JP2011078861A - Water purification recycle system - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a water purification recycle system which can recover sludge deposited in a marsh, a pond or the like and suspended matter to perform water purification, and can carbonize and recycle the recovered sludge and suspended matter. <P>SOLUTION: The water purification recycle system includes a process for adding a coagulant and ozone in a suction pump 1 when pumping up the sludge or the suspended matter and the like in a marsh, a pond or the like 2, a process for supplying recovered material of the sludge or the suspended matter and the like to which the coagulant and ozone have been added to a coagulation tank to separate the recovered material into the sludge or the suspended matter and the like and ozone-treated water, a process for jetting the ozone-treated water separated in the separation process toward sludge on the bottom of the marsh, pond or the like, a process for supplying the recovered material separated in the coagulation tank to a dehydrator to obtain a dehydrated cake, a process for drying the dehydrated cake and then adding it to a carbonizing furnace to perform carbonization treatment of the recovered material, and a process for returning the carbonized material obtained by the carbonization treatment to the marsh, a pond and the like. Heat generated during the carbonization treatment is used to dry the dehydrated cake. <P>COPYRIGHT: (C)2011,JPO&INPIT

Description

  The present invention relates to a water purification and recycling system. More specifically, the present invention collects suspended sludge such as sludge, algae, and sea cucumber deposited in swamps, ponds, etc. to purify water and purify the water. The present invention relates to a water purification and recycling method that can be carbonized and reused.

  Odors are generated due to deterioration of water quality in swamps, ponds, irrigation reservoirs, dredging, etc., causing environmental problems. Odor is thought to be caused by sludge deposited in these swamps and ponds, and suspension of sea cucumbers that have propagated in water. National and local governments regularly reduce sludge in order to reduce odors in ponds and swamps. Water purification is performed by removing water and suspensions.

  Since water purification equipment for collecting and removing sludge and suspensions is generally a large-sized device and not suitable for movement, conventionally, purification equipment has been installed for sludge and suspensions collected from ponds and swamps. It was transported to a facility where the collected material was processed. Moreover, in order to dispose of the collected recovered material, it was necessary to transport the waste to a disposal site. For this reason, there are problems such as an increase in overall processing costs including transportation costs and disposal costs.

  In order to solve the above problems, the sludge deposited in the pond or pond is collected, and the collected material is dewatered and dried on the spot to perform carbonization to make the carbide, and the carbide is returned to the pond or pond. Recycling has been proposed (for example, JP 2001-300288 A).

JP 2001-300288 A

  Water purification requires not only the removal of sludge but also water treatment that removes suspended suspensions and microorganisms in the water. To perform these multiple treatments simultaneously, the equipment becomes complicated and large. As a result, it is difficult to move the device, and it is not suitable for water purification treatment at the pond or swamp site. Further, if the processing apparatus is downsized to perform processing at the site, the processing capability of the apparatus itself is reduced, so that it takes time for processing, leading to an increase in processing costs.

  The present inventors incorporated a small high-efficiency micro-valve generating nozzle into a suction pump for collecting sludge and the like, and simultaneously performed water purification and sludge collection, and suctioned when collecting sludge and suspended suspensions. By adding a flocculant into the pump, these recovered materials can be efficiently agglomerated and dehydrated, so that they can be used for the next carbonization process in a short time, and as a result, without increasing the size of the processing apparatus. It has been found that water purification and carbonization of sludge and suspension can be performed efficiently. The present invention is based on this finding.

  Therefore, the object of the present invention is to collect sludge and suspended suspensions deposited in swamps, ponds, etc. to purify water and to purify the water and to recycle the recovered sludge and suspensions by carbonization. The purpose is to provide a purification and recycling system.

The water purification and recycling system according to the present invention pumps sludge or suspensions in swamps, ponds, etc. with a pump, puts them in a coagulation tank, and separates collected materials such as sludge or suspensions from water in the coagulation tank. And then dewatering the collected material and performing a carbonization treatment by putting it in a carbonization furnace, returning the obtained carbide to a swamp, pond, etc., and reusing it, a water purification method for swamps, ponds, etc.,
A step of adding flocculant and ozone to the sludge or suspension in the suction pump when pumping the sludge or suspension, etc .;
A step of charging the flocculant and ozone-added recovered material such as sludge or suspension into a coagulation tank to separate the recovered material such as sludge or suspension from the ozone-treated water;
The step of transferring the ozone-treated water separated in the separation step into the swamp, pond, etc. with a pump, and ejecting the ozone-treated water toward the sludge at the bottom of the swamp, pond, etc.,
Drying the agglomerates separated in the agglomeration tank,
Drying the agglomerates and then performing a carbonization treatment by putting them in a carbonization furnace, and returning the carbides obtained by the carbonization treatment to the swamp, pond, etc.
The heat generated during the carbonization treatment is used for drying the agglomerates.

