CN105236626B - The multistage light electrolysis Fenton's reaction device and its application method of a kind of module type iron carbon filler - Google Patents

Abstract

The invention discloses a multi-stage micro-electrolysis-Fenton reaction device with modular iron-carbon filler and a use method thereof, which belong to the field of environmental protection water treatment. It includes a sewage water inlet pump, H ₂ O ₂ dosing device and a pipeline mixer, and also includes a micro-electrolysis-Fenton reaction device, wherein the water inlet pump is connected to the H ₂ O ₂ dosing device, and the H ₂ O ₂ The dosing device is connected to the pipeline mixer, and the pipeline mixer is connected to the multi-stage micro-electrolysis-Fenton reaction device. The appearance of the multi-stage micro-electrolysis-Fenton reaction device is square, and the interior is along the midpoint of the opposite side. It is divided into 4 units, including 2 multi-level micro-electrolysis units, 1 oxidation flocculation unit and 1 sedimentation unit. The 2 multi-level micro-electrolysis units are connected to the oxidation flocculation unit, and the oxidation flocculation unit is connected to the precipitation unit. The invention solves the problems of easy passivation and difficult replacement of iron-carbon fillers, incomplete decolorization of waste water, easy blockage of aeration holes and difficulty in sedimentation of flocs.

Description

A multi-stage micro-electrolysis-Fenton reaction device with modular iron-carbon filler and its application method

technical field

The invention relates to the purification treatment project of waste water in printing and dyeing, chemical industry, electroplating, pesticide, coking and other industries, belongs to the field of environmental protection water treatment, and specifically relates to a multi-stage micro-electrolysis-Fenton reaction device of modular iron-carbon filler and its Instructions.

Background technique

Iron-carbon micro-electrolysis and Fenton oxidation technology are two different wastewater treatment technologies, which can be used independently to treat organic wastewater with high concentration, refractory biodegradability, and poor biodegradability.

Iron-carbon micro-electrolysis is under acidic conditions, when the wastewater is in full contact with the iron-carbon micro-electrolysis filler, a galvanic battery effect is formed between iron and carbon in the wastewater (electrode potential difference 1.2V), and an electrochemical reaction occurs in an aqueous solution containing an acidic electrolyte . The new ecological atoms [H] and Fe ²⁺ produced by the reaction can undergo redox reactions with many components in the wastewater, which can reduce the COD of the wastewater, increase the BOD, improve the biodegradability (B/C) and decolorize the wastewater and other effects.

The Fenton reaction is to mix Fe ²⁺ and H ₂ O ₂ together under acidic conditions with pH less than 4 to obtain OH with strong oxidizing ability (oxidation electrode potential 2.80V), so as to oxidize and decompose pollutants in wastewater Reaction. It has the advantages of rapid reaction, more thorough oxidation, and no secondary pollution.

In summary, both of them react under acidic conditions, and Fe ²⁺ produced in the iron-carbon micro-electrolysis process is one of the main reagents for the Fenton reaction. Based on the above reasons, researches have gradually combined iron-carbon micro-electrolysis and Fenton oxidation technology to form a new advanced oxidation technology for wastewater treatment—iron-carbon micro-electrolysis-Fenton oxidation technology. Under acidic conditions, Fe ²⁺ produced by iron-carbon micro-electrolysis reacts strongly with H ₂ O ₂ added to wastewater, reducing the dosage of Fe ²⁺ in the Fenton reaction and improving the treatment of pollutants by the device ability.

However, in practical applications, the currently commonly used iron-carbon micro-electrolysis-Fenton reaction device mainly has the following problems:

1). The shape of the traditional iron-carbon fillers used is generally spherical, granular, ring-shaped or small flakes. It is generally formed by physical pressing and has not been solidified by high-temperature firing. It is easy to soften, loosen, and be compacted during use. Long-term After operation, the surface of the filler is easy to fall off to form a passivation film, and some suspended particles such as iron-carbon sludge are gradually deposited on the surface of the filler at the bottom, which blocks the effective contact between the filler and the wastewater, resulting in a decrease in the efficiency of wastewater treatment.

2). In the traditional iron-carbon micro-electrolysis reactor, the packing is generally in a landfill state. When it is used, it is piled together without a relatively fixed structural support. After long-term operation, the size of the packing becomes smaller, and the porosity between the packings decreases; the upper layer contains more iron. The heavy filler gradually sinks, crushing the smaller filler in the lower layer and causing uneven distribution of the filler in the pool, forming a cut-off or dead water area, which not only affects the flow state of the wastewater, but also affects the micro-electrolysis effect, resulting in a decrease in treatment efficiency, and also makes subsequent fillers The difficulty of replacement is greatly increased. Even if all the wastewater in the reactor is emptied for cleaning, if the exposure time is longer, the entire packing layer may be agglomerated, resulting in the entire reactor being scrapped.

3). In the commonly used iron-carbon micro-electrolysis-Fenton reaction device, the micro-electrolysis fillers are stacked together as a layer. Due to the limited load-bearing capacity of the support plate, the thickness of the filler layer is generally small. After the wastewater passes through the micro-electrolysis layer, it continues to push upwards. In the process of flow, the iron-carbon filler cannot be contacted again, and the effect of micro-electrolysis is limited.

4). In the commonly used micro-electrolysis-Fenton reaction devices, most of the micro-electrolysis units start to aerate after adding H ₂ O ₂ . A large amount of oxygenation will convert Fe ²⁺ into Fe ³⁺ and slow down the Fenton reaction. However, after the Fenton oxidation, there is no oxygenation and aeration, resulting in more Fe ²⁺ in the effluent, and the Fe(OH) ₂ formed after adding alkali is lighter and difficult to precipitate, and the waste water Due to the color development of residual Fe ²⁺ , the wastewater has a high chroma and poor visual perception.

5). The flocs formed after the Fenton reaction, due to the long aeration time, there are many tiny bubbles attached to the surface of the flocs, which are not easy to settle, and the conventional sedimentation method is not effective.

