WO2011030485A1 - Flocculation precipitation treatment method - Google Patents
Flocculation precipitation treatment method Download PDFInfo
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- WO2011030485A1 WO2011030485A1 PCT/JP2010/003867 JP2010003867W WO2011030485A1 WO 2011030485 A1 WO2011030485 A1 WO 2011030485A1 JP 2010003867 W JP2010003867 W JP 2010003867W WO 2011030485 A1 WO2011030485 A1 WO 2011030485A1
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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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
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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
- C02F1/5209—Regulation methods for flocculation or precipitation
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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
- C02F1/34—Treatment of water, waste water, or sewage with mechanical oscillations
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/44—Time
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
Definitions
- the present invention is formed by a micro-floccing process in which an inorganic flocculant is injected into water to be treated such as river water, rain water, factory effluent and the like, and fine suspended particles contained in the water to be treated are agglomerated.
- a method for coagulating and precipitating water to be treated based on the combination of fine floc particles in a sludge / blanket tank and / or the combination of fine flocs and existing flocs, and the separation of the flocculent particles.
- a method for coagulating and precipitating water to be treated based on the combination of fine floc particles in a sludge / blanket tank and / or the combination of fine flocs and existing flocs, and the separation of the flocculent particles.
- the flocculation and precipitation treatment of the water to be treated is employed as a pretreatment for sand filtration.
- an inorganic flocculant is injected into the water to be treated, and fine suspended particles contained in the water to be treated.
- the coagulation sedimentation apparatus is roughly classified into a conventional system and a high-speed coagulation sedimentation basin system. The latter is further classified into a slurry circulation system and a sludge blanket system, and the present invention selects the latter.
- the precipitate is separated through the fine flocking step of the suspended particles and the fine flocking step.
- the current coagulation-precipitation treatment method is based on the following general formula shown by Smolkovsky.
- dN / dt - ⁇ (4G ⁇ / ⁇ ) ⁇ N (a) (N: number of particles (fine flock or flock) per unit volume ⁇ : collision efficiency based on influence of inorganic flocculant G: velocity gradient, ⁇ : average volume of particles (fine flock or flock) in unit volume)
- Patent Document 1 a multi-stage rapid stirring tank is provided, and the lower limit of the stirring strength is set for the first first tank, and stirring is performed for the second tank and below. After setting the upper limit of strength, by dividing and injecting the inorganic flocculant into each rapid stirring tank, it is possible to improve particle separation efficiency and reduce the concentration of remaining inorganic flocculant (See description related to claim 6 of the claims and claim 6 of the specification).
- the amount of the inorganic flocculant used is limited as compared with the prior art, and the stirring strength
- an inclined plate with a narrow pitch in the sedimentation pond In order to prevent the filtration function of the sand filtration tank from being deteriorated by the above-mentioned miniaturization of flocs, an inclined plate with a narrow pitch in the sedimentation pond And proposed a structure for efficiently separating fine flocs, and patent registration has already been made for the structure (Japanese Patent No. 4316671).
- the fine flocs are inevitably formed. Flocculates by aggregating with each other in the sludge blanket tank, and further adsorbs the fine flocs that subsequently flow in, thereby further promoting the flocking.
- the flocculated particles are also dense, and thus quickly settle in the sludge / blanket tank.
- the STR Sudden Time Ratio: the same temperature as the water to be treated 1
- Ts the suction time of treated water 1
- Tv 5A and 5B the graphs in FIGS. 5A and 5B end the temporal change of the STR value in the fine flocking process and the fine flocking process corresponding to the change. The correspondence with the change in the number of fine floc particles at the stage is shown.
- FIG. 5 (a) the experimental conditions in micro flocculation step for realizing the data
- G R value is rapid stirring intensity in one rapid agitation tank 10
- stirrring coefficient is C
- the stirring blade (b)
- the area is A (m 2 )
- the peripheral speed of the stirring blade is v (m / sec)
- the kinematic viscosity coefficient is ⁇ (m 2 / sec)
- the volume (capacity) of the stirring tank is V (m 3 ).
- kaolin white porcelain clay in clarified water, which realizes the degree of suspension of clarified water
- PAC polyaluminum chloride
- the number of particles (particles / mL) having a particle size of 0.5 to 1 ⁇ m decreases as shown in (a).
- the number (particles / mL) of particles having a particle size of 30 ⁇ m or more increases until the STR value reaches a predetermined value (specifically, 2 or less), but thereafter Is descending as in the case of (a).
- fine flocked particles are flocked.
- the small number of fine flock particles flowing in is that the N on the right side in the equation (a) is small, and thus dN
- / dt is small, that is, the rate of change from fine flock to flock is small. That is, when the number of floc particles flowing into the sludge / blanket tank is small as described above, the degree of the flocking process that occurs based on the flow of a predetermined amount of fine flock particles in the sludge / blanket tank Moreover, it must be reduced. Such a result inevitably impedes the function of separating the precipitate on the premise of flocking in the sludge / blanket tank.
- the degree of the flocking step is maintained at a predetermined level by directly returning the flocked particles precipitated in the sludge / blanket tank and discharged to the sludge storage tank to the sludge / blanket tank.
- a method is disclosed.
- the flocculent particles returning from the sludge storage tank have not undergone the rapid stirring process, and therefore the aggregating ability based on the residual coagulant is extremely poor. Flocking based on the formation of grains and dense micro flocs cannot be expected.
- An object of the present invention is to provide a method for coagulating and precipitating water to be treated so that the concentration of particles in the flocking process does not decrease in the sludge / blanket tank.
- an inorganic flocculant injecting step for injecting an inorganic flocculant into the water to be treated; and the water to be treated into which the inorganic flocculant has been injected are mixed and stirred in a rapid stirring tank to make fine particles in the water to be treated.
- the fine flocking process in which suspended particles are finely flocked in advance, and in the sludge / blanket tank, the fine flock particles that have flowed in and / or the fine flock particles or flock particles and the existing flock particles are combined.
- Water to be treated and a step of precipitating and separating the flocked particles, and discharging the precipitated flocked particles and the remaining particles separated without precipitation to the outside of the sludge / blanket tank, respectively.
- This is a coagulation-precipitation method, which supports the precipitation separation function based on flocking in a sludge / blanket tank caused by a decrease in the coagulation ability of inorganic coagulants.
- the precipitated flocculated particles are returned to the previous stage of the fine flocculation step and injected into the water to be treated at the same time as or before and after the injection of the inorganic flocculant.
- Conditions for executing the inorganic flocculant injection step that is, the type and amount of the inorganic flocculant, and the number of compartments in which the stirring tank is provided before the flocculation / precipitation treatment of the water to be treated with respect to the amount of the flocculant particles to be returned
- the stirring conditions in the fine flocculation step such as the stirring time and the degree of stirring are set to the same conditions as in the case where the water to be treated is transferred to the coagulation sedimentation treatment step
- the water to be treated is passed through at a predetermined injection amount, it is used to measure the weight per unit volume of particles in the flocking process in the water to be treated in the sludge / blanket tank.
- the concentration to be reduced with the lapse of time is adopted as an injection amount to be transferred to the coagulation sedimentation treatment of the water to be treated.