  In a preferred embodiment of the present invention, the flocculant and ozone are added from the suction port of the suction pump.

  Moreover, as a preferable aspect of the present invention, the ozone-treated water is ejected by a microbubble generating nozzle.

  Moreover, as a preferable aspect of the present invention, the method further includes a step of adding the agglomerate into a dehydrator to obtain a dehydrated cake, and the ozone-treated water separated by the dehydrator is fed by the microbubble generating nozzle. Spouts into water such as swamps and ponds.

  Moreover, as a preferable aspect of the present invention, after adding the flocculant and ozone, the recovered material such as the suspension is passed through a stirring line and charged into the aggregating tank.

  Furthermore, as a preferable aspect of the present invention, each of the above steps is performed as a series of steps at a site such as a swamp or a pond.

  According to the water purification method for swamps, ponds and the like according to the present invention, a small high-efficiency microvalve generating nozzle is incorporated in a suction pump for collecting sludge and the like, so that water purification and sludge recovery are performed simultaneously. By adding a flocculant into the suction pump at the time of recovery of the suspended suspension, these recovered products can be efficiently agglomerated and dehydrated so that they can be used for the next carbonization in a short time. Water purification and sludge or suspension carbonization can be efficiently performed without increasing the size of the processing apparatus.

  In addition, sludge and the like generated during the water purification process are carbonized and returned to the marshes, ponds, etc., so no industrial waste is generated. Furthermore, by returning the carbide obtained by carbonization treatment of this sludge to swamps, ponds, etc., this carbide adsorbs suspended matter and sludge in water, and furthermore, deodorization and deodorization of water can be performed by the activated carbon effect. Therefore, effective water quality purification can be performed.

The schematic diagram of the coagulant | flocculant and ozone addition process in one embodiment of the water purification method by this invention. 1 is a schematic side view of a net blower type suction pump used in an embodiment of the present invention. The perspective view of the state which decomposed | disassembled the micro bubble nozzle used in one embodiment of this invention. Sectional drawing which shows the state which cut | disconnected the micro bubble nozzle used in one embodiment of this invention in the surface containing the central axis. Sectional drawing which expanded the periphery of the mixing chamber R of the micro bubble nozzle used in one embodiment of this invention. The schematic side view of the stirring line used in one embodiment of the present invention. The schematic diagram which showed the outline of the isolation | separation process in a coagulation tank in one embodiment of the water quality purification method by this invention. The schematic diagram which showed the outline of the reuse process of the isolate | separated water | moisture content in one embodiment of the water quality purification method by this invention. The schematic of the drying process in one embodiment of the water quality purification method by the present invention. The schematic of the carbonization process in one embodiment of the water purification method by this invention. It is a longitudinal cross-sectional view of the carbonization furnace used in one embodiment of this invention. It is a downward sectional view in FIG. 1 is a schematic flow diagram of a water purification and recycling system according to an embodiment of the present invention.

  The water purification method for swamps, ponds, and the like according to the present invention is a method of pumping sludge or suspension in swamps, ponds, etc., into a coagulation tank, and collecting the sludge or suspension in the coagulation tank. Is separated from moisture, and the recovered material is dehydrated and then put into a carbonization furnace to perform carbonization treatment. The obtained carbide is returned to a swamp, a pond, etc., and reused. ) A step of adding flocculant and ozone to sludge or suspension in a suction pump when pumping sludge or suspension, etc., (2) sludge or suspension added with the flocculant and ozone A step of separating the recovered material such as sludge or suspension and the ozone-treated water, and (3) the ozone-treated water separated in the separation step The sludge is transferred to the swamp, pond, etc. by the pump, and the bottom of the swamp, pond, etc. (4) a step of drying the aggregate separated in the coagulation tank, and (5) drying the aggregate and then putting it into a carbonization furnace to perform carbonization treatment. Step (6) includes a step of returning the carbide obtained by the carbonization treatment to the swamp, the pond or the like. Each process will be described below with reference to the drawings.