Chinese invention patent, publication number: 103880225A, publication date: 2014.6.25, discloses a multi-stage iron-carbon micro-electrolysis coupling Fenton oxidation bed reactor, which is characterized in that it includes a lifting pump, a water inlet pipe, a hydrogen peroxide injection Adding device, water inlet pipeline mixer, water distribution room, multi-stage iron-carbon micro-electrolysis coupled Fenton oxidation bed reactor body, feed inlet, elemental iron and granular activated carbon mixture layer, water outlet clarification area, sieve plate water distribution system , sludge outlet, reactor outlet channel, outlet pipe and sedimentation tank, the sedimentation tank includes the sedimentation tank body, outlet pipe and mud discharge pipe. The invention proposes a multi-stage iron-carbon micro-electrolysis coupled Fenton oxidation bed reactor, which solves the problem of COD, ammonia nitrogen, total nitrogen and It is extremely effective for the treatment of refractory polycyclic and heterocyclic organic substances and toxic and harmful substances in wastewater. Its shortcoming is, 1) the hydrogen peroxide dosing device is arranged on the water inlet pipeline mixer, makes the wastewater and the hydrogen peroxide can not fully mix, further is unfavorable for the mixed liquid in the multistage iron-carbon micro-electrolysis coupling Fen The micro-electrolysis and Fenton reaction carried out in the body of the Oxidation Bed Reactor; 2) Elemental iron and granular activated carbon are a mixture layer. After long-term operation, the upper layer contains more iron and the heavier filler gradually sinks, crushing the lower layer Smaller fillers also cause uneven distribution of fillers in the mixture layer, which not only affects the flow state of wastewater, but also affects the effect of micro-electrolysis Fenton reaction, resulting in a decrease in treatment efficiency; 3) The refueling port is located between elemental iron and granular activated carbon On the side of the mixture layer, it is not possible to ensure that the filler is uniform during the refueling process, and the scrap iron slag must be cleaned up. If it is stacked for a long time, it will agglomerate, forming a short flow or dead water area, otherwise it will affect the effect of the micro-electrolysis Fenton reaction, and it is difficult to remove. Time-consuming and laborious, and inconvenient to replace; 4) After adding H ₂ O ₂ to the micro-electrolysis unit, there will be more Fe ²⁺ in the effluent, and the Fe(OH) ₂ formed after adding alkali is lighter and difficult to precipitate, and the waste water is due to The color development of residual Fe ²⁺ leads to higher chroma of wastewater and poor visual perception.

Contents of the invention

1. The problem to be solved

Aiming at the phenomenon that the fillers in wastewater treatment in the prior art are easy to passivate and agglomerate, and there are dead zones or short flow zones in the reactor, resulting in poor micro-electrolysis Fenton reaction effects, the present invention proposes a modular iron-carbon filler The multi-stage micro-electrolysis-Fenton reaction device and its use method solve the problems of poor wastewater treatment effect and color return of effluent. It has a simple structure, the filler is not easy to passivate and agglomerate, it is easy to install and replace, and there is no short flow area in the device. , The dead zone is generated, the filler is distributed in multiple layers in the pool, and the treatment effect is stable.

2. Technical solution

In order to solve the above problems, the technical solution provided by the invention is:

A multi-stage micro-electrolysis-Fenton reaction device with a modular iron-carbon filler, including a sewage inlet pump, H ₂ O ₂ dosing device and a pipeline mixer, and it also includes a micro-electrolysis-Fenton reaction device, wherein the _The sewage inlet pump is set _on the sewage inlet pipe, after the sewage inlet pipe is connected with the H2O2 _dosing device, the _H2O2 dosing device is connected with the pipeline mixer, and the pipeline mixer passes through the pipeline Communicate with the micro-electrolysis-Fenton reaction device;

The micro-electrolysis-Fenton reaction device includes four units, including two micro-electrolysis units, an oxidation flocculation unit and a precipitation unit, the two micro-electrolysis units are connected to the oxidation flocculation unit, and the oxidation flocculation unit is connected to the precipitation unit The side of the sedimentation unit is provided with an outlet pipe, and the bottom of the sedimentation unit is provided with a mud discharge pipe. The appearance of the micro-electrolysis-Fenton reaction device is square, and the interior is divided into 4 units on average along the midpoint of opposite sides; the two micro-electrolysis units are connected in parallel, and only one is used during normal operation, and the other unit is opened during outage maintenance, which can Ensure continuous operation of the unit.

Preferably, the H ₂ O ₂ dosing device includes a H ₂ O ₂ storage tank, an H ₂ O ₂ dosing pipe and a H ₂ O ₂ dosing pump; the bottom of the H ₂ O ₂ storage tank is connected to the H ₂ The O ₂ dosing pipe is connected, and the H ₂ O ₂ dosing pipe is provided with a H ₂ O ₂ dosing pump.

Preferably, the H ₂ O ₂ dosing pipe is inserted into the center point of the cross section along the vertical line of the sewage inlet pipe, and the outlet of the H ₂ O ₂ dosing pipe in the sewage inlet pipe is reversely cut along the direction of water flow, cutting The surface and the water flow direction form an angle of 45°~60°, expand the outlet area of the H ₂ O ₂ dosing pipe, and the distance between the position where the H ₂ O ₂ dosing pipe communicates with the sewage inlet pipe and the pipeline mixer is greater than 300mm , so that H ₂ O ₂ can be mixed evenly with sewage.

Preferably, a mud discharge pipe is provided at the bottom of the micro-electrolysis unit, and the mud discharge pipe is connected to a mud collection bucket, an aeration device is arranged on the mud collection bucket, a water distribution device is provided above the aeration device, and a water distribution device is provided above the water distribution device. There are 3-6 layers of micro-electrolysis reaction layers to increase the contact time between waste water and fillers and ensure the effect of micro-electrolysis reactions. There is a water outlet tank above the micro-electrolysis reaction layer, and a water outlet pipe is installed at the bottom of the right side of the water outlet tank. The aeration device is located The plane where the water distribution device is located and the plane where the micro-electrolysis reaction layer is located are parallel to each other, the water distribution device communicates with the pipeline mixer through a pipeline, and the outlet pipe in the micro-electrolysis unit is connected to the center of the oxidation flocculation unit. The water inlet pipe is connected. The water enters from the bottom of the micro-electrolysis unit, and the water exits from the outlet tank on the upper part of the micro-electrolysis unit. The sludge generated during operation is discharged from the sludge discharge pipe arranged at the bottom of the micro-electrolysis unit.

