JP2012239950A - Water cleaning system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a water cleaning system which can normalize water by separating even strongly toxic contaminants and various radioactive substances from the water and prevents workers from contacting slurry etc., separated from the water.SOLUTION: The water cleaning system includes mechanisms (4A and 4B; 5A and 5B) which supply an ion exchange reaction agent to contaminated water and mix them, mechanisms (7A and 7B; 8A and 8B) which supply an adsorbing flocculating agent to the water added with the ion exchange reaction agent and mix them, a separating mechanism (flocculation separation tank 10) which separates the water mixed with the adsorbing flocculating agent into a supernatant and a precipitate, first dehydrator (13A and 13B) which separate the water from the supernatant separated by the separating mechanism (10), and second dehydrator (17A-17H) which separate the water from the precipitant (slurry) separated by the separating mechanism (10).

Description

  The present invention relates to a technique for removing and purifying contaminants from water containing contaminants (including radioactive cesium and the like).

Conventionally, various techniques have been proposed as such techniques. For example, there is a technique that combines microbial treatment and ozone treatment (see Patent Document 1).
However, in recent years, there are a wide variety of types of pollutants, and pollutants that cannot be treated by microbial treatment (for example, very toxic pollutants and various radioactive substances) contaminate water. A case has occurred.

Moreover, in the prior art, the treated sludge, slurry, and the like are often handled manually by an operator.
However, in the case of highly toxic pollutants (including radioactive substances), high-purity pollutants are present in the slurry after being separated from water, so it is very dangerous to process manually. It is.
Accordingly, there is a demand for a water purification system that can avoid the danger of workers coming into contact with the slurry after being separated from water.

JP 2009-28683 A

  The present invention has been proposed in view of the above-described problems of the prior art, and even highly toxic pollutants and various radioactive substances can be separated from water to normalize the water. And it aims at provision of the water purification system which does not have a possibility that a worker may contact the slurry etc. after the separation process from water.

  The water purification system of the present invention is a mechanism (4A, 4B) for supplying and mixing ion exchange reactants (for example, iron ferrocyanide, nickel ferrocyanide, cobalt ferrocyanide, zeolite, etc.) to contaminated water. 5A, 5B), a mechanism (7A, 7B; 8A, 8B) for supplying and mixing the adsorbing flocculant to the water charged with the ion exchange reactant, and the water mixed with the adsorbing flocculant as a supernatant A separation mechanism (aggregation separation tank 10) for separating into precipitates, a first dehydrator (13A, 13B) for separating water from the supernatant separated by the separation mechanism (10), and a separation mechanism (10). A second dehydrator (17A to 17H) for separating water from the separated precipitate (slurry) is provided.

In the present invention, the first dehydrating device (13A, 13B) has a plurality of filtration members (for example, bag filters), and the plurality of filtration members and their piping are supplied with the supernatant from the separation mechanism (10). It has a function of exchanging the supplied filtration member, and the downstream side of the filtration member communicates with the transport pump (14),
It is preferable that a pressure measuring device (pressure gauge) is interposed in a piping system that communicates the separation mechanism (10) and the first dehydrating device (13A, 13B).

In the present invention, the second dehydrator (17A to 17H) has a plurality of filtration members (for example, bag filters), and the plurality of filtration members and their piping are separated from the precipitate (10) ( The slurry is supplied to the filter member, the downstream side of the filter member is connected to the vacuum pump (18),
It is preferable that a pressure measuring device (pressure gauge) is interposed in a piping system that communicates the separation mechanism (10) and the second dehydrating device (17A to 17H).

  Here, a compression device (compressor 20) is provided, and the compressed air discharge port of the compression device (20) is filtered by the first dehydration devices (13A, 13B) and the second dehydration devices (17A-17H). It is preferable to communicate with the upstream side of the member (opposite side of the transfer pump 12 or the vacuum pump 16).

  Furthermore, in the present invention, if the pollutant is a radioactive material, a solidifying agent is supplied to the precipitate (slurry) separated by the separation mechanism (10) instead of the second dehydrator (17A to 17H) and mixed. It is preferable to provide a solidifying agent mixing device (52) for the purpose.

According to the present invention having the above-described configuration, the mechanism (4A, 4B; 5A, 5B) for supplying and mixing the ion exchange reactant to the contaminated water is provided. If the ion exchange reactant supplied in the water contaminated by 5A, 5B) is, for example, iron ferrocyanide, nickel ferrocyanide, cobalt ferrocyanide, the ion exchange reactant adsorbs harmful pollutants. Then, a harmless substance (for example, iron, nickel, cobalt, etc.) is released into water (the pollutant is replaced with a harmless substance).
For example, if the pollutant is cesium (which is a radioactive substance) and iron ferrocyanide is used as the ion exchange reagent, the ferric ferrocyanide adsorbs and adsorbs cesium in the contaminated water. Instead of cesium, iron is released into the water.
Moreover, if it is a zeolite, it will adsorb pollutants in water.

The ion exchange reactant adsorbing the pollutant is in a state where the pollutant (for example, cesium) is adsorbed by the adsorbing flocculant supplied from the mechanism (7A, 7B; 8A, 8B) for supplying and mixing the adsorbing flocculant. Aggregate as it is. If such agglomerates and water are separated, the contaminated water can be purified.
Such water can be returned to the storage area where the contaminated water is stored, based on the type, concentration, and criteria of the contaminant, supplied to other normalization devices such as reverse osmosis membrane devices, It can be discharged into rivers and lakes.

Therefore, according to the present invention, the water containing the aggregate of the ion exchange reactant adsorbing the contaminant is separated into the supernatant and the precipitate by the separation mechanism (aggregation separation tank 10).
Here, the supernatant liquid separated by the separation mechanism (aggregation separation tank 10) may contain a contaminant having a low specific gravity. According to the present invention, the foreign matter having a low specific gravity is removed from the supernatant by the first dehydrator (13A, 13B).
Here, the first dehydrator (13A, 13B) has, for example, a plurality of filtering members (for example, bag filters), and separates the water purified by the filtering members.
Moreover, the water contained in the precipitate separated by the separation mechanism (flocculation separation tank 10) is separated by the second dehydration apparatus (17A to 17H). As a result, the water content of the precipitate containing the pollutant is reduced, and disposal or disposal is efficiently performed. At the same time, contaminants are removed from the water contained in the precipitate and cleaned.

In the present invention, if the first dehydrator (13A, 13B) has a plurality of filtration members (for example, bag filters), when separating contaminants having a low specific gravity from the supernatant by the filtration members, When the filter member is so-called “clogged”, the filtration ability or the ability to separate clean water is reduced.
On the other hand, if a pressure measuring device (pressure gauge) is interposed in the piping system that communicates the separation mechanism (10) and the first dehydrating device (13A, 13B), the filtering member will be attracted by pollutants with low specific gravity. When clogged, the pressure value measured by the pressure measuring device rises, so that it is possible to grasp that the filtration capacity of the filtration member is reaching its limit.
Then, if the plurality of filtration members and their pipes are configured so as to replace the filtration member to which the supernatant from the separation mechanism (10) is supplied, the filtration fluid is reaching the limit from the filtration member. By switching to a filtration member that has not been filtered, the filtration capacity of the first dehydrator (13A, 13B) is restored.