<Coagulant and ozone addition process>
FIG. 1 is a schematic diagram showing an outline of a process of adding a flocculant and ozone to sludge or suspension in a suction pump when pumping up sludge or suspension. In the water purification method for swamps, ponds and the like according to the present invention, when the sludge and suspension in the swamps and ponds 2 are pumped up by the suction pump 1, the flocculant and ozone are added in the pumps. The sludge and suspension pumped up are first put into the coagulation tank, but the addition of the coagulant 3 and ozone 4 may be added anywhere in the path from the suction pump 1 to the coagulation tank, The flocculant and ozone may be added simultaneously from one injection port, or each may be added from separate injection ports.

  As the suction pump 1, a submersible pump such as a sand pump can be used. The suction pump 1 is suspended by a winch 5 so that the suction pump 1 can be fixed at a desired depth position. In swamps and ponds 2 and the like, suspended suspensions such as algae and sea cucumbers exist near the surface of the water. By operating the winch 5 and fixing the suction pump 1 near the surface of the water, the suspension can be effectively removed. Can be removed by suction. Further, since sludge is usually present on the bottom of the swamp or pond, the sludge can be selectively removed by suction by operating the winch 5 and lowering the suction pump 1 to the bottom of the swamp or pond 2.

  As shown in FIG. 2, the suction pump 1 can suitably use a net blower type suction pump. The net blower type suction pump is composed of a suction pump main body 11 and the main body 11 covered with a net 12 which is opened downward so as to cover the main body, and the net 12 is covered with a cover 13 which is opened downward. is there. Air or the like can be supplied from the top 14 of the net cage 12, and a part of the supplied air passes from the mesh of the mesh cage 12 to the gap between the mesh cage 12 and the cover 13, and a part of the air Escapes downward (bottom direction) and is discharged to the outside. The air that has escaped into the gap between the net cage 12 and the cover 13 is discharged from the exhaust port 15 at the top of the cover 13. When this netting blower-type suction pump is driven in a state where it is submerged in the bottom of a swamp, a pond, etc., the air exhausted from the bottom of the netting 12 causes air to solidify sludge 16 accumulated at the bottom of the pond. Enters and loosens sludge, making it easy to suck sludge. In addition, the bottom of the swamp or pond is usually covered with chestnuts 17 and the like, and the sludge 16 is deposited on the chestnuts 17 and the like. The sludge 16 can be sucked while blowing away. Further, the air blown out from the mesh on the side surface of the net cage 12 to the cover 13 side causes the debris and fallen leaves of the trees that have settled on the bottom of the swamp, pond, etc. to clog the suction port 18 of the pump and reduce the suction power. Can be prevented. The mesh (mesh) of the mesh cage 12 is preferably about 10 to 30 mm.

  Sludge and suspension sucked from the suction pump 1 are sent to the aggregating tank through the pipe 6. In the present invention, as shown in FIG. 1, an inlet for the flocculant 3 and ozone 4 is provided in the pipe 6, and the flocculant and ozone are added to the sludge, suspension, etc. from there. There may be one injection port in the pipe, or a plurality of injection ports. Further, a three-way cock (not shown) may be provided at the suction port of the suction pump 1 instead of the injection port, and then the flocculant and ozone may be added to the sludge and the suspension.

  The flocculant is introduced from the flocculant tank 7 to the inlet 3 or the suction pump 1 through a pipe. Further, ozone is introduced into the inlet 4 or the suction pump 1 through the piping from the ozone generator 8. A conventionally well-known thing can be utilized suitably for a coagulant | flocculant and an ozone generator.

When ozone is added to sludge or suspension, sterilization, deodorization and decomposition of organic substances are performed by ozone reaction (O ₃ → O ₂ + O). Moreover, since oxygen generated by the ozone reaction is dissolved in the water of sludge and suspension, high-concentration oxygen water is generated. As described later, this high-concentration oxygen water is separated in a coagulation tank, etc., and then returned to the swamp and pond. This high-concentration oxygen water turns the anaerobic layer at the bottom of the swamp and pond into an aerobic layer. Can be replaced.