- the injection amount standard to adopt the injection amount by increasing and adjusting so as to become the above, the concentration of particles in the flocking process in the sludge blanket tank does not decrease over time
- the method of coagulating and precipitating water to be treated based on the transition to coagulating and precipitating treatment of water to be treated, (2)
- the conditions for executing the inorganic flocculant injection step that is, the type and amount of the inorganic flocculant, and the stirring conditions in the fine flocking step, such as the number of sections in which the stirring tank is provided, the stirring time, and the degree of stirring,
- the aluminum content ratio (Al / T) to the total weight of the inorganic coagulant is 0.05 in the previous stage
- the concentration based on the weight measurement per unit volume of the three components of the solidified solid of the water to be treated, the inorganic flocculant, and the flocculant particles returned from the sludge / blanket tank is 7.5 mg / L or more.
- a method for coagulating and precipitating water to be treated according to the above (1), characterized in that the amount of flocculant particles to be fed back is set. (3) Either of the above (1) and (2), wherein the precipitated flocked particles are transferred to a concentrator adjacent to the sludge / blanket tank and then returned to the flocked particles.
- the flocs in the sludge / blanket tank are realized in a stable state on the premise of the fine flocs by the rapid stirring tank.
- fine floc remaining in the clarified water is finer and denser than in the case of the prior art, so that high-quality clarified water can be obtained.
- particularly high-quality clarified water can be obtained when an upward flow inclined plate or an upward flow inclined pipe is installed in the vicinity of the upper outlet of the sludge / blanket tank.
- 2 is a graph showing temporal changes in turbidity (indicated by the number of flocked particles) of discharged precipitated water, and (a) shows a case where the diameter of the flocked particles is 0.5 to 1 ⁇ m. (B) shows the case where the diameter of the flocked particles is 7.0 ⁇ m or more.
- the basic configuration (1) includes an injection process of the inorganic flocculant 2, a fine flocking process through mixing and stirring by the stirrer 11 in the rapid stirring tank 10, and a sludge / blanket tank
- the basic steps are a flocculation step and a precipitation separation step through 5.
- the flocking process proceeds by the combination of fine flocks and / or the combination of fine flock particles or flock particles and existing flock particles.
- flocked particles having a predetermined particle size and weight are precipitated, and usually move to the sludge storage tank 9 via the concentrator 4, while the remaining particles separated without precipitation (floccing).
- the fine floc particles that remain without being broken, floc particles that have been flocked once but have been broken down into fragments, and floc particles that have a small particle size and weight, etc., together with the water to be treated 1 are subjected to the next sand filtration. (However, in most cases, before moving to the sand filtration tank, as shown in FIG. 1 and described in the embodiment, provided near the upper outlet of the sludge blanket tank 5. It goes through the upward flow inclined plate or the upward flow inclined pipe 8).
- the basic configuration (1) can obtain fine-grained and dense micro flocs by limiting the amount of inorganic flocculant injected and setting the degree of rapid stirring to a predetermined level or higher. is doing.
- the flocculent particles precipitated in the sludge / blanket tank 5 are returned to the previous stage of the fine flocking step, and the treated water 1 is injected simultaneously with or before and after the injection of the inorganic flocculant. Injecting.
- the amount of inorganic flocculant injected as pointed out in the background art section is limited, and the degree of rapid stirring is set to be large so that the fine floc particles become finer and denser.
- the decrease in the concentration of flocculated particles in the sludge blanket tank 5 is compensated.
- the weight per unit volume of the particles in the flocking process in the sludge / blanket tank 5 is measured. It is determined whether or not the concentration is reduced. If the concentration does not decrease, it is adopted as an injection amount to be transferred to the coagulation sedimentation treatment of the water 1 to be treated. If the concentration is decreased, the concentration does not decrease.
- the process proceeds to the coagulation precipitation treatment of the water 1 to be treated.
- conditions for executing the inorganic flocculant injection step (specifically, conditions regarding the type and amount of the inorganic flocculant) and stirring conditions (providing a stirring tank are provided).
- the conditions such as the number of compartments, the stirring time, the degree of stirring, etc.) are set to the same conditions as in the case of shifting to the original coagulation precipitation process.
- the step of returning the precipitated flocculated particles can be selected from the preceding, simultaneous and subsequent three steps with respect to the inorganic flocculant injection step. However, in order to exert the influence of the inorganic flocculant as much as possible, it is preferable to return at the same time as or after the inorganic flocculant injection step.
- the residual amount of the inorganic flocculant in the flocked particles that have settled in the sludge / blanket tank 5 and returned to the previous stage of the fine flocking process is considerably low.
- the return means that, for the fine flock flowing into the sludge / blanket tank 5 after all, the portion where the fine flock particles caused by suspended particles in the water to be treated 1 are not sufficient is complemented.
- the flocked particles settled in the sludge / blanket tank 5 are returned to the previous stage of the fine flocking process, and the injection amount based on the feedback is set in the sludge / blanket tank 5.
- the basic technical idea is to obtain the above effects.
- the concentrations of the three components by the suspended particles of the water 1 to be treated, the inorganic flocculant, and the returned flocked particles in the previous stage of the fine flocking step are respectively set.
- grains in the sludge blanket tank 5 at the time of 3.0 (mg / L), 5.0 (mg / L), and 7.5 (mg / L) is shown.
- the above-mentioned Al / T ratio of 0.05 corresponds to an extremely low numerical value (lower limit that can be adopted at an actual work site) as the amount of aluminum that can be adopted at a normal work site.
- Setting the R value to 150 sec ⁇ 1 and the rapid stirring time to 7 minutes is attributed to the setting of considerably high stirring conditions. Under such conditions, when the concentration of the above three components is 3.0 (mg / L) and 5.0 (mg / L), the flocification process in the sludge blanket tank 5 is performed. The concentration of certain particles gradually decreases with the passage of water passage time. On the other hand, when the concentration at the previous stage of the fine flocking process is 7.5 (mg / L), the concentration of the flocked particles in the sludge / blanket tank 5 is kept substantially constant.
- FIG. 3 shows the same conditions as in the experiment of FIG. 2, and the concentrations of the three components are 3.0 (mg / L), 5.0 (mg / L), and 7.5 (mg / L), respectively.
- the sludge / blanket tank 5 shows the state of change of the number of particles with the passing time of the precipitated water 3 flowing out in a state where the floc particles are purified and separated is shown ( a) shows the case of particles having a diameter of 0.5 to 1 ⁇ m, and (b) shows the number of particles having a diameter of 7.0 ⁇ m or more.
- the concentration of the three components is not less than a predetermined concentration of 7.5 (mg / L) or more, as shown in FIGS. 3 (a) and 3 (b), the number (concentration) of each particle in the precipitated water 3
- the reason for the decrease in flocs is that the amount of fine flocs particles flowing into the sludge / blanket tank 5 increases because the return amount of flocs particles is large, and the degree of flocking is maintained.
- the degree of destruction of the flocked particles is small by maintaining the degree of residual fine floc particles and the adhesion of the inorganic flocculant remaining in the fine floc particles (conversely, 3
- the concentration of the component is 3.0 (mg / L) and 5.0 (mg / L)
- the degree of flocking is insufficient, so the adhesive strength of the inorganic flocculant remaining in the fine flock is sufficient Flock because it is not maintained
- the extent of damage to the particles also can be considered large.).
- the basic configuration (2) is characterized by injecting an inorganic flocculant having an aluminum content ratio (Al / T) of 0.05 or less with respect to the total weight of the inorganic flocculant.
- Al / T aluminum content ratio
- the content of aluminum in the entire water to be treated depends on the concentration of the injected inorganic flocculant, but in the case of the content ratio (Al / T), the concentration is a normal inorganic flocculant injection.