Preferably, an automatic NaOH dosing system is provided above the oxidation flocculation unit. The NaOH automatic dosing system is composed of a NaOH solution storage tank, a NaOH dosing pipe and a NaOH induction dosing pump. The bottom of the NaOH solution storage tank is connected to the The NaOH dosing pipe is connected, the NaOH dosing pipe is provided with a NaOH induction dosing pump, the NaOH dosing pipe extends into the central water inlet pipe, and the central water inlet pipe is arranged on the central axis of the oxidation flocculation unit. The upper part of the water inlet pipe is vertically inserted into the water outlet tank on the top of the oxidation flocculation unit. A pH online monitor is installed in the water outlet tank. The pH online monitor is connected to the NaOH induction dosing pump, and an outlet pipe is installed at the bottom right side of the water outlet tank. , the bottom of the central water inlet pipe is provided with an umbrella-shaped diffuser, the bottom of the oxidation flocculation unit is provided with an aeration device, the bottom of the aeration device is provided with a mud collection bucket, and the bottom of the mud collection bucket is provided with a mud discharge pipe. The oxidation flocculation unit The outlet pipe inside is connected with the central water inlet pipe inside the sedimentation unit.

Preferably, a central water inlet pipe is provided on the central axis of the sedimentation unit, and the upper part of the central water inlet pipe is vertically inserted into the water outlet tank on the top of the sedimentation unit. The inclined plate in the sedimentation unit is aimed at the flocs formed after the Fenton reaction. Due to the long aeration time, there are many tiny bubbles attached to the surface of the flocs, which are not easy to settle, and the conventional sedimentation method is not effective; the inclined plate is used to enhance the sedimentation. Effect; the bottom of the central inlet pipe is provided with an umbrella-shaped diffuser, the bottom of the sedimentation unit is provided with a mud collecting bucket, and the bottom of the mud collecting bucket is provided with a mud discharge pipe.

Preferably, the aeration device has the same structure as the water distribution device, and is composed of a main pipe and a branch pipe. The branch pipes are symmetrically and evenly arranged on both sides of the main pipe. The holes and the vertical direction of the cross-section of the branch pipe form an angle of 45° and are evenly distributed on both sides of the vertical line. In order to prevent flocs or particles in the wastewater from blocking the orifice, the holes of the aeration device are used for aeration, and the holes of the water distribution device are used for water distribution.

Preferably, the micro-electrolysis reaction layer is composed of a support plate and a modular packing, and the modular packing is arranged side by side on the support plate, and the modular packing is composed of a sheet packing and a PVC bracket. The PVC bracket is in the shape of a cuboid with a built-in card slot, and the sheet fillers are vertically inserted into the card slot, and there are 600-1800 sheet fillers on each micro-electrolysis reaction layer.

Preferably, the central water inlet pipe has a diameter of D, an umbrella-shaped diffuser is provided at the bottom, the corner of the diffuser is 30°, and the length of the bottom is (1.2-1.5) D, and the front view of the mud collecting bucket is an inverted trapezoid, so The diameter of the mud discharge pipe is not less than 200mm.

A method for using a modular iron-carbon filler multi-stage micro-electrolysis-Fenton reaction device, the steps are:

A. according to the foregoing, construct the multistage micro-electrolysis-Fenton reaction device of a kind of modular iron-carbon filler;

B. Check and confirm that the mud discharge pipe is closed;

C. close a valve on the outlet pipe that communicates with the micro-electrolysis unit, sewage inlet pump and H ₂ O ₂ dosing pumps, so that only one micro-electrolysis unit in the micro-electrolysis-Fenton reaction device can be used for sewage treatment;

D. Open another valve on the outlet pipe connected to the micro _- electrolysis unit, the sewage inlet pump and the H2O2 dosing pump, so that only one micro _- electrolysis unit in the micro-electrolysis-Fenton reaction device can be used for sewage treatment ; Turn on the H ₂ O ₂ dosing pump to add H ₂ O ₂ to the sewage; the sewage enters the sewage inlet pipe through the sewage inlet pump, and the H ₂ O ₂ solution in the H ₂ O ₂ storage tank passes through the H ₂ O ₂ dosing pump, The H ₂ O ₂ dosing pipe flows out from the cutting surface of the H ₂ O ₂ dosing pipe, enters the sewage inlet pipe, and merges with the sewage, and the two are fully mixed at the pipeline mixer;

The sewage flowing out of the pipeline mixer enters the water distribution device in the micro-electrolysis unit, flows into the main pipe on the water distribution device, and flows out from the holes on the branch pipe. As the sewage continuously flows into the micro-electrolysis unit, the water level rises and the sewage Gradually contact with each micro-electrolysis reaction layer, the sewage is in full contact with the flake filler, that is, the iron-carbon filler, and under acidic conditions, the iron-carbon micro-electrolysis reaction occurs, and a galvanic battery effect is formed between iron and carbon in the wastewater, and the electrode potential difference is 1.2 V, an electrochemical reaction occurs in an aqueous solution containing an acidic electrolyte, and the new ecological atoms [H] and Fe ²⁺ produced by the reaction can undergo redox reactions with many components in the wastewater, which can reduce the COD of the wastewater and increase the BOD High, biochemical (B/C) improvement and wastewater decolorization effects;

The added H ₂ O ₂ and the Fe ²⁺ produced by the iron-carbon micro-electrolysis reaction are mixed together, and under the acidic condition of pH less than 4, a Fenton reaction occurs to obtain OH with strong oxidation ability (oxidation electrode potential 2.80V) , so that the reaction of oxidizing and decomposing pollutants in wastewater has the advantages of rapid reaction, thorough oxidation, and no secondary pollution;

In summary, both the iron-carbon micro-electrolysis reaction and the Fenton reaction are carried out under acidic conditions, and the Fe ²⁺ produced during the iron-carbon micro-electrolysis process is one of the main agents for the Fenton reaction. Fenton oxidation technology is combined to form a new advanced oxidation technology for wastewater treatment - micro-electrolysis-Fenton oxidation technology. Under acidic conditions, Fe ²⁺ produced by iron-carbon micro-electrolysis reaction, and H ₂ added to wastewater O ₂ has a strong oxidation reaction, which reduces the dosage of Fe ²⁺ in the Fenton reaction and improves the device's ability to treat pollutants.