  Here, it is possible to automate the switching of the filtering member and the operation of discharging the filtering member whose filtering ability is lost from the first dehydrator (13A, 13B), and the operator adheres to the filtering member. There is no direct contact with the contaminated contaminants (contaminants mixed in the supernatant liquid separated by the separation mechanism 10), and there is no risk of contamination or the like (if the contaminant is a radioactive substance, exposure).

In the present invention, the second dehydrator (17A to 17H) has a plurality of filtering members (for example, bag filters), and the separation mechanism (10) and the second dehydrator (17A to 17H) communicate with each other. If the pressure measuring device (PG2A, PG2B) is interposed in the piping system to be clogged, if the filtration member in the second dehydrating device (17A-17H) is clogged, the pressure measuring device (PG2A, Since the pressure value measured by PG2B) increases, it can be grasped that the filtration capacity of the filtration member is reaching the limit.
In such a case, if the plurality of filtration members and the piping thereof are configured to replace the filtration member to which the precipitate (slurry) from the separation mechanism (10) is supplied, the filtration capacity is reaching the limit. By switching from the member to an unused filtration member, the filtration capacity in the second dehydrator (17A to 17H) can be recovered.

In the second dehydrator (17A to 17H), if the downstream side of the filtration member is connected to the vacuum pump (18A, 18B), the water in the precipitate (slurry) separated by the separation mechanism (10) Since the vacuum pump (18A, 18B) is evacuated from the downstream side of the filter member, the ability to separate water from the precipitate is improved.
Also in the second dehydrating apparatus (17A to 17H), it is possible to automate the switching of the filtering member and the operation of discharging the filtering member whose filtering ability is lost, and the operator can contaminate the filtering member. There is no need to directly contact the substance (contaminant mixed in the precipitate separated by the separation mechanism 10).
Therefore, maintenance of the second dehydrating device (17A to 17H) (for example, replacement of the filtering member) is performed in a state where the safety of the worker is ensured, and contaminants are contained from the second dehydrating device (17A to 17H). The slurry to be discharged can be discharged.

  Moreover, in this invention, the compression apparatus (compressor 20) is provided, and the compressed air discharge port of a compression apparatus (20) is the 1st dehydration apparatus (13A, 13B) and the 2nd dehydration apparatus (17A-17H). For example, in the first dehydrating device (13A, 13B) and the second dehydrating device (17A to 17H), the filter is connected to the upstream side of the filter member (the opposite side of the transfer pump or the vacuum pump). When switching a filtering member (for example, a bag filter) that is performing an operation, the compressed liquid is supplied to the switched filtering member after finishing the filtering operation, so that the supernatant or slurry staying in the filtering member To increase the speed at which water permeates the filtration member, thereby improving the filtration capacity.

In the present invention, if the pollutant is a radioactive material, a solidifying agent mixing device (52) is provided in place of the second dehydrating device (17A to 17H) described above, and the solidifying agent mixing device (52) separates the separation mechanism. If the solidifying agent is supplied to and mixed with the precipitate (slurry) containing the radioactive substance separated in (10), the radioactive substance will be solidified in the designated container (54). It can be enclosed in a designated container (54) for disposal.
Therefore, the subsequent processing (radioactive material disposal processing) is performed safely and efficiently.

1 is a block diagram showing a first embodiment of the present invention. It is explanatory drawing of the filtration apparatus unit in 1st Embodiment. It is explanatory drawing which shows the principal part of the modification in 1st Embodiment. It is explanatory drawing of the concentrated mud vacuum filtration apparatus in 1st Embodiment. It is a block diagram which shows 2nd Embodiment of this invention.

Embodiments of the present invention will be described below with reference to the accompanying drawings.
First, a first embodiment will be described based on FIGS.
In FIG. 1, the water purification system according to the first embodiment denoted as a whole by reference numeral 101 includes a rough screen agitation adjustment tank 2, a first slurry pump 3, ion exchange reaction agitation tanks 4A and 4B, and adsorption aggregation. Reaction stirring tanks 7A and 7B are provided.
In addition, the water purification system 101 includes a flocculation / separation tank 10, a supernatant adjustment tank 11, a fourth slurry pump 12, supernatant filtration devices 13 </ b> A and 13 </ b> B, a transport pump 14, and a treated filtrate adjustment tank 15. I have.
Further, the water purification system 101 includes a concentrated mud slurry pump (for example, a tube pump) 16, concentrated mud vacuum filtration devices 17A to 17H (see FIG. 2), vacuum pumps 18A and 18B, filtered water and makeup water adjustment tank. 19A and 19B and an air compressor 20 are provided.

In FIG. 1, for example, contaminated water contaminated with radioactive substances or highly toxic substances stays in a contaminated water retention area 1 such as a watershed or pit.
The contaminated water staying in the contaminated water staying area 1 is taken up by the transport pump P1. The transport pump P1 is connected to the roughing screen agitation adjustment tank 2 via a line L1. An open / close valve V1 is interposed on the roughing screen stirring adjustment tank 2 side in the line L1.
A first slurry pump 3 is disposed on the discharge side of the roughing screen stirring adjustment tank 2. The first slurry pump 3 is connected to the first branch point B1 via the line L2.

The line L2 branches to the line L3A and the line L3B at the first branch point B1. The line L3A is connected to the ion exchange reaction stirring tank 4A, and the line L3B is connected to the ion exchange reaction stirring tank 4B.
An open / close valve V2A is interposed in the line L3A, and an open / close valve V2B is interposed in the line L3B.
Here, the two ion exchange reaction agitation tanks 4A and 4B are given different reference numerals in the accompanying drawings, but the specifications of the actual machines are the same. Also, three or more ion exchange reaction stirring tanks can be provided.

The discharge side of the ion exchange reaction stirring tank 4A is connected to the suction side of the second slurry pump 6A via a line L4A. The discharge side of the ion exchange reaction stirring tank 4B is connected to the suction side of the second slurry pump 6B via a line L4B.
The discharge side of the second slurry pump 6A is connected to the adsorption aggregation reaction stirring tank 7A via a line L5A. The discharge side of the second slurry pump 6B is connected to the adsorption aggregation reaction stirring tank 7B through a line L5B. An open / close valve V3A is interposed in the line L5A, and an open / close valve V3B is interposed in the line L5B.

The discharge side of the adsorption aggregation reaction stirring tank 7A is connected to the suction side of the third slurry pump 9A via a line L6A. The discharge side of the adsorption / aggregation reaction stirring tank 7B is connected to the suction side of the third slurry pump 9B via a line L6B.
The discharge side of the third slurry pump 9A is connected to the first junction G1 via the line L7A. The discharge side of the third slurry pump 9B is connected to the first junction G1 via the line L7B. An open / close valve V4A is interposed in the line L7A, and an open / close valve V4B is interposed in the line L7B.
Although the two adsorption | suction aggregation reaction stirring tanks 7A and 7B are attached | subjected the different code | symbol in attached drawing, the specification of an actual machine is the same. Further, three or more adsorption aggregation reaction stirring tanks may be provided.

