatively, using a dynamometer or the like, the power [kW] of the drive motor 43 of each of the first vortex mixer 4A and the second vortex mixer 4B is measured, and the frequency has a deviation so that the power of both is equal. Do it.
- the polymer flocculant can be dissolved with a low motive power with reduced power consumption.
- Such power control can be automatically controlled by a control unit using a computer. Or you may make it an operator control. Thereafter, even after shifting to the normal operation, monitoring may be performed as appropriate, and the power may be adjusted so that the first vortex mixer 4A and the second vortex mixer 4B work equally with each other.
- feedforward control can be performed.
- the rotational speed c [min -1] for example, the power of the rotational speed of the first vortex mixer 4A b [min -1] and a second vortex mixer 4B is equalized
- the set value with a deviation is determined in association with the required flow rate of the aqueous solution and controlled based on this information.
- Feed-forward control is performed to change the rotation speed.
- the viscosity of the aqueous solution of the polymer flocculant varies greatly depending on the component and molecular weight. Furthermore, in this embodiment, since the vortex mixers 4A and 4B are arranged in series to promote dissolution sequentially, the viscosity of the aqueous solution passing through the first vortex mixer 4A at the front stage and the second vortex mixer 4B at the rear stage is high. Different. Accordingly, the work tends to be uneven between the first vortex mixer 4A and the second vortex mixer 4B.
- the load on the second vortex mixer 4B in the latter stage is often excessive as compared with the first vortex mixer 4A in the first stage.
- This tendency is particularly strong in the case of a cross-linked polymer flocculant that is difficult to dissolve among those having a relatively low viscosity. Therefore, for example, the polymer flocculant is classified according to the viscosity of the aqueous solution. Then, the second eddy current mixer 4B is operated with the rotational speed c [min ⁇ 1 ] lower than the rotational speed b [min ⁇ 1 ] of the first vortex mixer 4A.
- the first eddy current mixer 4A is set to a frequency of 60 Hz
- the second eddy current mixer 4B is set to a frequency of 50 Hz. That is, the rotational speed is set to have a deviation so that the power is even.
- overload of the drive motor 43 of the second vortex mixer 4B can be prevented.
- a polymer flocculent can be dissolved with the low power which suppressed electric power consumption more.
- the required flow rate [L / min] of the aqueous solution and the rotational speed [min ⁇ 1 ] of the vortex mixers 4A and 4B (or the frequency [Hz]). ) Is determined in association with the viscosity of the polymer flocculant, and based on this information, the rotation speed b [min ⁇ 1 ] of the first vortex mixer 4A and the rotation of the second vortex mixer 4B are determined.
- the number c [min ⁇ 1 ] can be set appropriately.
- the first vortex mixer 4B and the second vortex mixer 4B in which an aqueous solution containing an undissolved polymer flocculant that could not be dissolved in the mixing tank 2 is arranged in series.
- the pressure is adjusted so that the pressure on the discharge side of the second vortex mixer 4B in the subsequent stage becomes a pressure suitable for dissolving the polymer flocculant.
- each of the vortex mixers 4A and 4B is provided with an impeller 42 in which a radial groove 45 is formed on the outer periphery of the eddy current mixer 4A.
- the aqueous solution can be pressurized to a high pressure by repeatedly forming along the surface 41d.
- an aqueous solution (dissolved solution) of the polymer flocculant can be obtained in a short time and with low power, and an excellent sludge treatment can be performed using the fresh aqueous solution of the polymer flocculant. And water treatment can be performed. Therefore, as compared with the conventional large storage tank and the melting method using a stirrer, the entire system can be saved in space, and the operating load of the system can be reduced. Furthermore, since it can be dissolved in a short time, the planned dissolution operation of the polymer flocculant becomes unnecessary.
- the vortex mixer may have three or more stages.
- the impeller 42 rotates in a non-contact manner with respect to other parts, and therefore, the action of mechanically crushing the polymer flocculant and the shear stress are hardly expressed.
- anxiety that the molecular structure of the polymer flocculant is destroyed and deteriorated, and anxiety that affects the sludge treatment process and the water treatment process can be reduced as compared with the prior art.