In the conventional reactor, there is no oxygenation and aeration after the Fenton oxidation, resulting in more Fe ²⁺ in the effluent, and the Fe(OH) ₂ formed after adding alkali is lighter and difficult to precipitate, and the residual Fe ^{2 +} Color development leads to high chroma of wastewater and poor visual perception; the present invention neither directly aerates nor adds alkali, avoiding the occurrence of the above two situations.

E. After adding H ₂ O ₂ , the aeration device of the micro-electrolysis unit aerates for 10 to 15 minutes every 45 minutes; and in the commonly used micro-electrolysis-Fenton reaction device, most of the micro-electrolysis units add H Aeration starts after ₂ O ₂ , a large amount of oxygenation will convert Fe ²⁺ into Fe ³⁺ , and Fe ²⁺ is one of the main reagents for the Fenton reaction, which will slow down the Fenton reaction rate and reduce the oxidation effect of pollutants The present invention aerates after an interval of 45 minutes without converting Fe ²⁺ into Fe ³⁺ , and the Fe ²⁺ produced by iron-carbon micro-electrolysis can increase the Fenton reaction rate and enhance the oxidation effect of pollutants. The sediment after iron-carbon reaction, Fenton reaction and aeration, the impurities and sediment in the sewage all sink into the mud collecting bucket;

In addition, the iron sludge that falls off from the upper layer of the micro-electrolysis reaction layer may adhere to the surface of the micro-electrolysis reaction layer, so the micro-electrolysis unit is intermittently aerated to desorb the iron sludge on the surface of the micro-electrolysis reaction layer. Improve the reaction effect of micro-electrolysis-Fenton device.

F. The aeration device at the bottom of the oxidation flocculation unit aerates continuously, and the air-water ratio is 6-15:1; the sewage with Fe ²⁺ in the micro-electrolysis unit flows into the center of the oxidation flocculation unit through the outlet pipe on the outlet tank. In the water pipe, the umbrella-shaped diffuser at the bottom of the central water inlet pipe enters the bottom of the oxidation flocculation unit; the inlet of the aeration device at the bottom of the oxidation flocculation unit is continuously aerated with an air-to-water ratio of 6 to 15:1, and the Fe ²⁺ in the wastewater is After oxidation to Fe ³⁺ , remove the chroma of sewage;

G. When the wastewater level reaches the outlet tank, the pH online monitor in the outlet tank monitors the pH value of the wastewater. When the pH is less than 6, the NaOH induction dosing pump is automatically turned on, and the NaOH solution is added to the central water inlet pipe to generate The floc Fe(OH) ₃ further entrains pollutants and settles into the mud collecting bucket;

After the micro-electrolysis-Fenton reaction, the effluent enters the oxidation flocculation unit, adding NaOH and continuously oxygenating, which can play the following roles: oxidize the residual Fe ²⁺ in the wastewater to Fe ³⁺ , remove the color of Fe ²⁺ , Avoid the phenomenon of color reversion of the effluent; further oxidize and decompose the organic matter in the wastewater; form flocs under alkaline conditions, and aerate to stir.

H. After the oxidation flocculation unit is treated, the wastewater flows from the outlet pipe at the bottom of the right side of the outlet tank into the center inlet pipe of the sedimentation unit, and enters the bottom of the sedimentation unit for further precipitation. In the mud collecting hopper, the water level of the treated wastewater gradually rises and enters the next process through the outlet pipe in the sedimentation unit;

I. When the mud collecting bucket of any unit in the micro-electrolysis unit, oxidation flocculation unit and sedimentation unit is full of sediment, open the corresponding mud discharge pipe to discharge mud;

J. When the modular packing in the micro-electrolysis unit is used up, or when it is out of service for maintenance, turn off the sewage inlet pump and the H2O2 dosing pump, and turn _on the water pump installed _on the outlet pipe of the micro-electrolysis unit to decompose the micro-electrolysis unit. All the waste water in the unit is sent to the oxidation flocculation unit, close the valve on the outlet pipe connected to this micro-electrolysis unit, open the valve _on the outlet pipe connected to another micro _- electrolysis unit, sewage inlet pump and H2O2 The drug pump ensures continuous and uninterrupted sewage treatment.

K. Remove the outlet tank in the micro _- electrolysis unit with the sewage inlet pump and H2O2 dosing pump closed, take out the micro _- electrolysis reaction layers in the micro-electrolysis unit in turn, and then put in new micro-electrolysis reaction layers in turn, Place the outlet tank on the micro-electrolysis unit for the next time the micro-electrolysis unit in use is out of service for maintenance or when the modular filler is used up.

Preferably, the micro-electrolysis reaction layer is composed of a support plate and a modular packing, and the modular packing is arranged side by side on the support plate, and the modular packing is composed of a sheet packing and a PVC bracket. The PVC bracket is in the shape of a cuboid with a built-in card slot, and the sheet filler is inserted vertically into the card slot;

The mass parts and mesh numbers of each component in the described flaky filler are respectively:

Cast iron or pig iron filings: 55-60 parts, 50-60 mesh;

Coke powder: 30-35 parts, 60-70 mesh;

Copper powder: 5-10 parts, 50-60 mesh;

Binder: 3 to 5 parts;

The binder includes fine yellow sand and Portland cement, with a mass ratio of 1:2 to 3;

Its production steps are as follows:

The barbed wire mesh with a size of 8*8*0.8 is used as the skeleton. After being formed by high-pressure pressing, it is fired in a furnace filled with nitrogen at a high temperature. The temperature is: 1050-1200°C, and the firing time is: 4-5 hours.