The first joining point G1 is connected to the suction port 10i of the flocculation / separation tank 10 through a line L8.
The coagulation / separation tank 10 is formed with a supernatant discharge port 10o1 for discharging the supernatant at the top, and includes a screw 10S driven by an electric motor at the bottom. The screw 10S extends to the vicinity of the precipitate discharge ports 10o2 and 10o3, and conveys the precipitate (slurry) precipitated at the bottom of the agglomeration separation tank 10 to the precipitate discharge ports 10o2 and 10o3.
The supernatant discharge port 10o1 of the flocculation / separation tank 10 is connected to the supernatant adjustment tank 11 via a line L9. The discharge side of the supernatant adjustment tank 11 is connected to the suction side of the fourth slurry pump 12 via the line L10, and the discharge side of the fourth slurry pump 12 is connected to the second junction G2 via the line L11. Has been. The line L11 is provided with an on-off valve V5.
The second junction point G2 is connected to the second branch point B2 via the line L12. A pressure gauge PG1 is interposed in the line L12.

The line L12 branches to the line L13A and the line L13B at the second branch point B2. The line L13A is provided with an on-off valve V6A and communicates with the suction side of the supernatant filtration device 13A. The connection line L13B is provided with an on-off valve V6B and is connected to the suction side of the supernatant filtration device 13B.
A discharge valve V7A is interposed on the discharge side of the supernatant filtration device 13A, and a discharge valve V7B is interposed on the discharge side of the supernatant filtration device 13B.

A line L14A is connected to the discharge valve V7A, and a line L14B is connected to the discharge valve V7B. The line L14A and the line L14B join at the third junction G3 and communicate with the line L15.
The line L15 is connected to the suction side of the fifth slurry pump 14, and the discharge side of the fifth slurry pump 14 is connected to the treated filtrate adjusting tank 15 via the line L16.
A transport pump P3 is installed at the bottom of the treated filtrate adjusting tank 15, and the filtered water in the treated filtrate adjusting tank 15 is sent to the contaminated water retention area 1 via the line L33 by the convey pump P3. It is done.

The second junction point G2 described above communicates with the air compressor 20. That is, the discharge side line L18 of the air compressor 20 branches to a line L19 and a line L20 at the third branch point B3, and the line L19 communicates with the second junction point G2 via the on-off valve V9.
The line L20 is provided with an on-off valve V10 and communicates with the filter unit UT. In FIG. 1 and FIG. 2, for simplification of illustration, the line L20 is shown in a state of being connected to the fourth branch point B4 in the filter unit UT. However, as will be described later with reference to FIG. 4, in practice, the line L20 is directly connected to each of the concentrated mud vacuum filtration devices 17A to 17H of the filtration device unit UT via a compressed air piping system (not shown). Communicating.
Similarly, in FIG. 1, the line L19 is shown in communication with the line L12 for the sake of simplicity, but in the actual machine, the line L19 is directly connected to the upper side via a compressed air line (not shown in FIG. 1). It communicates with the clarifiers 13A and 13B.
Further, the sediment discharge port 10o2 provided below the flocculation / separation tank 10 communicates with the filter unit UT via the line L17 and the concentrated mud slurry pump 16 (B4).

Details of the filter unit UT will be described with reference to FIG.
In FIG. 2, the filtration device unit UT has eight concentrated mud vacuum filtration devices 17A to 17H. In FIG. 2, four concentrated mud vacuum filtration devices 17A-17D are grouped together (Group A), and four concentrated mud vacuum filtration devices 17E-17H are grouped together (Group E). ).
The specifications of the eight concentrated mud vacuum filtration devices 17A to 17H in the actual machine are the same.
The number of concentrated mud vacuum filtration devices in the filtration device unit UT is not limited to eight, and may be seven or less or nine or more.

The fourth branch point B4 in the filtering device unit UT is connected to the fifth branch point B5 (group A side) via the line L21. A pressure gauge PG2A is interposed in the line L21. The fourth branch point B4 is connected to the fourth junction point G4 (group E side) via the line L22. A line L17X communicates with the fourth junction G4, and the line L17X communicates with the concentrated mud slurry pump 16 and the on-off valve V11 interposed on the discharge side thereof.
In group E (the side on which the concentrated mud vacuum filtration devices 17E to 17H are provided), the fourth junction G4 and the sixth branch point B6 are connected via a line L23. A pressure gauge PG2B is interposed in the line L23, and branches to a line L26 and a line L27 at a sixth branch point B6.
In group A (the side on which the concentrated mud vacuum filtration devices 17A to 17D are provided), the fifth branch point B5 and the seventh branch point B7 are connected by a line L24, and the fifth branch point B5 and the eighth branch point are connected. Point B8 is connected by line L25.

The line L24 branches to a line L28A and a line L28B at a seventh branch point B7, and the line L25 branches to a line L28C and a line L28D at an eighth branch point B8.
The line L28A is connected to the suction side of the concentrated mud vacuum filtration device 17A via an on-off valve V12A, and the line L28B is connected to the suction side of the concentrated mud vacuum filtration device 17B via an on-off valve V12B. The line L28C is connected to the suction side of the concentrated mud vacuum filtration device 17C via an on-off valve V12C, and the line L28D is connected to the suction port of the concentrated mud vacuum filtration device 17D via an on-off valve V12D. Has been.

A line L29A having an open / close valve V13A is connected to the discharge side of the concentrated mud vacuum filtration device 17A. A line L29B having an open / close valve V13B is connected to the discharge side of the concentrated mud vacuum filtration device 17B. A line L29C having an open / close valve V13C is connected to the discharge side of the concentrated mud vacuum filtration device 17C. A line L29D having an open / close valve V13D is connected to the discharge side of the concentrated mud vacuum filtration device 17D.
The line L29A to the line L29D are sequentially joined at the joining points G7 to G5 and communicate with the line L30A. The line L30A is connected to the suction port of the vacuum pump 18A (see FIG. 1) outside the filter unit UT.

In FIG. 2, on the side where the concentrated mud vacuum filtration devices 17E to 17H are provided (group E), the line L26 branches to a line L28E and a line L28F at a ninth branch point B9, and the line L27 is a tenth branch point. Branch to line L28G and line L28H at B10.
The line L28E is connected to the suction port of the concentrated mud vacuum filtration device 17E via the on-off valve V12E, and the line L28F is connected to the suction port of the concentrated mud vacuum filtration device 17F via the on-off valve V12F. Is connected to the suction port of the concentrated mud vacuum filtration device 17G via an on-off valve V12G, and the line L28H is connected to the suction side of the concentrated mud vacuum filtration device 17H via an on-off valve V12H.

A line L29E with an open / close valve V13E is connected to the discharge side of the concentrated mud vacuum filtration device 17E. A line L29F having an open / close valve V13F is connected to the discharge side of the concentrated mud vacuum filtration device 17F. A line L29G having an open / close valve V13G is connected to the discharge side of the concentrated mud vacuum filtration device 17G. A line L29H with an on-off valve V13H is connected to the discharge side of the concentrated mud vacuum filtration device 17H.
The lines L29E to L29H are sequentially joined at the fifth joining points G8 to G10, and communicate with the line L30H. The line L30H is connected to the suction port of the vacuum pump 18B (see FIG. 1) outside the filter unit UT.