  Ozone is preferably added by being ejected from a microbubble nozzle. A large amount of ozone per unit time can be added to sludge and suspension by the micro bubble nozzle. Moreover, by adding ozone made into microbubbles, the deodorizing effect is remarkably improved, and ozone can exist in water for a long time in a bubble state, so that the deodorizing effect can be maintained. Moreover, since oxygen can exist in water for a long time in the state of microbubbles after the ozone reaction,

  The micro bubble nozzle will be described. FIG. 3 is a perspective view of the microbubble nozzle in an exploded state, FIG. 4 is a cross-sectional view of the microbubble nozzle cut along a plane including its central axis, and FIG. 3 is an enlarged cross-sectional view of the periphery of a mixing chamber R. FIG.

As shown in FIG. 3, the microbubble nozzle 20 introduces the mixing chamber R, the first inlet IN ₁ for introducing the first mixture into the mixing chamber R, and the second mixture. And a second introduction port IN ₂ having a structure in which an ejection port for ejecting the first and second mixed materials to the outside of the mixing chamber R is provided at a position facing the first introduction port. It is. As shown in FIG. 4, on the inner surface (rear end surface, front end surface or inner peripheral surface) of the mixing chamber R formed in a cylindrical shape, a first inlet port IN ₁ , a second inlet port IN ₂ and an injection port OUT are provided. And are provided. The mixture introduced into the mixing chamber R from the inlets IN ₁ and IN ₂ is mixed in the mixing chamber to become a mixture C, and is jetted out of the mixing chamber R from the jet port OUT. The mixture to be introduced from the inlet IN ₁ is a medium such as water, and the mixture to be introduced from the inlet IN ₂ is a gas such as ozone or oxygen.

An inlet IN _{1 for} a medium such as water is provided on the rear end surface of the mixing chamber R (the front surface of the first member 21 described later), and an inlet IN _{2 for} a gas such as ozone or oxygen is provided in the mixing chamber R. It is provided on the side peripheral surface (the inner peripheral surface of the second member 22 described later). The mixture inlet IN ₂ is the mixture inlet IN ₁ and mixture injection port OUT of the rear end surface and the front end surface in the mixing chamber R may be provided at a position not provided. Mixture injection port OUT are mixing chamber front end surface of the R (the mixture inlet IN ₁ is a surface opposite to the rear end face provided, the back surface of the third member 23 to be described later) is provided on. Therefore, the first inlet port C ₁ of the introduction direction and the direction of introduction of the second introduction port C ₂ are orthogonal, the injection direction of the mixture C with the introduction direction of the first inlet port C ₁ is parallel collinear It is like that.

As shown in FIG. 4, the microbubble nozzle 20 includes a first member 21 having a first introduction port IN ₁ formed on the front surface and a second introduction port IN ₂ formed on an inner peripheral surface so that the mixing chamber R is inside. The second member 22 formed in the above and the third member 23 formed on the back surface of the mixture injection port OUT are configured to be disassembled.

The first member 21, by simply switching the second member 22 or the third member 23, it is possible to switch the diameter _{D IN1} and the diameter _{D IN2} and the diameter _{D OUT} and the diameter _{D R,} like the use of microbubbles nozzle 20 Accordingly, the specification of the nozzle 20 can be easily changed. Furthermore, when the micro bubble nozzle 20 is painful, the micro bubble nozzle 20 can be easily maintained, for example, by replacing each part.

As shown in FIG. 3, a circular recess is formed in two steps on the front surface of the first mixing member 21. As shown in FIG. 4, the second member 22 is fitted into the smaller recess, and the third member 23 is fitted into the larger recess. A screw groove is formed on the outer peripheral surface of the third member 23, and the screw groove can be screwed into a screw groove formed on the inner peripheral surface of the larger concave portion of the first member 21. Yes. Thus, the first member 21 and second member 22 to firmly close contact with the third member 23 in its axial direction, the first object to be a mixture C ₁ and the second object mixture is introduced into the mixing chamber R C ₂ and the like can be prevented from leaking from the gaps between the respective parts.

The opening shapes of the inlets IN ₁ and IN ₂ and the mixture injection port OUT are not particularly limited, and may be non-circular. However, in the embodiment of the present invention, as shown in FIG. Yes. The cross-sectional shape of the mixing chamber R (the shape of the cross section perpendicular to the central axis of the cylindrical mixing chamber R) is not particularly limited, but is circular in the embodiment of the present invention. The opening area of the mixture injection port OUT is set larger than the opening area of the narrow and inlets IN ₁ than the cross-sectional area of the mixing chamber R. In other words, the diameter D _OUT (FIG. 5) of the mixture injection port OUT is set to be smaller than the diameter D _R (FIG. 5) of the cross section of the mixing chamber R and larger than the diameter D _IN1 of the inlet port IN ₁ . . The opening area of the inlet port IN ₂ (diameter _{D IN2} inlet IN ₂ (FIG. 5)) as appropriate depending on the desired mixing ratio of _{C 1} which is an object to be a mixture (water), _{C 2} (ozone or oxygen) It is determined.