- the basic configuration (3) according to claim 3 performs the feedback after transferring the precipitated flocked particles to the concentrator 4, but in most of the embodiments, the basic configuration (3 ) Is adopted. However, it is originally possible to return the flocked particles precipitated directly from the sludge storage tank 9 instead of the concentrator 4.
- the stirring time in the first rapid stirring tank 10 is t 1 and the stirring time in the second rapid stirring tank 10 is t 2.
- N 1 Aexp ( ⁇ kt 1 ) in the first rapid stirring tank 10
- N 1 + 2 Aexp ( ⁇ kt 1 ⁇ kt 2 )
- N 1 + 2 is a numerical value smaller than N 1 , indicating that the degree of aggregation is further progressing.
- N 1 + 2 is a numerical value smaller than N 1 , indicating that the degree of aggregation is further progressing.
- the embodiment according to claim 5 is not an STR based on the strict definition as described above, but sufficiently adjusts the degree of use of the inorganic flocculant according to the basic configuration with the STR as described in claim 5. (Limited) can be performed.
- the fine flocs are fine and densified. For example, it is possible to grow to a floc of 30 ⁇ m or more while reflecting and maintaining the properties. Such flocs are smaller in diameter than flocs formed by injecting a large amount of an inorganic flocculant as in the prior art, but they have a high sedimentation speed because of their high density.
- an upward flow inclined plate or an upward flow inclined tube 9 when an upward flow inclined plate or an upward flow inclined tube 9 is provided, fine floc particles can be efficiently separated. it can.
- micro flocculation step is divided into two or more compartments, G R value (stirring coefficient and C as rapidly stirred intensity in each compartment, the area of the stirring blade A (m 2 ), The peripheral speed of the stirring blade is v (m / sec), the kinematic viscosity coefficient is ⁇ (m 2 / sec), and the volume (capacity) of the stirring tank is V (m 3 ), Numerical) represented by, per, select a unit of sec -1, rapid stirring per time at which T R values, if you select the unit of sec, G R ⁇ T R value is both the product is 30,000 It is characterized by being.
- the embodiment is characterized in that an upward flow inclined plate or an upward flow inclined pipe 8 is installed in the vicinity of the upper outlet in the sludge blanket tank 5 as in the invention of claim 8.
- the installation state is as shown in FIG.
- the G R value is set to 1250 sec ⁇ 1 and the T R value is set to 7.3 minutes for each of the three sections of the rapid stirring tank 10, and the basic configuration (1 ), (2), (3), and by setting the concentration of the above three components to 7.5 (mg / L) in the previous stage of the fine flocking process, as shown in the graph of FIG. -The density
- FIG. 4 (a) shows the comparison result of turbidity (mg / L) in the treated water 1 that has been purified and separated and transferred to the next sand filtration step.
- the turbidity when present was 0.040 (mg / L), whereas the turbidity when not present was 0.211 (mg / L), and a marked difference was observed.
- FIG. 4B shows the contrast of the flocculated particles that have been purified and separated corresponding to the respective particle size classifications, and the removal rate (corresponding to the respective particle size classifications when the upward flow inclined plate 8 is employed).
- the number of particles is used as a unit.
- the present invention can be used in all fields of sewage and sludge treatment industries using inorganic flocculants.
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Abstract
Description
凝集沈澱装置は、コンベンショナル方式と高速凝集沈澱池方式とに大別され、後者は更に、スラリー循環方式、スラッジ・ブランケット方式に分類されており、本願発明は、後者を選択している。
但し、いずれの方式も、懸濁粒子の微フロック化工程と微フロックのフロック化工程とを経て沈澱分離されることに変りはない。 The flocculation and precipitation treatment of the water to be treated is employed as a pretreatment for sand filtration. In the flocculation and precipitation method, an inorganic flocculant is injected into the water to be treated, and fine suspended particles contained in the water to be treated. Are aggregated into flocs having a diameter capable of being separated by precipitation, and the flocs are separated by precipitation by the action of gravity.
The coagulation sedimentation apparatus is roughly classified into a conventional system and a high-speed coagulation sedimentation basin system. The latter is further classified into a slurry circulation system and a sludge blanket system, and the present invention selects the latter.
However, in any of the methods, the precipitate is separated through the fine flocking step of the suspended particles and the fine flocking step.
dN/dt=-α(4GΦ/π)・N ・・・・・・(a)
(N:単位体積当たりの粒子(微フロック又はフロック)の個数
α:無機凝集剤の影響に基づく衝突効率
G:速度勾配、Φ:単位体積における粒子(微フロック又はフロック)の平均容積)
前記初等微分方程式の一般解は、N=Aexp(-kt) と表現することができる(但し、Aは、t=0の段階における単位体積当たりの粒子(微フロック又はフロック)の個数であり、k=α(4GΦ/π)である。)。
前記スモルコウスキー方程式に立脚したうえで、従来技術においては、無機凝集剤注入率の上昇に強く依存した運転法が採用されたことがあるが、その根拠は、無機凝集剤の注入率を大きく設定することによって、前記(a)式の衝突効率αの数値を大きくし、微フロックを基準とした場合のdN/dtの減少率を高め、フロック化を促進しようという点にある。 The current coagulation-precipitation treatment method is based on the following general formula shown by Smolkovsky.
dN / dt = -α (4GΦ / π) · N (a)
(N: number of particles (fine flock or flock) per unit volume α: collision efficiency based on influence of inorganic flocculant G: velocity gradient, Φ: average volume of particles (fine flock or flock) in unit volume)
The general solution of the elementary differential equation can be expressed as N = Aexp (−kt) (where A is the number of particles per unit volume (fine flock or flock) at the stage of t = 0, k = α (4GΦ / π)).
Based on the Smolkovsky equation, in the prior art, an operation method that relied heavily on the increase in the injection rate of the inorganic flocculant has been adopted. By setting the value, the numerical value of the collision efficiency α in the equation (a) is increased, the decrease rate of dN / dt when the fine flock is used as a reference, and the flocking is promoted.
このような状況に鑑み、特願2009-504161出願の発明(以下「先願発明」と略称する。)においては、無機凝集剤の使用量を従来技術の場合よりも限定したうえで、攪拌強度の増強などによって残留する微フロック及びフロックの高密度化及び微小化を実現化する一方、上記フロックの微小化によって、砂ろ過槽のろ過機能の低下を防ぐために、沈澱池内においてピッチの狭い傾斜板を採用し、微フロックを効率的に分離する構成を提唱し、前記構成については、既に特許登録が行われている(特許第4316671号)。 However, in the case of the above configuration provided by
In view of such a situation, in the invention of Japanese Patent Application No. 2009-504161 (hereinafter abbreviated as “prior application invention”), the amount of the inorganic flocculant used is limited as compared with the prior art, and the stirring strength In order to prevent the remaining flocs and flocs from becoming denser and finer by increasing the size of the flocs, etc., in order to prevent the filtration function of the sand filtration tank from being deteriorated by the above-mentioned miniaturization of flocs, an inclined plate with a narrow pitch in the sedimentation pond And proposed a structure for efficiently separating fine flocs, and patent registration has already been made for the structure (Japanese Patent No. 4316671).