As shown in FIG. 1, the discharge side of the vacuum pump 18A is connected to the filtered water and make-up water adjustment tank 19A via a line L31A, and the discharge side of the vacuum pump 18B is connected to the filtered water and make-up water adjustment tank via a line L31B. 19B.
In FIG. 1, a pump P2A is installed at the bottom of the filtered water and makeup water adjustment tank 19A, and the pump P2A is connected to the treated filtrate adjustment tank 15 via a line L32A. On the other hand, a pump P2B is installed at the bottom of the filtrate and makeup water adjustment tank 19B, and the pump P2B is connected to the treated filtrate adjustment tank 15 by a line L32B. As a result, the filtered treated water stored in the makeup water adjustment tanks 19A and 19B is transferred to the treated filtrate adjustment tank 15 via the lines L32A and L32B.
Although not shown in FIG. 1, a branch point may be provided in the middle of the lines L32A and L32B, and a line (not shown) may communicate with the supernatant adjustment tank 11 from the branch point. With such a configuration, the filtered treated water stored in the makeup water adjustment tanks 19 </ b> A and 19 </ b> B is also supplied to the supernatant adjustment tank 11.

In FIG. 1, the roughing screen agitation adjustment tank 2 includes an adjustment tank main body 21, an inclined screen 22, an electric stirrer 23, and a specific gravity densitometer 24.
A pump P <b> 1 installed in the sludge water storage area 1 pumps up contaminated water containing pollutants and supplies it to the inclined screen 22. This is because a relatively large dust contained in the contaminated water is removed by the inclined screen 22. The contaminated water from which relatively large dust is removed by the inclined screen 22 is supplied to the adjustment tank body 21.
Here, if the pollutant having a high specific gravity is precipitated in the adjustment tank main body 21, the pollutant concentration in the contaminated water supplied to the downstream side may not be stabilized. Therefore, the stirrer 23 is continuously operated so that the pollutant does not settle in the adjustment tank body 21, and the contaminant concentration in the contaminated water supplied from the adjustment tank body 21 to the downstream region is kept uniform.

In FIG. 1, each of the ion exchange reaction stirring tanks 4A and 4B includes a stirrer and a level sensor. The ion exchange reaction agitation tanks 4A and 4B are equipped with ion exchange reactant quantitative supply machines 5A and 5B, and the ion exchange reaction material is quantitatively exchanged from the ion exchange reactant quantitative supply machines 5A and 5B. It puts into stirring tank 4A, 4B.
Examples of the ion exchange reaction material charged from the ion exchange reaction agent quantitative supply machines 5A and 5B are iron ferrocyanide (a kind of pigment), cobalt ferrocyanide, and nickel ferrocyanide. In view of price, ferrocyanide is preferable.
Here, since the capacity | capacitance of ion exchange reactant fixed supply machine 5A, 5B is comparatively small, when operating the water purification system 101 over a long time, it is difficult to supply an ion exchange reactant quantitatively. On the other hand, according to the water purification system 101A according to the modification of the first embodiment (see FIG. 3), the ion exchange reactant quantitative supply device having the ability to quantitatively supply a large amount of the ion exchange reactant to be supplied. 50A and 50B (see FIG. 3), and has the ability to quantitatively supply the ion exchange reactant over a long period of time to each of the ion exchange reactant quantitative supply machines 5A and 5B.
When the water purification system 101 is operated over a long period of time by the ion exchange reactant quantitative supply units 50A and 50B, it is possible to ensure the quantitative supply of the ion exchange reactant.

In FIG. 1, an ion exchange reaction agent (for example, iron ferrocyanide) is introduced into the ion exchange reaction agitation tanks 4A and 4B, and the agitator is continuously operated for at least a reaction time in which the ion exchange reaction agent reacts with contaminants. , Stirring. The time for which the stirrer is continuously operated is controlled by a timer, for example.
In FIG. 1, when the on / off valve V2A on the ion exchange reaction stirring tank 4A side is opened, the on / off valve V2B on the ion exchange reaction stirring tank 4B side is closed, and when the on / off valve V2A is closed, the on / off valve V2B is closed. Is open. The ion exchange reaction agitation tanks 4A and 4B are alternately operated so that the ion exchange reaction agitation tanks 4A and 4B are simultaneously in a so-called "full" state, and the contaminated water in the sludge water storage area 1 is converted into the water purification treatment system 101. This is to avoid the situation where the supply cannot be made.
Whether or not the ion exchange reaction agitation tanks 4A and 4B are “full” is determined by detecting the liquid level with a level sensor. The pump P1 is configured to stop when the measurement result value of the level sensor of the ion exchange reaction agitation tanks 4A and 4B exceeds a threshold value.

If the first slurry pump 3 interposed on the discharge side of the roughing screen agitation adjustment tank 2 is activated, the ion exchange reaction agitation tanks 4A and 4B on the side where the on-off valves V2A and V2B are open will be contaminated with water. Is supplied.
In the ion exchange reaction agitation tanks 4A and 4B on the side to which the contaminated water is supplied, the ion exchange reactants are supplied from the ion exchange reactant quantitative supply units 5A and 5B, and the agitator is operated so that the contaminants and ions in the contaminated water are activated. The exchange reactant reacts.

The adsorption aggregation reaction agitation tanks 7A and 7B on the downstream side of the ion exchange reaction agitation tanks 4A and 4B are also equipped with a stirrer and a level sensor, respectively, and are equipped with adsorption agglutination reactant quantitative supply machines 8A and 8B. From the adsorbing and agglutinating agent quantitative feeders 8A and 8B, the adsorbing and aggregating material is quantitatively charged into the adsorbing and aggregating reaction stirring tanks 7A and 7B.
In the ion-exchange reaction agitation tanks 4A and 4B, harmful pollutants are adsorbed by the ion-exchange reactant, and harmless substances are released from the ion-exchange reactant, so that polluted water pollutants are replaced with harmless substances. The For example, if the pollutant is cesium and the ion exchange reactant is iron ferrocyanide, the iron ferrocyanide adsorbs cesium and releases iron into the contaminated water instead of the adsorbed cesium. In the case of zeolite, cesium in contaminated water is adsorbed.
In the adsorption and agglutination reaction agitation tanks 7A and 7B, the ion exchange reactant adsorbed with the contaminant is agglomerated by the adsorption and agglomeration reactant supplied from the adsorbing and agglutinating agent quantitative feeders 8A and 8B. If the agglomerated ion exchange reagent is separated from the water, the contaminated water can be purified.

Here, the capacity of the adsorbing and agglutinating agent quantitative feeders 8A and 8B is relatively small, and when the water purification system 101 operates for a long time, the adsorbing and aggregating reaction agent is quantitatively measured in the adsorbing and aggregating reaction agitation tanks 7A and 7B. It is difficult to supply.
In the modification 101A of the first embodiment shown in FIG. 3, adsorption / aggregation reactant quantitative supply machines 80A and 80B having a large capacity are separately provided. The adsorbing and aggregating reactant quantitative supply units 80A and 80B are configured to quantitatively supply the adsorbing and aggregating reactant quantitative supply units 8A and 8B, respectively.
When the water purification system 101 is operated over a long period of time, the quantitative supply of the adsorbing and aggregating reactant can be ensured by the adsorbing and aggregating agent quantitative supply units 80A and 80B.