Due to the addition of copper, it forms a larger potential difference than traditional iron-carbon fillers, and has the characteristics of no passivation, no fragmentation, and no agglomeration during use; the number of sheet-like filler units in the modular filler can be determined by the quality of wastewater. It can be grasped flexibly and appropriately increased or decreased; the support plate is made of glass fiber reinforced plastic grating bars and bears heavy weight.

The shape of the traditional iron-carbon fillers used is generally spherical, granular, ring-shaped or small flakes. They are generally formed by physical pressing and have not been solidified by high-temperature firing. They are easy to soften, loosen, and be compacted during use. After long-term operation, the fillers The surface is easy to fall off to form a passivation film, and some suspended particles such as iron-carbon mud are gradually deposited on the surface of the filler at the bottom, which blocks the effective contact between the filler and the wastewater, resulting in a reduction in the wastewater treatment effect; the present invention adopts this form of layer separation, Avoiding the deposition of suspended particles on the surface of the filler, so that the iron-carbon filler can effectively and fully contact the wastewater, and improve the wastewater treatment effect;

In traditional iron-carbon micro-electrolysis reactors, the fillers are generally in a landfill state. When in use, they are piled together without a relatively fixed structural support. After long-term operation, the size of the fillers becomes smaller, and the porosity between the fillers decreases; the upper layer contains more iron and is heavier. The filling gradually sinks, crushing the smaller filling in the lower layer and causing uneven distribution of filling in the pool, forming a cut-off or dead water area, which not only affects the flow state of wastewater, but also affects the effect of micro-electrolysis, resulting in a decrease in treatment efficiency and making subsequent replacement of filling difficult. increase; even if all the waste water in the reactor is emptied to clean up, if the exposure time is longer, the whole packing layer may be all agglomerated, causing the whole reactor to be scrapped; the present invention arranges multi-layer micro-electrolysis reaction layers in the micro-electrolysis unit, The layers are separated, and each layer is supported by a support plate. There are multiple groups of modular packing arranged side by side on the support plate. The modular packing is composed of sheet packing and PVC brackets. The PVC brackets are Cuboid shape, built-in card slot, the sheet-shaped filler is inserted vertically into the card slot, long-term operation, there is no filler sinking, resulting in uneven distribution, resulting in the phenomenon of cut-off or dead water area, and there is no agglomeration or When the reactor is scrapped, the micro-electrolysis efficiency is stable and efficient. After a period of operation, the micro-electrolysis reaction layer can be taken out, the PVC bracket can be recycled, and the packing can be replaced to continue to use. It is convenient to operate, saves costs, and improves the utilization rate of the packing. , improve the effect of sewage treatment;

In the commonly used iron-carbon micro-electrolysis-Fenton reaction device, the micro-electrolysis fillers are stacked together as a layer. Due to the limited load-bearing capacity of the support plate, the thickness of the filler layer is generally small. After the wastewater passes through the micro-electrolysis layer, it continues to push upward. In the micro-electrolysis unit, the micro-electrolysis reaction layer cannot be contacted again, and the micro-electrolysis effect is limited; the present invention sets a multi-layer micro-electrolysis reaction layer in the micro-electrolysis unit, and the layers are separated, and each layer is supported by a support plate. Modular filler, the upward push flow of wastewater can contact with multi-layer micro-electrolysis reaction layer, which increases the contact time between wastewater and filler, the treatment efficiency is better than traditional micro-electrolysis filler, and the treatment effect is stable.

The multi-stage micro-electrolysis-Fenton reflection device of the present invention can be used in small-scale sewage treatment systems as well as large-scale urban sewage treatment systems. It only needs to design structural dimensions with different parameters and technical characteristics according to different application occasions.

3. Beneficial effect

Compared with the prior art, the beneficial effects of the present invention are:

(1) The present invention aims at the flocs formed after the Fenton reaction. Due to the long aeration time, there are many tiny bubbles attached to the surface of the flocs, which are not easy to settle, and the effect of the conventional sedimentation method is not good; a slant plate is set to enhance the sedimentation effect The holes of the aeration device are used for aeration, and the holes of the water distribution device are used for water distribution, so as to prevent the flocs or particles in the waste water from blocking the orifice; these settings can make the device operate effectively and reduce maintenance failures The efficiency ensures the normal operation of the device; the appearance of the micro-electrolysis-Fenton reaction device is square, and the interior is divided into 4 units on average along the midpoint of the opposite side; the two micro-electrolysis units are connected in parallel, only one is used during normal operation, and the shutdown Opening another unit during maintenance can ensure the continuous operation of the device, and there will be no situation that the reactor will suspend operation when the packing is replaced or the reactor is shut down for maintenance;

( ₂ ) _The sewage of the present invention enters the sewage water inlet pipe through the sewage water inlet pump, and the _H2O2 solution in the _H2O2 storage tank passes through the _{H2O2 dosing} pump, and the _{H2O2 dosing} pipe is _fed from the _H2O2 The cutting surface of the dosing pipe flows out, enters the sewage inlet pipe, and merges with the sewage, and the two are fully mixed at the pipeline mixer; the sewage flowing out of the pipeline mixer enters the water distribution device in the micro-electrolysis unit, and flows into the dry water distribution device on the water distribution device. The pipe flows out from the hole on the branch pipe. As the sewage continuously flows into the micro-electrolysis unit, the water level rises, and the sewage gradually contacts with each micro-electrolysis reaction layer. Under these conditions, the iron-carbon micro-electrolysis reaction occurs, a galvanic cell effect is formed between iron and carbon in the wastewater, the electrode potential difference is 1.2V, an electrochemical reaction occurs in an aqueous solution containing an acidic electrolyte, and the new ecological atoms [H] and Fe ²⁺ , etc. can undergo redox reactions with many components in wastewater, which can achieve the effects of reducing COD, increasing BOD, improving biodegradability (B/C) and decolorizing wastewater;