しかしながら、前記のように、細粒・高密な微フロックがフロック化した場合には、当該フロック化粒子もまた高密度であるため、スラッジ・ブランケット槽内において速やかに沈澱する。
このような場合、スラッジ・ブランケット槽に流入してくる微フロックの濃度が所定量以下である場合には、上記のように速やかに沈澱するフロック化粒子を補充することができないことを原因としてスラッジ・ブランケット槽内のフロックの濃度は、順次減少する。 When the amount of the inorganic flocculant injected is limited and the stirring strength of the rapid stirring tank is set to a predetermined level or more as in the invention of the prior application, the fine flocs are inevitably formed. Flocculates by aggregating with each other in the sludge blanket tank, and further adsorbs the fine flocs that subsequently flow in, thereby further promoting the flocking.
However, as described above, when fine-grained, high-density fine flocs are flocculated, the flocculated particles are also dense, and thus quickly settle in the sludge / blanket tank.
In such a case, if the concentration of fine floc flowing into the sludge / blanket tank is below a predetermined amount, the sludge is caused by the fact that it is impossible to replenish the flocked particles that quickly settle as described above.・ The concentration of floc in the blanket tank will gradually decrease.
によって表わされる数値)を、1500sec-1と設定したうえで、懸濁粒子を含む被処理水に代えて、清澄水中にカオリン(白陶土であって、清澄水の懸濁の程度を実現する疑似懸濁粒子の集合体)を1mg/Lの濃度となるように注入すると共に、無機凝集剤であるポリ塩化アルミニウム(PAC)を5mg/Lの濃度となるように注入している。 FIG. 5 (a), the experimental conditions in micro flocculation step for realizing the data, G R value is rapid stirring intensity in one rapid agitation tank 10 (stirring coefficient is C, the stirring blade (b) The area is A (m 2 ), the peripheral speed of the stirring blade is v (m / sec), the kinematic viscosity coefficient is γ (m 2 / sec), and the volume (capacity) of the stirring tank is V (m 3 ). if you did this,
Is set to 1500 sec −1, and instead of the treated water containing suspended particles, kaolin (white porcelain clay in clarified water, which realizes the degree of suspension of clarified water) The aggregate of suspended particles) is injected to a concentration of 1 mg / L, and polyaluminum chloride (PAC) as an inorganic flocculant is injected to a concentration of 5 mg / L.
このような実験結果は、急速攪拌の進行と共に無機凝集剤の凝集能力が低下し、残留している無機凝集剤粒子が破壊され、粒子数が減少することを示しているが、このような減少の度合いは、急速攪拌槽の数が増えるに従って、更に顕著な状態となる。 According to FIGS. 5 (a) and 5 (b), under the experimental conditions as described above, the number of particles (particles / mL) having a particle size of 0.5 to 1 μm decreases as shown in (a). As shown in (b), the number (particles / mL) of particles having a particle size of 30 μm or more increases until the STR value reaches a predetermined value (specifically, 2 or less), but thereafter Is descending as in the case of (a).
These experimental results show that the aggregating ability of the inorganic flocculant decreases with the progress of rapid stirring, the remaining inorganic flocculant particles are destroyed, and the number of particles decreases. The degree of becomes more remarkable as the number of rapid stirring tanks increases.
即ち、前記のようにスラッジ・ブランケット槽に流入してくるフロック粒子の数が少ない場合には、スラッジ・ブランケット槽においては、所定数量の微フロック粒子の流入に基づいて生ずるフロック化工程の程度もまた減少せざるを得ない。
そして、このような結果は、スラッジ・ブランケット槽におけるフロック化を前提とする沈澱分離機能に支障が生ずることにならざるを得ない。 In the sludge / blanket tank, fine flocked particles are flocked. As described above, the small number of fine flock particles flowing in is that the N on the right side in the equation (a) is small, and thus dN This means that / dt is small, that is, the rate of change from fine flock to flock is small.
That is, when the number of floc particles flowing into the sludge / blanket tank is small as described above, the degree of the flocking process that occurs based on the flow of a predetermined amount of fine flock particles in the sludge / blanket tank Moreover, it must be reduced.
Such a result inevitably impedes the function of separating the precipitate on the premise of flocking in the sludge / blanket tank.
しかしながら、特許文献2の方法では、汚泥貯留槽から帰還しているフロック化粒子は、急速攪拌工程を経ていないため、凝集剤の残留に基づく凝集能力が極めて乏しく、スラッジ・ブランケット槽内において、細粒・高密な微フロックの形成を前提とするフロック化を期待することができない。 In Patent Document 2, the degree of the flocking step is maintained at a predetermined level by directly returning the flocked particles precipitated in the sludge / blanket tank and discharged to the sludge storage tank to the sludge / blanket tank. A method is disclosed.
However, in the method of Patent Document 2, the flocculent particles returning from the sludge storage tank have not undergone the rapid stirring process, and therefore the aggregating ability based on the residual coagulant is extremely poor. Flocking based on the formation of grains and dense micro flocs cannot be expected.
(1)被処理水に無機凝集剤を注入する無機凝集剤注入工程と、前記無機凝集剤が注入された前記被処理水を急速攪拌槽中にて混合攪拌して前記被処理水中の微細な懸濁粒子をあらかじめ微フロック化する微フロック化工程と、スラッジ・ブランケット槽内にて、流入した当該微フロック粒子同士の結合及び/又は微フロック粒子若しくはフロック粒子と既存のフロック粒子との結合に基づくフロック化工程、及び当該フロック化粒子を沈澱分離し、沈澱したフロック化粒子及び沈澱せずに分離したその余の粒子をそれぞれスラッジ・ブランケット槽の外部に排出する工程とを有する被処理水の凝集沈澱処理方法であって、無機凝集剤の凝集能力の低下を原因とするスラッジ・ブランケット槽内におけるフロック化に基づく沈澱分離機能に支障が生ずることを防止するために、前記沈澱したフロック化粒子を、微フロック化工程の前段階に帰還し、前記無機凝集剤の注入と同時又はその前後に被処理水に注入させている場合の当該帰還するフロック化粒子の注入量につき、被処理水の凝集沈澱処理を行う前段階に、無機凝集剤の種類及び注入量という無機凝集剤注入工程を実行する条件、及び攪拌槽を設ける区画数、攪拌時間、攪拌の程度という微フロック化工程における攪拌条件を、前記被処理水の凝集沈澱処理工程に移行した場合と同一条件に設定している予備実験において、前記帰還を行うフロック化粒子における所定の注入量の場合に、被処理水を通過させた際、スラッジ・ブランケット槽内における被処理水中のフロック化工程にある粒子の単位体積当たりの重量測定に基づく濃度が時間の経過と共に減少するか否かを判別し、減少しない場合には、被処理水の凝集沈澱処理に移行する注入量として採用し、減少する場合には、前記濃度が減少しない程度以上となるように増加して調整することによる注入量を採用するという注入量の基準を設定することによって、スラッジ・ブランケット槽内におけるフロック化工程にある粒子の前記濃度が時間の経過と共に減少しない状態としたうえで、被処理水の凝集沈澱処理に移行することに基づく被処理水の凝集沈澱処理方法、
(2)無機凝集剤の種類及び注入量という無機凝集剤注入工程を実行する条件、及び攪拌槽を設ける区画数、攪拌時間、攪拌の程度という微フロック化工程における攪拌条件を、前記被処理水の凝集沈澱処理工程に移行した場合と同一条件に設定している予備実験において、微フロック化工程の前段階において、無機凝集剤の全重量に対するアルミニウムの含有比率(Al/T)を0.05以下としたうえで被処理水の凝固固形物、無機凝集剤、スラッジ・ブランケット槽から帰還したフロック化粒子の3成分の単位体積当たりの重量測定に基づく濃度が7.5mg/L以上となるように帰還するフロック化粒子の注入量を設定することを特徴とする前記(1)に記載の被処理水の凝集沈澱処理方法、
(3)沈澱したフロック化粒子を、スラッジ・ブランケット槽に隣接しているコンセントレータに移行させたうえで、当該フロック化粒子を帰還させることを特徴とする前記(1)、(2)の何れかに記載の被処理水の凝集沈澱処理方法、
からなる。 In order to solve the above problems, the basic configuration according to