The diameter _DIN1 is usually 30 mm or less. The diameter _DIN1 is preferably 20 mm or less, more preferably 15 mm or less, and further preferably 10 mm or less. The diameter _DIN1 is usually 1 mm or more, preferably 2 mm or more. The upstream side of the inlet port IN ₁ may be formed straight (as a straight pipe line having an inner diameter larger than the diameter D _IN1 ), but in this embodiment, as shown in FIG. The flow rate of the mixture C ₁ is gradually increased as it approaches the inlet port IN ₁ .

The diameter _DIN2 is usually 30 mm or less. The diameter _DIN2 is preferably 20 mm or less, more preferably 10 mm or less, and further preferably 5 mm or less. The diameter _DIN2 is usually 0.5 mm or more, preferably 1 mm or more.

Mixture injection port OUT of diameter _{D OUT} (FIG. 5) is larger than the diameter _{D IN1} of the mixture inlet IN _1, no particular limitation is smaller than the diameter _{D R} of the mixing chamber R. The diameter D _OUT is normally set larger by 0.5 mm or more than the diameter D _IN1 . The diameter D _OUT is preferably larger than the diameter D _IN1 by 1 mm or more, more preferably 1.5 mm or more. On the other hand, the diameter _{D OUT} is usually mixing chamber R of the diameter _{D R} 0.5 mm or more than, is set preferably at least 1mm smaller.

The diameter D _R (FIG. 5) of the mixing chamber R is not particularly limited as long as it is larger than the diameter D _OUT of the mixture injection port OUT. In particular, there is no particular limitation on the upper limit of the diameter _{D R,} typically 50mm or less, preferably, 40 mm or less, and more preferably, 30mm or less.

In the direction along the central axis of the mixture R in the cylindrical length _{L R} (FIG. 5), depends balance with such a diameter _{D IN1, D IN2, D OUT} , D R, is not particularly limited. However, if the length _LR is too short, vortex flow is less likely to occur in the mixing chamber R, and the mixed materials C ₁ and C ₂ may not be sufficiently mixed in the mixing chamber R. When the diameters D _IN1 and D _{IN2 of the} inlets IN ₁ and IN _2, the diameter D OUT of the mixture injection port OUT, and the diameter _{DR of the} mixing chamber _R are within the above ranges, the length _LR is usually 0.5 mm or more. The length _{L R} of the mixing chamber R is preferable to be 1mm or more, and more preferably 2mm or more. The mixing chamber to increase the length L _R of the R, vortex is likely to occur in the mixing chamber R, but the mixture C _1, C ₂ is easily mixed, because the dimensions of the microbubbles nozzle 20 is increased, typically 30mm It is as follows. The length _{L R} of the mixing chamber R is preferable to be 20mm or less, and more preferably 10mm or less.

  The sludge or suspension to which the flocculant and ozone are added needs to be sufficiently stirred before being put into the next flocculation tank. For the stirring, a conventionally known stirrer such as a spiral mixer or a static mixer can be used. In the present invention, the sludge or suspension is stirred by incorporating a stirring line 30 as shown in FIG. The stirring line has a structure in which tubes that bend 90 degrees vertically are combined and connected. The sludge or the like that is sucked and transported in the pipe is subjected to an impact when passing through the pipe that bends at 90 degrees and is sufficiently stirred. In the present invention, by combining the microbubble nozzle and the agitation line as described above, it is not necessary to install a turbid water treatment apparatus as in the conventional water purification treatment, and therefore not only can the cost required for water quality treatment be reduced. The processing equipment itself can also be reduced in size.

By setting the pipe diameter D to 1.5 to 2.0 times the diameter of the transport pipe, the stirring line reduces the flow rate of sludge and the like, and the stirring time becomes 1.75 to 4 times. By lengthening the stirring time, the flocculant, the suspension, and the sludge are mixed firmly, and deodorization with ozone can be performed more completely. In the stirring line, it is preferable that the lengths L ₁ and L ₂ of the straight pipe portions are 20 to 30 cm, and about 15 to 15 portions bent 90 degrees are provided. The total length of the stirring line may be about 20 to 25 m.