When the second slurry pump 6A is actuated, the adsorption / aggregation reaction agent quantitative supply unit 8A is actuated, and a predetermined amount of adsorption / aggregation reaction agent is charged into the adsorption / aggregation reaction agitation tank 7A. The ion exchange reactant that is agitated and adsorbs the contaminants aggregates.
When the second slurry pump 6B is activated, the adsorption / aggregation reaction agent quantitative supply unit 8B is activated, and a predetermined amount of adsorption / aggregation reaction agent is charged into the adsorption / aggregation reaction agitation tank 7B. The ion exchange reactant that has been agitated and adsorbed the contaminants aggregates.
In either one of the adsorptive agglutination reaction agitation tanks 7A and 7B, the agitation is completed when the adsorbing agglomeration reactant quantitative supply devices 8A and 8B and the agitation in the agglutination agitation reaction tanks 7A and 7B are completed. The third slurry pumps 9 </ b> A and 9 </ b> B on the closed side are operated to transfer the aggregated contaminants (ion exchange reactant adsorbing the contaminants) and water to the aggregation separation tank 10.

Here, in the adsorption / aggregation reaction agitation tanks 7A and 7B, the agglutination reaction of the ion exchange reactant that adsorbs the contaminant is proportional to the amount of the adsorption / aggregation reactant supplied from the adsorption / aggregation agent quantitative supply machines 8A and 8B. And proceed.
In order to appropriately control the agglomeration reaction of the ion exchange reactant adsorbing the contaminants by adjusting the amount of the adsorbed agglomeration agent input, the screen agitation adjustment tank 2 is adjusted by the density meter 24 provided in the roughing screen agitation adjustment tank 2. The specific gravity of the contaminated water is measured, and the pollutant concentration is determined from the measured value. Then, based on the determined pollutant concentration, the amount of the adsorbing and agglutinating agent introduced from the adsorbing and aggregating agent quantitative supply machines 8A and 8B is determined.
However, if the property of the contaminated water can be predicted, the amount of the adsorbed agglutination reactant supplied from the adsorbed agglutination reactant quantitative supply machines 8A and 8B may be inverter controlled based on the prediction result of the property of the contaminated water. Is possible.

As shown in FIG. 1, in the flocculation / separation tank 10, a supernatant discharge port 10o1 for discharging a supernatant is formed on the upper side, and a concentration sensor 10R is installed below the supernatant discharge port 10o1. Yes. Further, the aggregating / separating tank 10 is equipped with a level sensor 10L for detecting the amount of liquid stored therein.
The screw 10S provided at the bottom of the coagulation separation tank 10 is configured to be driven by an electric motor. The screw 10S extends to the vicinity of the precipitate discharge ports 10o2 and 10o3, and conveys the precipitate (slurry) precipitated at the bottom of the agglomeration separation tank 10 to the precipitate discharge ports 10o2 and 10o3, thereby agglomerating. It has a function of pushing the sediment accumulated in the separation tank 10 into the sediment discharge ports 10o2 and 10o3. The rotational speed of the screw 10S in the aggregating / separating tank 10 or the amount of sediment transported is controlled based on the concentration detected by the concentration sensor 10R.
In FIG. 1, only the sediment outlet 10o2 communicates with the filter unit UT, and the sediment outlet 10o3 is only connected to the vacuum pump 16S. However, it is possible to provide a plurality of filtration device units UT and communicate with the sediment discharge port 10o3 and the vacuum pump 16S. In addition, on-off valves V8 and V8S are interposed in the sediment discharge ports 10o2 and 10o3, respectively.

In FIG. 1, a fourth slurry pump 12 is interposed downstream of the supernatant adjustment tank 11. The fourth slurry pump 12 is used when the liquid level detected by the level sensor 11L provided in the supernatant adjustment tank 11 (the liquid level of the supernatant liquid in the supernatant adjustment tank 11) is above the upper limit position. It is configured to operate and stop when the liquid level falls below the lower limit position.
In FIG. 1, the ion exchange reaction agitation tanks 4A and 4B, the adsorption and agglomeration reaction agitation tanks 7A and 7B, and the treated filtrate adjustment tank 15 are also equipped with level sensors in the same manner as the supernatant adjustment tank 11, It is configured to operate when the measured liquid level is above the upper limit position, and to stop when the liquid level falls below the lower limit position.

In the region downstream of the supernatant adjustment tank 11 and upstream of the treated filtrate adjustment tank 15, supernatant filtration devices 13A and 13B are provided. The supernatant filtration devices 13A and 13B are provided to remove contaminants having a low specific gravity, and the supernatant filtration devices 13A and 13B are configured to repeatedly operate and stop. Therefore, the supernatant liquid sent out from the supernatant adjustment tank 11 (the supernatant liquid separated in the flocculation / separation tank 10) is continuously supplied to one of the supernatant filtration devices 13A and 13B.
The switching timing between the operating state and the stopping state of the supernatant filtration devices 13A and 13B, or the switching timing of the on-off valve V6A and on-off valve V6B is determined by the measured value of the pressure gauge PG1 interposed in the line L12. When the measured value of the pressure gauge PG1 exceeds a predetermined value, it means that a so-called “clogging” has occurred on one of the supernatant filtration devices 13A and 13B operating at that time. When such a state is reached, the operation and stop of the supernatant filtration devices 13A and 13B are switched, and maintenance of the supernatant filtration device on the “clogged” side is performed.
The structures of the supernatant filtration devices 13A and 13B are substantially the same as the concentrated mud vacuum filtration devices 17A and 17B shown in FIG.
In FIG. 1, two supernatant filtration devices 13A and 13B are shown, but three or more supernatant filtration devices may be provided.

The supernatant liquid (treated water) treated by the supernatant filtration devices 13A and 13B is transferred to the treated filtrate adjusting tank 15 by the transport pump (evacuation pump) 14 and stored.
When the amount of water (treated water) in the treated filtrate adjustment tank 15 reaches a predetermined amount or more, it is returned again to the contaminated water retention area 1 by the transport pump P3 provided in the treated filtrate adjustment tank 15.
Although not shown in FIG. 1, instead of returning the filtered water in the treated filtered water adjusting tank 15 to the contaminated water retention area 1, another purification treatment facility (for example, a reverse osmosis membrane device) (not shown). Can be supplied. Alternatively, it can be discharged into a river or the like.

In FIG. 1, the downstream side of the coagulation separation tank 10 will be described.
A concentrated mud slurry pump 16 is provided on the downstream side of the sediment discharge port 10o2 in the coagulation separation tank 10. The slurry pump 16 is configured so that the discharge amount can be adjusted, and for example, a tube pump is used.
As described above with reference to FIG. 2, the individual concentrated mud vacuum filtration devices 17A to 17H in the filtration device unit UT have the same specifications. FIG. 4 shows a concentrated mud vacuum filtration device 17A.
Here, although not explicitly shown in FIGS. 1 and 2, each of the individual concentrated mud vacuum filtration devices 17 </ b> A to 17 </ b> H is not shown in FIGS. 1 and 2, as will be described with reference to FIG. 4. Compressed air is communicated to each of the concentrated mud vacuum filtration devices 17A to 17H via a compressed air piping system (for example, lines L40, L42A, on-off valve V40A in FIG. 4), and compressed air is supplied from the air compressor 20 (see FIG. 1). It is configured to be supplied to each of the concentrated mud vacuum filtration devices 17A to 17H.