(1) An inorganic flocculant injecting step for injecting an inorganic flocculant into the water to be treated; and the water to be treated into which the inorganic flocculant has been injected are mixed and stirred in a rapid stirring tank to make fine particles in the water to be treated. In the fine flocking process in which suspended particles are finely flocked in advance, and in the sludge / blanket tank, the fine flock particles that have flowed in and / or the fine flock particles or flock particles and the existing flock particles are combined. Water to be treated, and a step of precipitating and separating the flocked particles, and discharging the precipitated flocked particles and the remaining particles separated without precipitation to the outside of the sludge / blanket tank, respectively. This is a coagulation-precipitation method, which supports the precipitation separation function based on flocking in a sludge / blanket tank caused by a decrease in the coagulation ability of inorganic coagulants. In order to prevent occurrence of water, the precipitated flocculated particles are returned to the previous stage of the fine flocculation step and injected into the water to be treated at the same time as or before and after the injection of the inorganic flocculant. Conditions for executing the inorganic flocculant injection step, that is, the type and amount of the inorganic flocculant, and the number of compartments in which the stirring tank is provided before the flocculation / precipitation treatment of the water to be treated with respect to the amount of the flocculant particles to be returned In the preliminary experiment in which the stirring conditions in the fine flocculation step such as the stirring time and the degree of stirring are set to the same conditions as in the case where the water to be treated is transferred to the coagulation sedimentation treatment step, When the water to be treated is passed through at a predetermined injection amount, it is used to measure the weight per unit volume of particles in the flocking process in the water to be treated in the sludge / blanket tank. It is determined whether or not the concentration to be reduced with the lapse of time. If not, it is adopted as an injection amount to be transferred to the coagulation sedimentation treatment of the water to be treated. By setting the injection amount standard to adopt the injection amount by increasing and adjusting so as to become the above, the concentration of particles in the flocking process in the sludge blanket tank does not decrease over time In a state, the method of coagulating and precipitating water to be treated based on the transition to coagulating and precipitating treatment of water to be treated,
(2) The conditions for executing the inorganic flocculant injection step, that is, the type and amount of the inorganic flocculant, and the stirring conditions in the fine flocking step, such as the number of sections in which the stirring tank is provided, the stirring time, and the degree of stirring, In the preliminary experiment set to the same conditions as in the case of shifting to the coagulation-precipitation treatment step, the aluminum content ratio (Al / T) to the total weight of the inorganic coagulant is 0.05 in the previous stage of the fine flocking step. The concentration based on the weight measurement per unit volume of the three components of the solidified solid of the water to be treated, the inorganic flocculant, and the flocculant particles returned from the sludge / blanket tank is 7.5 mg / L or more. A method for coagulating and precipitating water to be treated according to the above (1), characterized in that the amount of flocculant particles to be fed back is set.
(3) Either of the above (1) and (2), wherein the precipitated flocked particles are transferred to a concentrator adjacent to the sludge / blanket tank and then returned to the flocked particles. A coagulation-precipitation treatment method of water to be treated as described in
Consists of.
更には、実施例において後述するように、上向流傾斜板又は上向流傾斜管をスラッジ・ブランケット槽の上側出口付近に設置した場合には、特に良質な清澄水を得ることができる。 In the present invention according to the basic configurations (1), (2), and (3), the flocs in the sludge / blanket tank are realized in a stable state on the premise of the fine flocs by the rapid stirring tank. As a result, fine floc remaining in the clarified water is finer and denser than in the case of the prior art, so that high-quality clarified water can be obtained.
Furthermore, as will be described later in the examples, particularly high-quality clarified water can be obtained when an upward flow inclined plate or an upward flow inclined pipe is installed in the vicinity of the upper outlet of the sludge / blanket tank.
フロック化工程に伴い、所定の粒径及び重量を有するフロック化粒子は沈澱し、通常コンセントレータ4を経て、汚泥貯留槽9に移動する一方、沈澱せずに分離されたその余の粒子(フロック化せずに残留した微フロック粒子、一度フロック化するも、破壊されて細分化したフロック化粒子、更には粒径及び重量の小さいフロック化粒子等)は、被処理水1と共に、次の砂ろ過槽に移行することになる(但し、大抵の場合には、砂ろ過槽に移行する前に、図1に示し、かつ実施例において説明するように、スラッジ・ブランケット槽5の上側出口付近に設けられている上向流傾斜板又は上向流傾斜管8を経ることになる。)。 In the sludge /
In association with the flocking step, flocked particles having a predetermined particle size and weight are precipitated, and usually move to the
このような基本構成(1)においては、スラッジ・ブランケット槽5において沈澱したフロック化粒子を、微フロック化工程の前段階に帰還し、無機凝集剤の注入と同時又はその前後に被処理水1に注入している。 It is naturally planned that the basic configuration (1) can obtain fine-grained and dense micro flocs by limiting the amount of inorganic flocculant injected and setting the degree of rapid stirring to a predetermined level or higher. is doing.
In such a basic configuration (1), the flocculent particles precipitated in the sludge /
但し、前記帰還するフロック化粒子の注入量につき、事前の予備実験において、所定の帰還する注入量の場合に、スラッジ・ブランケット槽5内におけるフロック化工程にある粒子の単位体積当たりの重量測定に基づく濃度が減少するか否かを判別し、減少しない場合には、被処理水1の凝集沈澱処理に移行する注入量として採用し、減少する場合には、前記濃度が減少しない程度以上となるように増加して調整することによる注入量を採用するという注入量の基準を設定したうえで、被処理水1の凝集沈澱処理に移行している。 By such feedback and injection, the amount of inorganic flocculant injected as pointed out in the background art section is limited, and the degree of rapid stirring is set to be large so that the fine floc particles become finer and denser. In some cases, the decrease in the concentration of flocculated particles in the
However, for the injection amount of the flocked particles to be returned, in a preliminary experiment, in the case of a predetermined injection amount to be returned, the weight per unit volume of the particles in the flocking process in the sludge /
但し、無機凝集剤による影響をできるだけ発揮させるためには、無機凝集剤注入工程と同時又は後の段階にて帰還させることが好ましい。 The step of returning the precipitated flocculated particles can be selected from the preceding, simultaneous and subsequent three steps with respect to the inorganic flocculant injection step.
However, in order to exert the influence of the inorganic flocculant as much as possible, it is preferable to return at the same time as or after the inorganic flocculant injection step.