  The stirring line as described above can be easily produced by connecting, for example, a PVC pipe or the like. PVC pipes and the like are not only inexpensive and easily available, but also have good maintainability because they are rustproof. Moreover, since it is lightweight, it can be brought into the field and an agitation line can be easily assembled.

<Separation process in agglomeration tank>
FIG. 7 is a schematic diagram showing an outline of the separation step in the coagulation tank. The sludge or suspension to which the flocculant and ozone have been added as described above is subjected to a separation step in the flocculant tank 40 to remove moisture. The agglomeration tank 40 is a multiple multiplex type agglomeration tank in which a plurality of agglomeration tanks are connected in parallel. In the multiple multiplex agglomeration tank, a first agglomeration tank 41 and a second agglomeration tank 42 are connected via a roughing filter 44, and the second agglomeration tank 42 and the third agglomeration tank 43 are It is a vertical filter settling tank connected through a fine filter 45. The collected material such as the sludge and suspension sucked is first put into the first flocculation tank 41, where the settled floc having a relatively large specific gravity is separated, and then in the second and third flocculation tanks 42, 43. The sedimentation floc 46 having a smaller specific gravity is separated. The water, which is the supernatant liquid after separation, is reused as described later from the third aggregating tank 43 through the pipe 47.

  The multiple multiplex type agglomeration tank may connect two agglomeration tanks equipped with two chambers through a filter. For example, the one agglomeration tank has a depth of 100 cm, a depth of 100 cm, and a length of about 150 cm. A vertical agglomeration tank can be suitably used.

<Recycle process of separated water>
The water separated in the separation step is returned to the original swamp, pond, etc. through the pipe. This transferred water contains a large amount of oxygen or ozone as described above. By introducing this high-concentration oxygen (ozone) water into swamps and ponds, deodorization, sterilization, decomposition of organic matter, and the like are promoted, so that water purification treatment can be performed more efficiently.

  In the present invention, it is preferable that the separated high-concentration oxygen (ozone) water is ejected toward the sludge at the bottom of the swamp and pond by the above-described microbubble nozzle. By ejecting high-concentration oxygen (ozone) water toward the sludge, the anaerobic layer of sludge at the bottom of the swamp and pond can be replaced with an aerobic layer. Microbial action can be activated to promote the decomposition of organic matter. Moreover, since the residence time of bubbles in water becomes longer by using a microbubble nozzle, effects such as deodorization by high-concentration oxygen (ozone) water are further improved. The high-concentration oxygen (ozone) water sprayed from the microbubble nozzle submerged in the pond, swamp, etc. 2 may be once released through the bubble retention device 9 as shown in FIG. By installing the bubble retention device 9, microbubbles can be released gently. For example, by setting the diameter of the discharge port of the bubble retention device 9 to be 1.5 times or more the diameter of the drain pipe, the microbubbles can be discharged more slowly.

<Aggregate drying step>
Next, the sedimentation floc (aggregate) 46 taken out from the lower part of the coagulation tank is subjected to a drying process, where moisture is removed. The water is used until the water content of the aggregate becomes 30% by weight or less. FIG. 9 shows a schematic diagram of the drying step in the present invention. The agglomerate 46 containing a large amount of moisture is conveyed into the dryer 50, where drying is performed until the moisture content becomes 30% by weight or less. The dryer 50 can utilize heat generated from a carbonization furnace described later. By reusing waste heat from the carbonization furnace, it is possible to reduce the energy cost of the entire water purification system and to reduce carbon dioxide emissions. Moreover, since the exhaust gas discharged from the dryer is also clean, the surrounding environment is not deteriorated.

  In the present invention, before the aggregate is dried, the water content of the aggregate may be lowered to some extent by dewatering the sedimented flocs with a dehydrator (not shown) to obtain a dehydrated cake. By installing a dehydrator, the time for the subsequent drying process can be shortened. A conventionally known vacuum dehydrator or the like can be suitably used as the dehydrator, but is not limited thereto.

  When a dehydrator is installed, the water separated by the dehydration step of the aggregates contains high concentration oxygen (ozone) as described above. Therefore, as explained in the section of the separation step above, it is preferable to return the separated high-concentration oxygen (ozone) water to the swamp and the pond, and the bottom of the swamp and the pond by the microbubble nozzle It is preferable to eject high-concentration oxygen (ozone) water treated with ozone toward the sludge.