(3 _{) the H that the present invention adds O 2 and} the Fe that iron-carbon ^{microelectrolysis} reaction produces mix together, under the acid condition of pH less than 4, Fenton reaction takes place, obtains the very strong OH (oxidation Electrode potential 2.80V), so as to oxidize and decompose the pollutants in the wastewater, which has the advantages of rapid reaction, complete oxidation, and no secondary pollution;

(4) iron-carbon micro-electrolysis reaction of the present invention and Fenton reaction all are to react under acidic conditions, and the Fe that produces in iron-carbon micro-electrolysis process ²⁺ is one of main medicament of Fenton reaction, iron-carbon micro-electrolysis and Fenton oxidation technology is combined to form a new advanced oxidation technology for wastewater treatment - micro-electrolysis-Fenton oxidation technology. Under acidic conditions, Fe ²⁺ produced by iron-carbon micro-electrolysis reaction is combined with H ₂ O ₂ undergoes a strong oxidation reaction, which reduces the dosage of Fe ²⁺ in the Fenton reaction and improves the device's ability to treat pollutants; the conventional reactor does not have oxygenation and aeration after the Fenton oxidation, resulting in Fe ²⁺ is more, and the Fe(OH ₎ that forms after adding alkali is lighter and difficult for precipitation, and in the waste water, due to residual Fe ²⁺ color development, the chromaticity of the waste water is higher, and the visual perception is poor; the present invention has neither Direct aeration without adding alkali avoids the occurrence of the above two situations;

(5) In the commonly used micro-electrolysis-Fenton reaction devices, most of the micro-electrolysis units start to aerate after adding H ₂ O ₂ , a large amount of oxygenation will convert Fe ²⁺ into Fe ³⁺ , and Fe ²⁺ It is one of the main agents for the Fenton reaction, which will slow down the Fenton reaction rate and reduce the oxidation effect of pollutants; the invention will aerate after 45 minutes, and will not convert Fe ²⁺ into Fe ³⁺ , resulting in iron-carbon micro-electrolysis Fe ²⁺ can increase the Fenton reaction rate and enhance the oxidation effect of pollutants. The iron-carbon reaction, Fenton reaction and sediment after aeration, impurities and sediment in the sewage all sink into the mud collection bucket; in addition, the iron sludge that falls off from the upper layer of micro-electrolysis reaction layer may adhere to On the surface of the micro-electrolysis reaction layer, intermittent aeration is performed in the micro-electrolysis unit to desorb the iron sludge on the surface of the micro-electrolysis reaction layer to improve the reaction effect of the micro-electrolysis-Fenton device;

(6) The effluent after the micro-electrolysis-Fenton reaction of the present invention enters the oxidation flocculation unit, and NaOH is added and oxygenated continuously, which can play the following role: the residual Fe ²⁺ in the wastewater is oxidized to Fe ³⁺ , and Fe 3+ is removed. ²⁺ chromaticity, to avoid the phenomenon of color reversion of effluent; to further oxidize and decompose organic matter in wastewater; to form flocs under alkaline conditions, and aeration plays a stirring role;

(7) The flaky filler of the present invention is formed by high-temperature firing after adding copper powder and binder into flakes in the traditional iron-carbon filler; due to the addition of copper, it forms a larger potential than the traditional iron-carbon filler It has the characteristics of no passivation, no fragmentation, and no agglomeration during use; the number of sheet-like packing units in the modular packing can be flexibly controlled according to the water quality of the wastewater, and can be appropriately increased or decreased; the support plate is made of glass fiber reinforced plastic Composed of grid bars, heavy bearing;

(8) The shape of the traditional iron-carbon fillers used is generally spherical, granular, ring-shaped or small flakes. They are generally formed by physical compression and have not been solidified by high-temperature firing. They are easy to soften, loosen, and be compacted during use. Long-term After operation, the surface of the filler is easy to fall off to form a passivation film, and some suspended particles such as iron and carbon mud are gradually deposited on the surface of the filler at the bottom, which blocks the effective contact between the filler and the wastewater, resulting in a reduction in the wastewater treatment effect; the present invention adopts this layer-by-layer separation The form avoids the suspended particles from depositing on the surface of the filler, so that the iron-carbon filler can effectively and fully contact the wastewater, and improve the wastewater treatment effect;

(9) In traditional iron-carbon micro-electrolysis reactors, the packing is generally in a landfill state, and there is no relatively fixed structural support when stacked together during use. After long-term operation, the size of the packing becomes smaller, and the porosity between the packings decreases; the upper layer contains more iron The heavy filler gradually sinks, crushing the smaller filler in the lower layer and causing uneven distribution of the filler in the pool, forming a cut-off or dead water area, which not only affects the flow state of the wastewater, but also affects the micro-electrolysis effect, resulting in a decrease in treatment efficiency, and also makes subsequent fillers The difficulty of replacement is greatly increased; even if all the waste water in the reactor is emptied for cleaning, if the exposure time is long, the entire packing layer may be agglomerated, resulting in the entire reactor being scrapped; The reaction layer is separated layer by layer, and each layer is supported by a support plate. There are multiple sets of modular packing arranged side by side on the support plate. The modular packing is composed of sheet packing and PVC brackets. The PVC The bracket is in the shape of a cuboid and has a built-in card slot. The sheet-like filler is inserted vertically into the card slot. After long-term operation, there is no phenomenon that the filler sinks, causing uneven distribution, and forming a cut-off or dead water area. In the case of agglomeration or the reactor being scrapped, the micro-electrolysis efficiency is stable and efficient. After a period of operation, the micro-electrolysis reaction layer can be taken out, the PVC bracket can be recycled, and the filler can be replaced to continue to use, which is convenient for operation, saves costs, and improves Filler utilization rate, improve sewage treatment effect;