このような帰還したフロック化粒子が、無機凝集剤と共に、急速攪拌槽10において混合攪拌を受けた場合には、被処理水1中の懸濁粒子と同様に、改めて微フロック化し、再びスラッジ・ブランケット槽5内に流入することになる。
したがって、前記帰還は、結局、スラッジ・ブランケット槽5に流入する微フロックにつき、被処理水1中の懸濁粒子を原因とする微フロック粒子だけでは足りない部分を補完することを意味しており、微フロックを基準とした場合の前記(a)式において、右辺のNの数を増大させ、結局、dN/dtにおける微フロックの減少の程度をも増大させることによって、逆にフロック化が生ずる程度を増大させることに他ならない。 The residual amount of the inorganic flocculant in the flocked particles that have settled in the sludge /
When such returned flocculated particles are mixed and stirred in the
Therefore, the return means that, for the fine flock flowing into the sludge /
このような条件下において、前記の3成分による濃度が3.0(mg/L)の場合、及び5.0(mg/L)の場合には、スラッジ・ブランケット槽5内におけるフロック化工程にある粒子の濃度は、通水時間の経過と共に順次低下している。
これに対し、微フロック化工程の前段階における前記濃度が7.5(mg/L)の場合には、スラッジ・ブランケット槽5におけるフロック化粒子の濃度が概略一定に保たれている。 The above-mentioned Al / T ratio of 0.05 corresponds to an extremely low numerical value (lower limit that can be adopted at an actual work site) as the amount of aluminum that can be adopted at a normal work site. Setting the R value to 150 sec −1 and the rapid stirring time to 7 minutes is attributed to the setting of considerably high stirring conditions.
Under such conditions, when the concentration of the above three components is 3.0 (mg / L) and 5.0 (mg / L), the flocification process in the
On the other hand, when the concentration at the previous stage of the fine flocking process is 7.5 (mg / L), the concentration of the flocked particles in the sludge /
このような場合、基本構成(2)において、沈澱したフロックの帰還によって、スラッジ・ブランケット槽5内におけるフロック化機能を維持することが可能となることから、前記実施形態の数値限定は、極めて有用な基準を提供している。
尚、アルミニウムの被処理水全体における含有量は、注入された無機凝集剤による濃度によって左右されるが、前記含有比率(Al/T)の場合には、当該濃度は、通常の無機凝集剤注入の場合と同程度に設定することによって、前記のような高密度化した微フロックの形成を実現することができる。 The basic configuration (2) is characterized by injecting an inorganic flocculant having an aluminum content ratio (Al / T) of 0.05 or less with respect to the total weight of the inorganic flocculant. When the content ratio is set small, fine flocs with extremely high density are usually formed.
In such a case, in the basic configuration (2), it is possible to maintain the function of flocking in the sludge /
The content of aluminum in the entire water to be treated depends on the concentration of the injected inorganic flocculant, but in the case of the content ratio (Al / T), the concentration is a normal inorganic flocculant injection. By setting to the same level as in the above case, it is possible to realize the formation of fine flocs with a higher density as described above.
但し、コンセントレータ4ではなく、汚泥貯留槽9から直接沈澱したフロック化粒子の帰還を行うことは、本来可能である。 The basic configuration (3) according to claim 3 performs the feedback after transferring the precipitated flocked particles to the
However, it is originally possible to return the flocked particles precipitated directly from the
N1+2=Aexp(-kt1-kt2)
と表現でき、結局、N1+2は、N1よりも小さな数値となっており、凝集の程度が更に進行していることを示している。
そして、実際の作業現場では、被処理水1中における径が0.5~1μmの懸濁粒子の低減化に寄与することができる。 To explain in accordance with a general solution based on the Smolkowski equation, the stirring time in the first
N 1 + 2 = Aexp (−kt 1 −kt 2 )
After all, N 1 + 2 is a numerical value smaller than N 1 , indicating that the degree of aggregation is further progressing.
In an actual work site, it is possible to contribute to the reduction of suspended particles having a diameter of 0.5 to 1 μm in the
但し、請求項5に係る実施形態は、上記のような厳密な定義によるSTRではなく、請求項5記載通りのSTRを以って、十分前記基本構成に係る無機凝集剤の使用の程度の調整(限定)を行うことができる。 The embodiment according to
However, the embodiment according to
このようなフロックは、従来技術のように、多量の無機凝集剤を注入することによって形成されたフロックに比べると径は小さいものの、高密度化しているため、大きな沈降速度を有するので、沈澱池における沈澱分離に寄与することができ、更には実施例において後述するように、上向流傾斜板又は上向流傾斜管9を設けた場合には微フロック粒子の分離を効率的に行うことができる。 Then, as in the embodiment of
Such flocs are smaller in diameter than flocs formed by injecting a large amount of an inorganic flocculant as in the prior art, but they have a high sedimentation speed because of their high density. In addition, as will be described later in the embodiment, when an upward flow inclined plate or an upward flow inclined
によって表わされる数値)を、につき、sec-1の単位を選択し、急速攪拌時間であるTR値につき、secの単位を選択した場合、双方の積であるGR・TR値が30000以上であることを特徴としている。 The embodiment of
Numerical) represented by, per, select a unit of sec -1, rapid stirring per time at which T R values, if you select the unit of sec, G R · T R value is both the product is 30,000 It is characterized by being.
そして、前記のように、双方の積を30000以上と設定した場合には、前記高密度化を十分保証することができ、上記30000という数値は、極めて有用な基準を提供している。 Generally, in each compartment of performing rapid stirring, to increase the agitation intensity G R, yet by increasing the stirring time T R, can reduce the number of fine suspended particles, the density of fine flocks .
As described above, when the product of both is set to 30000 or more, the high density can be sufficiently ensured, and the numerical value of 30000 provides a very useful standard.
即ち、図4(a)は、浄化・分離され、次の砂ろ過工程に移行する被処理水1における濁度(mg/L)の対比結果を示すが、上向流傾斜板8を設けている場合の濁度は、0.040(mg/L)であるのに対し、設けていない場合の濁度は、0.211(mg/L)であり、顕著な相違が観察された。 In the vicinity of the outlet on the upper side of the sludge /
That is, FIG. 4 (a) shows the comparison result of turbidity (mg / L) in the treated
何れにせよ、上向流傾斜板又は上向流傾斜管8の設置によって、スラッジ・ブランケット槽5から流出するその余の粒子を分離することによって濁度を減少させ、沈澱分離を一層助長し、被処理水1を更に清澄化することができる。 FIG. 4B shows the contrast of the flocculated particles that have been purified and separated corresponding to the respective particle size classifications, and the removal rate (corresponding to the respective particle size classifications when the upward flow inclined plate 8 is employed). The number of particles is used as a unit.) As the particle size of the flocculated particles cleaned and separated without precipitation is larger, the effect of purification and separation of the upward flow inclined plate 8, that is, the particle size increases. It turns out that the effect of carrying out precipitation removal of the flocculent particle | grains which are carrying out is large.