<Carbonization process>
FIG. 10 shows a schematic diagram of the carbonization process. The carbonization furnace 60 is provided with two first exhaust gas combustion furnaces 61 and second exhaust gas combustion furnaces 62. In the first and second exhaust gas combustion furnaces 61 and 62, the gas discharged from the carbonization furnace 60 is fired at a high temperature, and the high temperature exhaust gas from the first exhaust gas combustion furnace 61 is returned to the carbonization furnace 60 again. A supply pipe 63 for supplying high-temperature exhaust gas from the two exhaust gas combustion furnace 62 to the dryer 50 is provided. By using such a carbonization apparatus, there is no apparatus contamination, piping clogging, etc., and cleanliness and odor pollution can be eliminated.

  Supplying dry agglomerates as raw materials to the carbonization furnace 60 is performed by supplying raw materials to a crusher with a shovel loader or the like, and the crushed materials are supplied by a feeder 64 with a built-in vibrating screen 65 so that the sizes of the particles are aligned as necessary. 66 or the like and transported to a hopper 68 with a double damper 67 at the top of the carbonization furnace 60. The double damper 67 is provided in order to maintain the reducing atmosphere by shutting off the inside of the carbonization furnace 60 from the outside when the raw material chips are charged into the carbonization furnace 60. The carbonized carbide is discharged from below and transferred to the carbide stocker 70 by the screw conveyor 69 or the like.

  The carbonization furnace 60 includes two exhaust gas combustion furnaces, the first exhaust gas combustion furnace 61 is used for heating the carbonization furnace 60, and the second exhaust gas combustion furnace 62 is used for drying aggregates, and these two exhaust gases are used. The combustion furnace can sufficiently incinerate the exhaust gas at a high temperature, and the agglomerate can be sufficiently dried and carbonized.

  Next, a piping flow from dry agglomerates including various supply pipes to carbonized products will be described with reference to FIG. The carbonization furnace 60 has a carbonization furnace circulation pipe 72 that circulates the exhaust gas through the suction blower 71 and the first exhaust gas combustion furnace 61. Further, a drying pipe 73 branching from the carbonization furnace circulation pipe 72 to the first exhaust gas combustion furnace 61 is provided to the second exhaust gas combustion furnace 62. A dryer pipe 63 from the second exhaust gas combustion furnace 62 to the dryer 50 is provided. An exhaust pipe 74 is provided from the dryer 50, and the exhaust gas is released into the atmosphere through a smoke purification device 75 such as a bag filter.

  Since the exhaust gas combustion furnaces 61 and 62 combust the exhaust gas at a high temperature, it is preferable to increase the number of burners and to make a combustion apparatus having a large heating capacity as compared with the conventional heating furnace only.

  As shown in FIG. 11 or FIG. 12, the carbonization furnace has a conical wall 76 in which the inner wall of the main body of the carbonization furnace 60 extends downward. As shown in FIG. 11, the conical wall 76 has a tapered shape that extends downward. For example, when the height of the conical wall 76 is 2.5 m, the diameter is 1.1 m at the upper part and about 1.2 m at the lower part. A sufficient bridging prevention effect is obtained by the enlargement of. This eliminates the clogging of raw materials due to the bridge formation of the raw materials during carbonization, and continuous supply and continuous discharge can be performed smoothly.

  Further, the carbide take-out device 77 below the inside of the carbonizing furnace 60 is a rotary disk type, and a structure is provided in which a stirrer 78 composed of a stirring disk or a stirring blade is provided above the carbide take-out device 77 coaxially therewith. Since the inner wall of the main body of the carbonization furnace 60 is a conical wall 76 that extends downward, an effect of preventing bridging can be obtained without the agitator 78, but the agitator 78 is more preferably provided. Since the structure of the stirrer 78 may be a simple disk, a stirring blade or a simple radial bar, the equipment cost can be suppressed.

  Heated gas supply ports 79 for firing and carbonizing the raw material in the carbonization furnace 60 in a reduced state are provided at a plurality of locations on the circumference of the conical wall 76. FIG. 12 shows a lower cross section of FIG. 11. In this case, the heated gas is distributed from the carbonization furnace circulation pipe 72 to the three heated gas supply ports 79 in three directions by the surrounding branch pipe 73.