(10) In the commonly used iron-carbon micro-electrolysis-Fenton reaction device, the micro-electrolysis fillers are stacked together as a layer. Due to the limited load-bearing capacity of the support plate, the thickness of the filler layer is generally small. After the waste water passes through the micro-electrolysis layer, it continues to push upwards. In the process of flow, the iron-carbon filler cannot be contacted again, and the micro-electrolysis effect is limited; the present invention arranges multi-layer micro-electrolysis reaction layers in the micro-electrolysis unit, and the layers are separated. Each layer is supported by a support plate, and the support plates are juxtaposed There are multiple sets of modular fillers, and the upward push flow of wastewater can contact with the multi-layer micro-electrolysis reaction layer, which increases the contact time between wastewater and fillers, and the treatment efficiency is better than that of traditional micro-electrolysis fillers, and the treatment effect is stable;

(11) The multi-stage micro-electrolysis-Fenton reflection device of the present invention can be used in small-scale sewage treatment systems and can also be used in large-scale urban sewage treatment systems, only need to design the structural dimensions of the technical characteristics of different parameters according to different application occasions.

Description of drawings

Fig. 1 is the schematic diagram of water distribution device of the present invention;

Fig. 2 is branch pipe cross-sectional view of the present invention;

Fig. ₃ is the H2O2 dosing device of the present invention Schematic diagram of the structure _;

Fig. 4 is a schematic diagram of the modular iron-carbon filler of the present invention.

1. Sewage inlet pump; 2. H ₂ O ₂ dosing pump; 2-1, H ₂ O ₂ storage tank; 2-2, H ₂ O ₂ dosing pipe; 3. Pipeline mixer; 4-14-1 Dry pipe; 4-14-2, branch pipe; 4-15 modular packing; 4-15-1, sheet packing; 4-15-2, PVC bracket.

Detailed ways

The present invention will be further described below in conjunction with specific embodiments.

Example 1

Combined with Figures 1-4, a multi-stage micro-electrolysis-Fenton reaction device with modular iron-carbon fillers, including sewage inlet pump 1, H ₂ O ₂ dosing device and pipeline mixer 3, it also includes micro-electrolysis- Fenton reaction device, wherein the sewage inlet pump ₁ is arranged _on the sewage inlet pipe, after the sewage inlet pipe communicates with the H2O2 dosing device, the _H2O2 dosing device and the pipeline mixer ₃ In communication, the pipeline mixer 3 communicates with the micro-electrolysis-Fenton reaction device through a pipeline;

The H ₂ O ₂ dosing device includes a H ₂ O ₂ storage tank 2-1, a H ₂ O ₂ dosing pipe 2-2 and a H ₂ O ₂ dosing pump 2; the H ₂ O ₂ storage tank 2 -1 is in communication with the H ₂ O ₂ dosing pipe 2-2, and the H ₂ O ₂ dosing pipe 2-2 is provided with a H ₂ O ₂ dosing pump 2.

The H ₂ O ₂ dosing pipe 2-2 is inserted into the center point of the cross-section along the vertical line of the sewage inlet pipe, and the outlet of the H ₂ O ₂ dosing pipe 2-2 in the sewage inlet pipe is on the opposite side along the water flow direction. Cutting, the cutting surface forms an included angle of 45°～60° with the water flow direction, expands the outlet area of the H ₂ O ₂ dosing pipe 2-2, and the position where the H ₂ O ₂ dosing pipe 2-2 communicates with the sewage inlet pipe is connected to the The distance between the pipe mixers ₃ is greater _than 300mm, so that the H2O2 can be mixed evenly with the sewage.

The micro-electrolysis-Fenton reaction device includes four units, including two micro-electrolysis units, an oxidation flocculation unit and a precipitation unit, the two micro-electrolysis units are connected to the oxidation flocculation unit, and the oxidation flocculation unit is connected to the precipitation unit The side of the sedimentation unit is provided with an outlet pipe, and the bottom of the sedimentation unit is provided with a mud discharge pipe. The appearance of the micro-electrolysis-Fenton reaction device is square, and the interior is divided into 4 units on average along the midpoint of opposite sides; the two micro-electrolysis units are connected in parallel, and only one is used during normal operation, and the other unit is opened during outage maintenance, which can Ensure continuous operation of the unit.

The bottom of the micro-electrolysis unit is provided with a mud discharge pipe, and the mud discharge pipe is connected to the mud collection bucket. An aeration device is arranged on the mud collection bucket. A water distribution device is provided above the aeration device. A 3- 6 layers of micro-electrolysis reaction layers to increase the contact time between waste water and fillers to ensure the effect of micro-electrolysis reactions. There is a water outlet above the micro-electrolysis reaction layer, and a water outlet pipe is installed at the bottom of the right side of the water outlet. The plane where the aeration device is located, the layout The plane where the water device is located is parallel to the plane where the micro-electrolysis reaction layer is located, and the water distribution device is communicated with the pipeline mixer 3 through a pipeline, and the outlet pipe in the micro-electrolysis unit is connected to the central water inlet pipe in the oxidation flocculation unit connected. The water enters from the bottom of the micro-electrolysis unit, and the water exits from the outlet tank on the upper part of the micro-electrolysis unit. The sludge generated during operation is discharged from the sludge discharge pipe arranged at the bottom of the micro-electrolysis unit.

The micro-electrolysis reaction layer is composed of a support plate and a modular packing 4-15, and the modular packing 4-15 is arranged side by side on the supporting plate, and the modular packing 4-15 is composed of a sheet-shaped packing 4-15 -1. It is composed of PVC bracket 4-15-2. The PVC bracket 4-15-2 is cuboid and has a built-in slot. The sheet filler 4-15-1 is vertically inserted into the slot. There are altogether 600-1800 flake fillers 4-15-1 on each micro-electrolysis reaction layer.