In any case, the installation of the upward flow inclined plate or the upward flow inclined pipe 8 reduces the turbidity by separating the remaining particles flowing out of the sludge /
2 第1凝集剤注入工程における無機凝集剤(第1の無機凝集剤)の第1注入位置
3 沈澱水
4 コンセントレータ
5 スラッジ・ブランケット槽
6 スラッジ・ブランケット層
7 清澄ゾーン
8 上向流傾斜板又は上向流傾斜管
9 汚泥貯留槽
10 急速攪拌槽
11 急速攪拌機
101 急速攪拌槽の第1区画
102 急速攪拌槽の第2区画
103 急速攪拌槽の第3区画 DESCRIPTION OF
Claims (8)
- 被処理水に無機凝集剤を注入する無機凝集剤注入工程と、前記無機凝集剤が注入された前記被処理水を急速攪拌槽中にて混合攪拌して前記被処理水中の微細な懸濁粒子をあらかじめ微フロック化する微フロック化工程と、スラッジ・ブランケット槽内にて、流入した当該微フロック粒子同士の結合及び/又は微フロック粒子若しくはフロック粒子と既存のフロック粒子との結合に基づくフロック化工程、及び当該フロック化粒子を沈澱分離し、沈澱したフロック化粒子及び沈澱せずに分離したその余の粒子をそれぞれスラッジ・ブランケット槽の外部に排出する工程とを有する被処理水の凝集沈澱処理方法であって、無機凝集剤の凝集能力の低下を原因とするスラッジ・ブランケット槽内におけるフロック化に基づく沈澱分離機能に支障が生ずることを防止するために、前記沈澱したフロック化粒子を、微フロック化工程の前段階に帰還し、前記無機凝集剤の注入と同時又はその前後に被処理水に注入させている場合の当該帰還するフロック化粒子の注入量につき、被処理水の凝集沈澱処理を行う前段階に、無機凝集剤の種類及び注入量という無機凝集剤注入工程を実行する条件、及び攪拌槽を設ける区画数、攪拌時間、攪拌の程度という微フロック化工程における攪拌条件を、前記被処理水の凝集沈澱処理工程に移行した場合と同一条件に設定している予備実験において、前記帰還を行うフロック化粒子における所定の注入量の場合に、被処理水を通過させた際、スラッジ・ブランケット槽内における被処理水中のフロック化工程にある粒子の単位体積当たりの重量測定に基づく濃度が時間の経過と共に減少するか否かを判別し、減少しない場合には、被処理水の凝集沈澱処理に移行する注入量として採用し、減少する場合には、前記濃度が減少しない程度以上となるように増加して調整することによる注入量を採用するという注入量の基準を設定することによって、スラッジ・ブランケット槽内におけるフロック化工程にある粒子の前記濃度が時間の経過と共に減少しない状態としたうえで、被処理水の凝集沈澱処理に移行することに基づく被処理水の凝集沈澱処理方法。 Inorganic flocculant injection step of injecting an inorganic flocculant into the water to be treated, and the treated water into which the inorganic flocculant has been injected are mixed and stirred in a rapid agitation tank, and fine suspended particles in the water to be treated In the sludge / blanket tank and / or in the sludge / blanket tank based on the combination of the fine floc particles that flowed in and / or the combination of the fine flock particles or floc particles with existing floc particles Coagulating and precipitating treatment of the water to be treated having a step of precipitating and separating the flocculated particles, and discharging the precipitated flocculated particles and the remaining particles not precipitated to the outside of the sludge / blanket tank, respectively. This method interferes with the precipitate separation function based on flocking in the sludge / blanket tank due to the decrease in the flocculating ability of the inorganic flocculant. In order to prevent slipping, the precipitated flocculent particles are returned to the previous stage of the fine flocculation step, and the water is injected into the water to be treated at the same time as or before or after the injection of the inorganic flocculant. Conditions for executing the inorganic flocculant injection step of the type and amount of the inorganic flocculant, and the number of compartments where the stirring tank is provided, before the flocculation and precipitation treatment of the water to be treated for the amount of flocculant particles to be returned In a preliminary experiment in which the stirring conditions in the fine flocculation step such as the stirring time and the degree of stirring are set to the same conditions as in the case of shifting to the coagulation and precipitation treatment step of the water to be treated, predetermined in the flocked particles performing the feedback When the water to be treated is allowed to pass through, the amount of particles per unit volume in the flocculation process in the water to be treated in the sludge / blanket tank is measured. It is determined whether or not the concentration decreases with the passage of time. If the concentration does not decrease, it is adopted as an injection amount to be transferred to the coagulation / precipitation treatment of the water to be treated. By setting the injection amount standard to adopt the injection amount by increasing and adjusting so that the concentration of particles in the flocating process in the sludge blanket tank does not decrease over time In addition, a method for coagulating and precipitating water to be treated based on the transition to coagulating and precipitating treatment of water to be treated.
- 無機凝集剤の種類及び注入量という無機凝集剤注入工程を実行する条件、及び攪拌槽を設ける区画数、攪拌時間、攪拌の程度という微フロック化工程における攪拌条件を、前記被処理水の凝集沈澱処理工程に移行した場合と同一条件に設定している予備実験において、微フロック化工程の前段階において、無機凝集剤の全重量に対するアルミニウムの含有比率(Al/T)を0.05以下としたうえで被処理水の凝固固形物、無機凝集剤、スラッジ・ブランケット槽から帰還したフロック化粒子の3成分の単位体積当たりの重量測定に基づく濃度が7.5mg/L以上となるように帰還するフロック化粒子の注入量を設定することを特徴とする請求項1に記載の被処理水の凝集沈澱処理方法。 The conditions for executing the inorganic flocculant injection step, which are the type and amount of the inorganic flocculant, and the stirring conditions in the fine flocking step, such as the number of sections in which the stirring tank is provided, the stirring time, and the degree of stirring, In the preliminary experiment set to the same conditions as when the process was shifted to the treatment process, the aluminum content ratio (Al / T) with respect to the total weight of the inorganic flocculant was set to 0.05 or less in the previous stage of the fine flocking process. The solids of the water to be treated, the inorganic flocculant, and the flocked particles returned from the sludge / blanket tank are fed back so that the concentration based on the weight measurement per unit volume of the three components is 7.5 mg / L or more. The method for coagulating and precipitating water to be treated according to claim 1, wherein an injection amount of the flocked particles is set.
- 沈澱したフロック化粒子を、スラッジ・ブランケット槽に隣接しているコンセントレータに移行させたうえで、当該フロック化粒子を帰還させることを特徴とする請求項1、2の何れか1項に記載の被処理水の凝集沈澱処理方法。 The covered flocculated particles are transferred to a concentrator adjacent to the sludge / blanket tank, and then the flocculated particles are returned. A method of coagulating and precipitating treatment water
- 微フロック化工程が、2以上の区画に分割された急速攪拌槽を被処理水が順次移行し得るような直列に接続した状態にて備えていることを特徴とする請求項1、2、3の何れか1項に記載の被処理水の凝集沈澱処理方法。 The fine flocking step is provided with a rapid stirring tank divided into two or more sections in a state of being connected in series so that the water to be treated can be sequentially transferred. The coagulation sedimentation processing method of to-be-processed water of any one of these.
- 凝集集塊物残留量を示す指標として、微フロック化工程が終了した段階における被処理水のSTR(Suction Time Ratio:被処理水と同温・等量の蒸留水を、同一の吸引の程度によって同一のろ紙を吸引させた場合に、被処理水の吸引時間をTsとし、蒸留水の吸引時間をTvとした場合、Ts/Tvによって表現される指標による比率)が2.5以下であることを特徴とする請求項1、2、3、4の何れか1項に記載の被処理水の凝集沈澱処理方法。 STR (Suction Time Ratio: distilled water of the same temperature and equal amount as the treated water, at the same level of suction, as an indicator of the residual amount of agglomerated agglomerates When the same filter paper is sucked, when the suction time of treated water is Ts and the suction time of distilled water is Tv, the ratio by the index expressed by Ts / Tv) is 2.5 or less. The method for coagulating and precipitating water to be treated according to any one of claims 1, 2, 3, and 4.