<Carbide recycling process>
The present invention includes a step of returning the carbide obtained as described above to a swamp, a pond or the like. The carbide generally takes a porous form because only organic matter burns in the agglomerates. When such a porous carbide is submerged in a swamp, pond, etc., it can adsorb minute suspended matters and sludge in water and functions as a water purification agent. The carbide is not particularly limited in various forms, and a plurality of carbide pieces packed in a net may be submerged in a swamp, a pond, or the like.

<Water purification and recycling system>
FIG. 13 shows a schematic flow diagram of the water purification and recycling system according to the present invention. First, as described above, sludge or suspensions in swamps, ponds, etc. are pumped up by a pump and put into a coagulation tank. At this time, the flocculant and ozone are added to the sludge or suspension in the suction pump. By this step, the deodorized suction material and the organic matter are efficiently decomposed in a short time. Subsequently, the recovered material such as sludge or suspension added with the flocculant and ozone is put into the coagulation tank, and the recovered material such as sludge or suspension is separated from the ozone-treated water. The ozone-treated high-concentration oxygen (ozone) water separated in this separation step is transferred to the original swamp, pond, etc. by a pump, and the ozone is directed toward the sludge at the bottom of the swamp, pond, etc. Blow out treated water. This reused high-concentration oxygen (ozone) water softens and loosens the sludge at the bottom of the swamp and pond, and also helps clean up the water in the swamp and pond. On the other hand, the agglomerate precipitated and separated in the agglomeration tank is put into a carbonization furnace through a drying step and, if desired, a dehydration step, and carbonized. The carbide obtained by this carbonization is returned to the original swamp, pond, and the like. Therefore, industrial waste is not generated in a series of water purification and recycling, and the reused carbide can also be used for water purification of swamps, ponds, and the like.

DESCRIPTION OF SYMBOLS 1 Suction pump 2 Swamp, pond, etc. 3 Coagulant inlet 4 Ozone inlet 5 Winch 6 Piping 7 Coagulant tank 8 Ozone generator 9 Bubble retention device 11 Suction pump body 12 Net cage 13 Cover 18 Pump suction port 20 Micro bubble nozzle 30 Stirring line 40 Coagulation tank 44, 45 Filter 46 Sedimentation flock (aggregate)
DESCRIPTION OF SYMBOLS 50 Dryer 60 Carbonization furnace 61 1st exhaust gas combustion furnace 62 2nd exhaust gas combustion furnace 64 Supply machine 76 Conical wall 77 Carbide extraction apparatus 78 Stirrer 79 Heating gas supply port

Claims (6)

The sludge or suspended matter in a swamp, pond, etc. is pumped up by a pump and put into a coagulation tank, and the recovered material such as sludge or suspension is separated from moisture in the coagulating tank, and the recovered material is dehydrated and carbonized. A water purification method for swamps, ponds, etc., which is put into a furnace, carbonized, and the resulting carbides are returned to swamps, ponds, etc. for reuse.
A step of adding flocculant and ozone to the sludge or suspension in the suction pump when pumping the sludge or suspension, etc .;
A step of charging the flocculant and ozone-added recovered material such as sludge or suspension into a coagulation tank to separate the recovered material such as sludge or suspension from the ozone-treated water;
The step of transferring the ozone-treated water separated in the separation step into the swamp, pond, etc. with a pump, and ejecting the ozone-treated water toward the sludge at the bottom of the swamp, pond, etc.,
Drying the agglomerates separated in the agglomeration tank,
Drying the agglomerates and then performing a carbonization treatment by putting them in a carbonization furnace, and returning the carbides obtained by the carbonization treatment to the swamp, pond, etc.
A method characterized in that heat generated during the carbonization treatment is used for drying the aggregate.   The method according to claim 1, wherein the addition of the flocculant and ozone is performed from the suction port of the suction pump.   The method according to claim 1, wherein the ozone-treated water is ejected by a microbubble generating nozzle.   The method further comprises the step of charging the agglomerate into a dehydrator to obtain a dehydrated cake, and the ozone-treated water separated by the dehydrator is jetted into water such as a swamp or a pond by the microbubble generating nozzle. The method as described in any one of Claims 1-3.   The method according to any one of claims 1 to 4, wherein after the flocculant and ozone are added, the recovered material such as the suspension is passed through a stirring line and charged into the aggregating tank.   The method according to claim 1, wherein each of the steps is performed as a series of steps at a site such as a swamp or a pond.

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