In FIG. 4, the concentrated mud vacuum filtration device 17A includes a bag filter 17Af, a treatment liquid tank 17At, and a level sensor 17As provided in the treatment liquid tank 17At.
The upstream side of the concentrated mud vacuum filtration device 17A is not directly connected to the concentrated mud vacuum filtration device 17A, unlike the case shown in FIGS. As shown in FIG. 4, the line L28A communicates with the concentrated mud vacuum filtration device 17A via the on-off valve V12, the junction G17, and the line L44A.
A line L20 through which compressed air discharged from the air compressor 20 (see FIG. 1) flows is through a compressed air line L40 (indicated by a two-dot chain arrow in FIG. 4), an on-off valve V40A, and a compressed air line L42. It communicates with the junction G17. The compressed air line L40 is not shown in FIGS.
Although not shown, the upstream piping system of the concentrated mud vacuum filtration devices 17B to 17H is also configured in the same manner as shown in FIG. 4, and the compressed air discharged from the air compressor 20 (see FIG. 1) flows. A compressed air line communicating with the line L20 joins.

The precipitate (slurry) separated from the supernatant in the coagulation separation tank 10 (see FIG. 1) contains a large amount of water, but the contaminants are adsorbed (replaced) by the ion exchange reactant. The water in the precipitate (slurry) contains almost no contaminants. Therefore, the water contained in the precipitate (slurry) is separated by the concentrated mud vacuum filtration devices 17A to 17H to reduce the water content of the precipitate (slurry).
Here, the sediment (slurry) sent to the concentrated mud vacuum filtration devices 17A to 17H has a higher contaminant concentration and a higher specific gravity than the supernatant sent to the supernatant filtration devices 13A and 13B. Therefore, it is difficult to separate water by filtration only with the bag filter 17Af. Therefore, as shown in FIG. 1, in the concentrated mud vacuum filtration devices 17A to 17H, in order to dehydrate the precipitate (slurry) as much as possible, the vacuum pumps 18A and 18B are used to evacuate the inside of the concentrated mud vacuum filtration devices 17A to 17H. doing.

In FIG. 4, when the water (treated water) is filtered from the precipitate (slurry) separated from the supernatant in the flocculation / separation tank 10 (see FIG. 1) by the concentrated mud vacuum filtration device 17A, the open / close valve V12A is used. Is opened, and the precipitate separated in the flocculation / separation tank 10 is conveyed to the concentrated mud vacuum filtration device 17A via the line L28A, the on-off valve V12A, and the line L44A. In this case, the on-off valve V42A is closed.
In this case, the precipitate (slurry) is conveyed to the concentrated mud vacuum filtration devices 17A to 17D (A group), and the vacuum pump 18A evacuates the concentrated mud vacuum filtration devices 17A to 17D. In FIG. 4, the symbol MX indicates the precipitate (slurry) dehydrated by the filter 17Af of the concentrated mud vacuum filtration device 17A.

By continuing the operation of separating the water contained in the precipitate (slurry), the bag filter 17Af in the concentrated mud vacuum filtration device 17A is so-called “clogged”. A pressure gauge PG2A (see FIG. 2) is interposed in the line L21 (see FIG. 2) communicating with the line L28A. For example, in FIG. 2, when all of the concentrated mud vacuum filtration devices 17A to 17D (A group) are clogged, the pressure measured by the pressure gauge PG2A increases. By measuring the pressure, it is detected that all of the concentrated mud vacuum filtration devices 17A to 17D (A group) are clogged, and the on-off valves V12A to V12D are closed to concentrate the mud vacuum filtration devices 17A to 17D ( Stop the sediment (slurry) transfer to Group A).
In such a state, the on-off valve V12A is closed in FIG. Since the on-off valve V42A is opened, the compressed air from the air compressor 20 (see FIG. 1) is concentrated via the compressed air line L40, the on-off valve V40A, the compressed air line L42, the confluence G17, and the line L44A. It is supplied to the mud vacuum filtration device 17A. Although not shown in FIG. 4, the compressed mud vacuum filtration devices 17 </ b> B to 17 </ b> D are similarly supplied with compressed air.

In the clogged concentrated mud vacuum filtration devices 17A to 17D, by sending compressed air into the bag filter 17Af, the precipitate (slurry) in the bag filter 17Af is pressed and water is further separated. The burden on the vacuum pump 18A can be reduced accordingly.
In FIG. 2, while the supply of sediment (slurry) to the concentrated mud vacuum filtration devices 17A to 17D is stopped, the precipitate (slurry) is supplied to the concentrated mud vacuum filtration devices 17E to 17H (group E). Switch as expected. Then, the vacuum pump 18B evacuates the concentrated mud vacuum filtration devices 17E to 17H.
If clogging occurs in the concentrated mud vacuum filtration devices 17E to 17H (group E), the on-off valves V12E to V12H of the concentrated mud vacuum filtration devices 17E to 17H (group E) are closed, and the on-off valve V40A in FIG. The on-off valve corresponding to is opened, and compressed air is supplied to each of the concentrated mud vacuum filtration devices 17E to 17H (group E).
That is, the operation of the concentrated mud vacuum filtration devices 17A to 17D (group A) and the concentrated mud vacuum filtration devices 17E to 17H (group E) in FIG. 2 is switched every time clogging occurs.

Next, a series of water treatment procedures in the water purification system 101 of the first embodiment will be described mainly with reference to FIG.
In FIG. 1, the pumping pump P <b> 1 is operated to supply the contaminated water from the contaminated water retention area 1 to the rough screen screening agitation tank 2. Large foreign matters (such as dust) contained in the contaminated water are removed by the inclined screen 22 of the roughing screen agitation tank 2.
The contaminated water from which large foreign matters have been removed is stored in the adjustment tank body 21. Contaminated water stored in the adjustment tank main body 21 is kept constant in the adjustment tank main body 21 without the contaminants being precipitated by continuously operating the agitator 23.
The contaminated water in the adjustment tank main body 21 is ion exchange reaction stirring tanks 4A and 4B (on the side where the on-off valves V2A and V2B are opened by the first slurry pump 3; in the following description, for example, the ion exchange reaction stirring tank 4A ).
An ion exchange reaction agent, for example, iron ferrocyanide, is quantitatively supplied from the ion exchange reaction agent quantitative supply machine 5A to the ion exchange reaction stirring tank 4A to which the contaminated water is supplied. Then, the contaminated water in the tank is stirred by a stirrer whose operation time is controlled by a timer.

In the ion exchange reaction agitation tank 4A, harmful pollutants are adsorbed by the ion exchange reaction agent, and harmless substances are released from the ion exchange reaction agent. Therefore, the pollutants in the contaminated water are replaced with harmless substances. Is removed from contaminated water.
If the pollutant to be removed is sufficiently removed by the ion exchange reactant, the contaminated water is transferred to the adsorption aggregation reaction stirring tank 7A by the second slurry pump 6A.
A fixed amount of adsorbing flocculant is supplied to the contaminated water transferred to the adsorbing / aggregating reaction stirring tank 7A from the adsorbing / aggregating reagent quantitative supply unit 8A. The supplied adsorptive flocculant causes the ion exchange reactant adsorbed with harmful pollutants in the ion exchange reaction agitation tank 4A to aggregate. Thereby, the pollutant (ion exchange reaction agent adsorbing the pollutant) is separated from the contaminated water and aggregates.
The treatment liquid present in the water in a state where the ion exchange reactant adsorbing the contaminants is aggregated is transferred to the aggregation separation tank 10 via the third slurry pump 9A.