- 微フロック化工程の各区画における急速攪拌強度であるGR値(攪拌係数をCとし、攪拌翼の面積をA(m2)とし、攪拌翼の周辺速度をv(m/sec)とし、動粘性係数をγ(m2/sec)とし、攪拌槽の体積(容量)をV(m3)とした場合、
によって表わされる数値)につき、sec-1の単位を選択し、急速攪拌時間であるTR値につき、secの単位を選択した場合、双方の積であるGR・TR値が30000以上であることを特徴とする請求項1、2、3、4、5の何れか1項に記載の被処理水の凝集沈澱処理方法。 G R value is rapid stirring intensity in each compartment of the fine flocculation step (stirring coefficient is C, the area of the stirring blade and A (m 2), the peripheral speed of the stirring blade v and (m / sec), the dynamic When the viscosity coefficient is γ (m 2 / sec) and the volume (capacity) of the stirring tank is V (m 3 ),
For values) represented by, select the unit of sec -1, per T R value is rapid stirring time, if you select the unit of sec, G R · T R value is both the product is 30,000 or more The method for coagulating and precipitating water to be treated according to any one of claims 1, 2, 3, 4, and 5. - 急速攪拌強度GR値を150sec-1以上とし、急速攪拌時間TR値を180秒(3分)以上に設定することを特徴とする請求項6記載の被処理水の凝集沈澱処理方法。 The rapid agitation intensity G R value and 150 sec -1 or more, rapid stirring time T R value of 180 seconds (3 minutes) setting coagulating sedimentation processing method of the water to be treated according to claim 6, characterized in that above.
- スラッジ・ブランケット槽内の上側出口付近に、上向流傾斜板又は上向流傾斜管を設置していることを特徴とする請求項1、2、3、4、5、6、7の何れか1項に記載の被処理水の凝集沈澱処理方法。 The upflow-flow inclined plate or the upflow-flow inclined pipe is installed in the sludge blanket tank near the upper outlet, according to any one of claims 1, 2, 3, 4, 5, 6, and 7. The method for coagulating and precipitating water to be treated according to Item 1.
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JP6752113B2 (en) * | 2016-11-04 | 2020-09-09 | オルガノ株式会社 | Operation method of sludge blanket type coagulation sedimentation device and sludge blanket type coagulation sedimentation device |
CN108033528A (en) * | 2017-12-14 | 2018-05-15 | 大连百达开成不动产咨询有限公司 | Flocculant agitator tank |
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Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS4978362A (en) * | 1972-12-05 | 1974-07-29 | ||
JPS6220606U (en) * | 1985-07-22 | 1987-02-07 | ||
JPH11244868A (en) * | 1998-03-05 | 1999-09-14 | Nkk Corp | Coagulating sedimentation apparatus for sewage |
JP2006000715A (en) * | 2004-06-15 | 2006-01-05 | Japan Organo Co Ltd | Equipment and method for flocculation precipitation treatment |
JP2007203133A (en) * | 2006-01-31 | 2007-08-16 | Toshiaki Ochiai | Coagulation treatment method and its treatment apparatus for nonprocessed water |
JP2009045532A (en) * | 2007-08-16 | 2009-03-05 | Toshiaki Ochiai | Coagulating sedimentation method and apparatus |
JP4316671B2 (en) * | 2007-08-17 | 2009-08-19 | 壽昭 落合 | Coagulation precipitation treatment method |
JP4336754B1 (en) * | 2009-03-05 | 2009-09-30 | 壽昭 落合 | Aggregation method |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2930594B2 (en) * | 1988-12-06 | 1999-08-03 | オルガノ株式会社 | Coagulation settling equipment |
JPH02261505A (en) * | 1989-03-31 | 1990-10-24 | Ebara Infilco Co Ltd | Method for controlling chemical injection in flocculating and settling device |
JPH0978362A (en) * | 1995-09-11 | 1997-03-25 | Howa Mach Ltd | Calender roller apparatus |
JPH11244870A (en) * | 1998-03-05 | 1999-09-14 | Nkk Corp | Flocculating and settling device for sewage and cleaning method thereof |
JP3429694B2 (en) * | 1998-12-21 | 2003-07-22 | 住友重機械工業株式会社 | Coagulation sedimentation apparatus and blanket interface control method |
JP3429693B2 (en) * | 1998-12-21 | 2003-07-22 | 住友重機械工業株式会社 | Coagulation sedimentation apparatus and blanket interface control method |
CN101417847A (en) * | 2007-10-23 | 2009-04-29 | 栗田工业株式会社 | Domestic living waste water treater |
JP5173538B2 (en) * | 2008-04-03 | 2013-04-03 | 水ing株式会社 | Water treatment method |
-
2009
- 2009-09-08 JP JP2009206968A patent/JP4516152B1/en not_active Expired - Fee Related
-
2010
- 2010-06-10 CN CN2010800024307A patent/CN102176952B/en not_active Expired - Fee Related
- 2010-06-10 WO PCT/JP2010/003867 patent/WO2011030485A1/en active Application Filing
- 2010-06-10 KR KR1020127003294A patent/KR20120033349A/en not_active Application Discontinuation
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS4978362A (en) * | 1972-12-05 | 1974-07-29 | ||
JPS6220606U (en) * | 1985-07-22 | 1987-02-07 | ||
JPH11244868A (en) * | 1998-03-05 | 1999-09-14 | Nkk Corp | Coagulating sedimentation apparatus for sewage |
JP2006000715A (en) * | 2004-06-15 | 2006-01-05 | Japan Organo Co Ltd | Equipment and method for flocculation precipitation treatment |
JP2007203133A (en) * | 2006-01-31 | 2007-08-16 | Toshiaki Ochiai | Coagulation treatment method and its treatment apparatus for nonprocessed water |
JP2009045532A (en) * | 2007-08-16 | 2009-03-05 | Toshiaki Ochiai | Coagulating sedimentation method and apparatus |
JP4316671B2 (en) * | 2007-08-17 | 2009-08-19 | 壽昭 落合 | Coagulation precipitation treatment method |
JP4336754B1 (en) * | 2009-03-05 | 2009-09-30 | 壽昭 落合 | Aggregation method |
Non-Patent Citations (2)
Title |
---|
KUNIO EBIE ET AL: "(4-3) Gyoshushori ni Okeru Kyusoku Kakuhan no Yakuwari ni Kansuru Kisoteki Kento", DAI 57 KAI ZENKOKU SUIDO KENKYU HAPPYOKAI KOENSHU, JAPAN WATER WORKS ASSOCIATION, 25 April 2006 (2006-04-25), pages 142 - 143 * |
KUNIO EBIE ET AL: "(4-8) Kyusoku Kakuhan Tekiseika Gijutsu no Tekiyo ni yoru Shoki Ryushi Kosu Node no Teikaho no Kento", DAI 57 KAI ZENKOKU SUIDO KENKYU HAPPYOKAI KOENSHU, JAPAN WATER WORKS ASSOCIATION, 25 April 2006 (2006-04-25), pages 152 - 153 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP6145240B1 (en) * | 2017-04-17 | 2017-06-07 | 壽昭 落合 | Coagulation precipitation treatment method |
WO2018193794A1 (en) * | 2017-04-17 | 2018-10-25 | 落合壽昭 | Treatment method for condensed sludge |
JP2018176086A (en) * | 2017-04-17 | 2018-11-15 | 壽昭 落合 | Flocculation precipitation treatment method |
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