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Abstract
Description
ここで、一般の渦流(かりゅう)ポンプであっても、膨潤した未溶解の高分子凝集剤を溶解する目的で使用されている場合は、本発明の作用・効果を得る目的で使用されているので、前記渦流ミキサーに含まれると解釈される。なお、渦流(かりゅう)ポンプは、カスケードポンプと称されることもある。
(2)前記送液手段から前記圧力調節手段に至る水溶液の流路には、各段で水溶液を順次加圧する少なくとも2段以上の渦流ミキサーが直列配置された構成とすることもできる。
(3)各段の渦流ミキサーの動力を検知する動力検知手段と、前記動力検知手段で検知される各段の渦流ミキサーの動力が均等になるように、各段の渦流ミキサーの羽根車の回転数を制御する動力調節手段と、をさらに備えた構成とすることもできる。
(4)前記送液手段で送液する水溶液の流量設定値に対応付けられ、且つ、各段の渦流ミキサーの動力が均等になるように回転数の偏差をもたせた、各段の渦流ミキサーの動力設定値の情報を有し、前記送液手段で送液する水溶液の流量と前記情報に基づいて各段の渦流ミキサーの動力を制御する動力調節手段を、さらに備えた構成とすることもできる。
(5)目標濃度になるように高分子凝集剤を溶解させたときの水溶液の粘度に対応付けられ、且つ、各段の渦流ミキサーの動力が均等になるように回転数の偏差をもたせた、各段の渦流ミキサーの動力設定値の情報を有し、前記送液手段で送液する水溶液の流量と前記情報に基づいて各段の渦流ミキサーの動力を制御する動力調節手段を、さらに備えた構成とすることもできる。
なお、「各段の渦流ミキサーの動力が均等になるように」とは、不均等な状態が解消される方向に向けて均等化するという技術的意義であり、動力を完全に同じ値に揃えることを意味するのではない。従って、たとえ動力に差異(例えば、±10%程度)があったとしても均等化がされていれば「各段の渦流ミキサーの動力が均等になるように」に含まれる。
続いて、上述の混合溶解システム1を用いて、高分子凝集剤の溶解液を得る方法について説明する。なお、以下の説明では、カチオン系の高分子凝集剤の場合を主体にして説明するが、特筆しない限り、他の高分子凝集剤でも同様の作用・効果を奏する。混合溶解システム1が起動されると、まず、溶媒である水を混合槽2に所定の流量で供給すると共に、所定の濃度の水溶液となるように高分子凝集剤を所定の流量で添加する。濃度の一例としては、0.1~0.3質量%、好ましくは0.2質量%に設定することができる。その一方で、送液ポンプ3、第1渦流ミキサー4A及び第2渦流ミキサー4Bを各々駆動させると共に、圧力制御部52による制御圧力の設定値を決定/変更する。ここでは、一例として圧力設定値を0.3MPaとする。
2 混合槽
3 送液ポンプ
4A 第1渦流ミキサー
4B 第2渦流ミキサー
45 溝
5 圧力調節バルブ
51 圧力センサー
52 圧力制御部
Claims (6)
- 固体状の高分子凝集剤を、溶媒である水と混合するための混合槽と、
混合した高分子凝集剤を含んだ水溶液を、前記混合槽から送液する送液手段と、
前記送液手段から吐出される前記水溶液の流路の途中に配置されるケーシングと、外周に放射状の溝が全周に亘って形成された羽根車を有し、前記ケーシング内で前記羽根車を回転させて、該ケーシングの内周壁に沿う水溶液の渦流れを形成しながら加圧して、高分子凝集剤を混合溶解させるための渦流ミキサーと、
前記渦流ミキサーを通過した前記水溶液の流路の途中に配置され、前記渦流ミキサーの吐出側の圧力を制御する圧力調節手段と、を備え、
前記圧力調節手段は、高分子凝集剤の種類に対応付けて決めた圧力設定値の情報を有し、前記情報に基づいて、前記渦流ミキサーの吐出側の圧力が高分子凝集剤の種類に対応する圧力となるように、圧力制御することを特徴とする高分子凝集剤混合溶解システム。 - 前記送液手段から吐出される前記水溶液の流路には、各段で水溶液を順次加圧する少なくとも2段以上の渦流ミキサーが直列配置されていることを特徴とする請求項1に記載の高分子凝集剤混合溶解システム。
- 各段の渦流ミキサーの動力を検知する動力検知手段と、
前記動力検知手段で検知される各段の渦流ミキサーの動力が均等になるように、各段の渦流ミキサーの羽根車の回転数を制御する動力調節手段と、をさらに備えていることを特徴とする請求項2に記載の高分子凝集剤混合溶解システム。 - 前記送液手段で送液する水溶液の流量設定値に対応付けられ、且つ、各段の渦流ミキサーの動力が均等になるように回転数の偏差をもたせた、各段の渦流ミキサーの動力設定値の情報を有し、前記送液手段で送液する水溶液の流量と前記情報に基づいて各段の渦流ミキサーの動力を制御する動力調節手段を、さらに備えていることを特徴とする請求項2に記載の高分子凝集剤混合溶解システム。
- 目標濃度になるように高分子凝集剤を溶解させたときの水溶液の粘度に対応付けられ、且つ、各段の渦流ミキサーの動力が均等になるように回転数の偏差をもたせた、各段の渦流ミキサーの動力設定値の情報を有し、前記送液手段で送液する水溶液の流量と前記情報に基づいて各段の渦流ミキサーの動力を制御する動力調節手段を、さらに備えていることを特徴とする請求項2に記載の高分子凝集剤混合溶解システム。
- 固体状の高分子凝集剤を、溶媒である水と混合する工程と、
混合した高分子凝集剤を含む水溶液を、渦流ミキサーに送り込む工程と、
前記渦流ミキサーにおいて、該渦流ミキサーのケーシングの内周壁に沿って水溶液の渦流れを形成しながら加圧して、高分子凝集剤を混合溶解させる工程と、
前記渦流ミキサーを通過した前記水溶液の流路の途中に配置した圧力調節手段で前記渦流ミキサーの吐出側の圧力を制御する工程と、を含み、
前記圧力を制御する工程は、高分子凝集剤の種類に対応付けて決めた圧力設定値の情報に基づいて、前記渦流ミキサーの吐出側の圧力が高分子凝集剤の種類に対応する圧力となるように、圧力制御することを特徴とする高分子凝集剤の混合溶解方法。
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CN107106941B (zh) | 2019-08-23 |
US20180071699A1 (en) | 2018-03-15 |
JP5731089B1 (ja) | 2015-06-10 |
KR101984528B1 (ko) | 2019-05-31 |
JP2016129878A (ja) | 2016-07-21 |
US10201788B2 (en) | 2019-02-12 |
KR20170091145A (ko) | 2017-08-08 |
CN107106941A (zh) | 2017-08-29 |
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