In the flocculation / separation tank 10, the treatment liquid present in the water is retained for a predetermined time in a state where the ion exchange reactant adsorbing the contaminant is aggregated, and separated into a supernatant and a precipitate (slurry, sludge).
The supernatant liquid separated in the flocculation separation tank 10 flows into the supernatant adjustment tank 11 via the line L9, and is transferred from the supernatant adjustment tank 11 to the supernatant filtration devices 13A and 13B by the fifth slurry pump 12. Transport.

In the supernatant filtration devices 13A and 13B), contaminants having a low specific gravity (not including contaminants having a high specific gravity) contained in the supernatant liquid separated in the coagulation / separation tank 10 are removed by the bag filter.
The supernatant filtration devices 13A and 13B operate and stop alternately. When one of the supernatant filtration devices 13A and 13B becomes clogged, the operation is stopped and the bag filter is replaced in a known manner.
The supernatant liquid separated in the flocculation / separation tank 10 is filtered by the supernatant filtration device 13A (or 13B), and then supplied to the treated filtrate adjusting tank 15 by the sixth transport pump 14, and the treated filtrate adjusting tank 15 is stored.

On the other hand, the precipitate (slurry) separated in the flocculation separation tank 10 is supplied to each of the concentrated mud vacuum filtration devices 17A to 17H in the filtration device unit UT from the precipitate discharge port 10o2 via the line L17 and the concentrated mud slurry pump 16. And dehydrated in each of the concentrated mud vacuum filtration devices 17A to 17H. At the time of dehydration, each of the concentrated mud vacuum filtration devices 17A to 17H is evacuated by the vacuum pumps 18A and 18B, so that the water dehydrated from the precipitate (slurry) is supplied to the filtered water and makeup water adjustment tanks 19A and 19B. Sucked.
In each of the concentrated mud vacuum filtration devices 17A to 17H, when clogging occurs, the operation and the stop are switched, and the bag filter is replaced in a known manner.

The water (treated water) sucked into the filtered water / replenished water adjusting tanks 19A, 19B is transferred to the treated filtered water adjusting tank 15 by the transport pumps P2A, P2B.
The water (purified contaminated water) stored in the treated filtrate adjustment tank 15 is sent to the contaminated water retention area 1 by the transport pump P3.
Here, the water stored in the treated filtered water adjustment tank 15 may be supplied to a facility (not shown: for example, a reverse osmosis membrane) provided separately, or may be discharged into a taken river or the like. It is.

In 1st Embodiment, it has ion exchange-reactor fixed quantity supply machine 5A, 5B and ion-exchange-reaction stirring tank 4A, 4B, and an ion-exchange reactive agent is a harmful pollutant in ion-exchange-reaction stirring tank 4A, 4B. Adsorbs and releases harmless substances into water.
By such an action by the ion exchange reactant, the pollutant in the contaminated water is replaced with a harmless substance, and the pollutant is removed from the contaminated water.

The ion exchange reactant that adsorbs the pollutant is aggregated while adsorbing the pollutant by the adsorbing flocculant supplied from the adsorbing and agglutinating agent quantitative feeders 8A and 8B in the adsorbing and aggregating reaction agitation tanks 7A and 7B. . The aggregate and water are separated in the aggregation separation tank 10. As a result, most of the contaminants are removed from the separated water and cleaned.
Such water is returned to the storage area 1 where the contaminated water is stored, based on the type, concentration, and standards of the pollutants, and supplied to other cleaning equipment such as reverse osmosis membrane devices. And can be released into lakes and lakes.

According to the first embodiment, the water containing the aggregate of the ion exchange reactant adsorbing the contaminant is separated into the supernatant and the precipitate by the aggregation separation tank 10.
Here, a contaminant having a low specific gravity is mixed in the supernatant liquid separated by the coagulation / separation tank 10. According to the first embodiment, the foreign matter having a low specific gravity is removed from the supernatant by the supernatant filtration devices 13A and 13B.
Moreover, the deposit (slurry) separated by the coagulation separation tank 10 is vacuum dehydrated by the concentrated mud vacuum filtration devices 17A to 17H and the vacuum pumps 18A and 18B. As a result, the water content of the precipitate containing the pollutant is reduced, and disposal or disposal is efficiently performed. Water that has been vacuum dehydrated from the precipitate is cleaned by removing contaminants.

In the illustrated embodiment, the supernatant filtration devices 13A and 13B have a plurality of filtration members (for example, bag filters). When such a filtering member causes so-called “clogging”, the filtering ability or the ability to separate clean water is lowered.
In preparation for such a situation, a pressure gauge PG1 is interposed in the piping system that connects the flocculation separation tank 10 and the supernatant filtration devices 13A and 13B, and when the filtration member is clogged by a pollutant having a low specific gravity, It is detected that the pressure value measured by the pressure gauge PG1 rises and the filtration capacity of the filtration member in the supernatant filtration devices 13A and 13B is reaching the limit.
The supernatant filtration devices 13A and 13B are configured to be switchable in operation. Therefore, the supernatant filtration device (13A, 13B) having the filtration member whose filtration capacity is reaching the limit is stopped, and the supernatant filtration device (13A, 13B) having the filtration member not performing filtration is stopped. By operating the other, the filtration capacity in the supernatant filtration devices 13A and 13B is restored.
Here, the switching of the filtering member and the operation of discharging the filtering member whose filtering ability is lost from the supernatant filtering devices 13A and 13B can be automated, and the operator can remove the contaminants attached to the filtering member. There is no direct contact with (contaminant mixed in the supernatant liquid separated in the flocculation / separation tank 10), and there is no risk of contamination or the like (if the pollutant is a radioactive substance, exposure).

In the illustrated embodiment, the concentrated mud vacuum filtration devices 17A to 17H have a plurality of bag filters, and pressure gauges PG2A and PG2B are connected to the piping system that connects the flocculation separation tank 10 and the concentrated mud vacuum filtration devices 17A to 17H. Is intervening. And the concentrated mud vacuum filtration apparatus 17A-17H is comprised so that a driving | operation and a stop can be switched.
In the case where the precipitate (slurry) is supplied to the concentrated mud vacuum filtration devices 17A to 17D (A group) and the precipitate (slurry) is not supplied to the concentrated mud vacuum filtration devices 17E to 17H (E group), concentration is performed. When the filtration member in the mud vacuum filtration devices 17A to 17D is clogged, the pressure measured by the pressure gauge PG2A increases. Accordingly, it can be detected that the filtration capacity of the filtration member in the concentrated mud vacuum filtration devices 17A to 17D (A group) is reaching its limit.

And the supply of the sediment (slurry) to the concentrated mud vacuum filtration devices 17A to 17D (A group) having the filtration member whose filtration capacity is reaching the limit is stopped, and the precipitate (slurry) is vacuum filtered. It can be switched to supply to the devices 17E to 17H (E group).
As a result, the bag filter whose filtration capability is reaching its limit is switched to an unused bag filter, and the filtration capability of the concentrated mud vacuum filtration device (any one of 17A to 17H) can be recovered.
Furthermore, in the concentrated mud vacuum filtration devices 17A to 17H, since the downstream side of the bag filter is connected to the vacuum pumps 18A and 18B, the water in the precipitate (slurry) separated in the coagulation separation tank 10 is transferred to the bag filter. The vacuum pumps 18A and 18B are evacuated from the downstream side. Therefore, the ability to separate water from the precipitate is improved.

Also in the concentrated mud vacuum filtration devices 17A to 17H, it is possible to automate the work of exchanging the bag filter and discharging the bag filter whose filtration capacity has been lost. There is no need to contact (slurry) directly, and the risk of contact with high-concentration contaminants can be prevented.
Therefore, maintenance of the concentrated mud vacuum filtration devices 17A to 17H (for example, replacement of the bag filter) is performed in a state in which the safety of the worker is ensured, and precipitates containing contaminants from the concentrated mud vacuum filtration devices 17A to 17H ( Slurry) can be discharged.

  In the first embodiment, the compressor 20 is provided, and the compressed air discharge port of the compressor 20 is upstream of the filtration members of the supernatant filtration devices 13A and 13B and the concentrated mud vacuum filtration devices 17A to 17H (the conveying pump 12 or Communicating with the other side of the vacuum pump 16), compressed air stays in the filter member and presses the supernatant or slurry against the filter member, improving the dewatering ability from contaminants or sediment (slurry) I can do it.

Next, a second embodiment of the present invention will be described with reference to FIG.
The second embodiment of FIG. 5 is an embodiment when the contaminant to be treated is a radioactive substance (for example, cesium).
And 2nd Embodiment of FIG. 5 differs in the structure which processes the processed material (sediment) containing the sludge isolate | separated by 10 A of coagulation-separation tanks with respect to 1st Embodiment of FIGS. 1-4. .
Hereinafter, the difference between the second embodiment of FIG. 5 and the first embodiment of FIGS. 1 to 4 will be mainly described.

5, the water purification system generally indicated by reference numeral 102 omits the filtration device unit UT, the vacuum pumps 18A and 18B, and the filtered water / makeup water adjustment tanks 19A and 19B shown in FIG.
On the other hand, in FIG. 5, a concentrated mud stirring adjustment tank 50, a uniaxial paddle continuous kneading mixer 52, and an adsorbed solidification material quantitative supply machine 53 are provided on the downstream side of the aggregation separation tank 10 </ b> A.

In FIG. 5, a sludge discharge hole 10o2 is provided at the bottom of the coagulation / separation tank 10A, and is connected to the suction side of the concentrated mud slurry pump 16 via a line L17.
On-off valve V11 is provided on the discharge side of the concentrated mud slurry pump 16, and is connected to the suction side of the concentrated mud stirring adjustment tank 50 via a line L49.
The discharge side of the concentrated mud stirring adjustment tank 50 is connected to the suction side of the second concentrated mud slurry pump 51 via a line L50. On the discharge side of the second concentrated mud slurry pump 51, an on-off valve V50 is interposed and connected to the first suction port 52i1 of the uniaxial paddle continuous kneading mixer 52 through a line L51.

The uniaxial paddle continuous kneading mixer 52 has a second suction port 52i2, and an adsorbed solidified material quantitative supply unit 53 communicates with the second suction port 52i2. The adsorbed solidified material quantitative supply unit 53 is configured to supply a fixed amount of adsorbed solidified material per unit time to the uniaxial paddle continuous kneading mixer 52.
The discharge side of the uniaxial paddle continuous kneading mixer 52 communicates with the designated storage container 54 via the line L52.

In the second embodiment, iron ferrocyanide is used as the ion exchange reactant introduced into the contamination in the adsorption / aggregation reaction stirring tanks 7A and 7B if the contaminant is, for example, cesium. Ferric ferrocyanide adsorbs cesium in contaminated water and releases iron harmless to the human body instead of adsorbed cesium.
In addition, when zeolite is charged in the adsorption / aggregation reaction stirring tanks 7A and 7B, the zeolite adsorbs contaminants in the water.

According to the second embodiment of FIG. 5, in the uniaxial paddle continuous kneading mixer 52, the solidifying agent is supplied to and mixed with the precipitate (slurry) containing the radioactive material separated in the coagulation separation tank 10A.
As a result, the precipitate (slurry) containing the radioactive substance is supplied into the designated container 54 and then solidified. Thereby, the sludge (slurry) containing a radioactive substance can be enclosed in the designated container 54 for radioactive substance disposal.
Therefore, the subsequent processing (radioactive material disposal processing) is performed safely and efficiently.

The illustrated embodiment is merely an example, and is not intended to limit the technical scope of the present invention.
In the illustrated embodiment, a case where contaminants are mainly removed is described.
However, the present invention can also be applied to a case where desalination is performed by removing sodium chloride and other components from seawater.
In addition, the present invention can be widely applied as a technique for separating various solutes that have been difficult to separate from an aqueous solution from water as a solvent.

DESCRIPTION OF SYMBOLS 1 ... Contaminated water retention area | region 2 ... Rough removal screen stirring adjustment tank 3 ... 1st slurry pump 4A, 4B ... Ion exchange reaction stirring tank 5A, 5B ... Ion exchange reactant fixed supply Machine 6A, 6B ... Second slurry pump 7A, 7B ... Adsorption / aggregation reaction agitation tank 8A, 8B ... Adsorption / aggregation reactant quantitative supply machine 9A, 9B ... Third slurry pump 10 ... Coagulation / separation tank 11: Supernatant adjustment tank 12 ... Fourth slurry pumps 13A, 13B ... Supernatant filter / bag filter 14 ... Fifth slurry pump 15 ... Processed filtered water Adjustment tank 16 ... Concentrated mud slurry pump (tube pump)
17A-17H ... Concentrated mud vacuum filtration device 18 ... Vacuum pumps 19A, 19B ... Filtration water and makeup water adjustment tank 20 ... Air compressor

Claims (4)

  A mechanism for supplying and mixing ion exchange reactants to contaminated water, a mechanism for supplying and mixing adsorbent flocculants to water charged with ion exchange reactants, and water mixed with adsorbent flocculants Separation mechanism for separating supernatant and precipitate, first dehydration device for separating water from the supernatant separated by the separation mechanism, and second dehydration for separating water from the precipitate separated by the separation mechanism A water purification system comprising an apparatus. The first dehydrating apparatus has a plurality of filtration members, and the plurality of filtration members and the piping thereof have a function of replacing the filtration members to which the supernatant liquid from the separation mechanism is supplied. The downstream side communicates with the transfer pump,
The water purification system according to claim 1, wherein a pressure measuring device is interposed in a piping system that connects the separation mechanism and the first dehydrating device. The second dehydrating apparatus has a plurality of filtration members, and the plurality of filtration members and the piping thereof have a function of replacing the filtration members to which the precipitate from the separation mechanism is supplied, and are downstream of the filtration members. The side is connected to the vacuum pump,
The water purification system according to any one of claims 1 and 2, wherein a pressure measuring device is interposed in a piping system communicating the separation mechanism and the second dehydrating device.   The pollutant is a radioactive material, and instead of the second dehydrating device, a solidifying agent mixing device for supplying and mixing the solidifying agent to the precipitate separated by the separation mechanism is provided. Any water purification system.

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