An automatic NaOH dosing system is provided above the oxidation flocculation unit. The NaOH automatic dosing system is composed of a NaOH solution storage tank, a NaOH dosing pipe and a NaOH induction dosing pump. The bottom of the NaOH solution storage tank is connected to the NaOH dosing pump. The NaOH dosing pipe is provided with a NaOH induction dosing pump, and the NaOH dosing pipe extends into the central water inlet pipe, and the central water inlet pipe is arranged on the central axis of the oxidation flocculation unit. The upper part is inserted vertically into the water outlet tank on the top of the oxidation flocculation unit. A pH online monitor is installed in the water outlet tank. The pH online monitor is connected to the NaOH induction dosing pump. An umbrella-shaped diffuser is provided at the bottom of the water pipe, an aeration device is provided at the bottom of the oxidation flocculation unit, a mud collection bucket is provided under the aeration device, and a mud discharge pipe is provided below the mud collection bucket. The water pipe communicates with the central water inlet pipe in the sedimentation unit.

The aeration device has the same structure as the water distribution device, and is composed of a main pipe 4-14-1 and a branch pipe 4-14-2, and the branch pipe 4-14-2 is symmetrically and evenly arranged side, the branch pipe 4-14-2 is perpendicular to the main pipe 4-14-1, and the surface of the branch pipe 4-14-2 is provided with holes, which are evenly distributed in the vertical direction at an angle of 45° to the cross section of the branch pipe 4-14-2. both sides of the line. In order to prevent flocs or particles in the waste water from clogging the orifice, the main pipe 4-14-1 of the aeration device is connected to an external air compressor, and the air compressor feeds compressed air into the main pipe 4-14-1. Air, the holes of the aeration device are used for aeration, which can oxidize Fe ²⁺ (blue-green) to Fe ³⁺ (brown-yellow), which is more conducive to precipitation and can further reduce the chromaticity of the effluent to blow off the micro-electrolyte The fine particles and sludge on the surface of the filler can avoid the decrease of micro-electrolysis effect caused by the adhesion of particles during long-term use. The water distribution device is used for water distribution.

The central axis of the sedimentation unit is provided with a central water inlet pipe, and the upper part of the central water inlet pipe is vertically inserted into the water outlet tank on the top of the sedimentation unit. Inclined plate, for the flocs formed after Fenton reaction, due to the long aeration time, there are many tiny bubbles attached to the surface of the flocs, which are not easy to settle, and the effect of conventional sedimentation methods is not good; inclined plates are used to enhance the sedimentation effect; An umbrella-shaped diffuser is arranged at the bottom of the water pipe, a mud collecting bucket is arranged at the bottom of the sedimentation unit, and a mud discharge pipe is arranged under the mud collecting bucket.

The central water inlet pipe has a diameter of D, an umbrella-shaped diffuser is installed at the bottom, the corner of the diffuser is 30°, and the length of the bottom is (1.2-1.5) D. The diameter of the pipe shall not be less than 200mm to prevent mud from clogging and causing poor mud discharge.

A method for using a modular iron-carbon filler multi-stage micro-electrolysis-Fenton reaction device, the steps are:

A According to the above, construct the multistage micro-electrolysis-Fenton reaction device of a kind of modular iron-carbon filler;

B. Check and confirm that the mud discharge pipe is closed;

C. Close a valve on the outlet pipe connected to the micro-electrolysis unit, sewage inlet pump 1 and H ₂ O ₂ dosing pump 2, so that only one micro-electrolysis unit in the micro-electrolysis-Fenton reaction device can be used for sewage deal with;

D. Open another valve on the outlet pipe that communicates with the micro-electrolysis unit, sewage inlet pump 1 and H ₂ O ₂ dosing pump 2, so that only one micro-electrolysis unit in the micro-electrolysis-Fenton reaction device can be used Sewage treatment: turn on the H ₂ O ₂ dosing pump 2 to add H ₂ O ₂ to the sewage; the sewage enters the sewage inlet pipe through the sewage inlet pump 1, and the H ₂ O ₂ solution in the H ₂ O ₂ storage tank 2-1 passes through the H 2 O 2 ₂ O ₂ dosing pump 2, the H ₂ O ₂ dosing pipe 2-2 flows out from the cutting surface of the H ₂ O ₂ dosing pipe 2-2, enters the sewage inlet pipe, and merges with the sewage. The two are in the pipeline mixer 3 fully mixed;

The working principle of micro-electrolysis is:

When the wastewater is in full contact with the improved iron-carbon micro-electrolysis packing unit, a micro-electrolysis reaction occurs with iron as the anode and carbon (copper) as the cathode. The electrode reaction is as follows:

Anode (Fe): Fe-2e=Fe ²⁺ E ⁰ ＝-0.44V,

Cathode (C): 2H ⁺ +2e = H ₂ E ⁰ = 0V,

The following reactions occur at the cathode in the presence of oxygen:

O ₂ +4H ⁺ +4e＝H ₂ OE ⁰ ＝-1.23V

O ₂ +2H ₂ O+4e＝5OH ^-- E ⁰ ＝0.40V

Copper powder is used as the cathode material, the electrode potential under acidic conditions is: E ⁰ =-0.34V; the electrode potential under alkaline conditions: E ⁰ =-0.22V. The existence of copper powder expands the potential difference and applicable pH range of the micro-electrolysis reaction, that is, the micro-electrolysis reaction can continue to proceed under the pH neutral or even alkaline conditions where the traditional iron-carbon micro-electrolysis effect is not good, so that the waste water Pollutants are decomposed more thoroughly under the action of micro-electrolysis.

The Fenton reaction works as follows:

When hydrogen peroxide (H ₂ O ₂ ) is added to the micro-electrolysis reactor, the Fe ²⁺ produced by the micro-electrolysis reaction catalyzes the decomposition of H ₂ O ₂ to produce OH with strong oxidative properties:

Fe ²⁺ +H ₂ O ₂ ＝Fe ³⁺ +OH ^- +·OH E ⁰ ＝2.80V

·OH has a strong oxidizing ability, especially in acidic wastewater, second only to F in nature. Common small molecular organic compounds can be completely oxidized, and aromatic organic compounds and some heterocyclic organic compounds that are difficult to be oxidized by common oxidants can be almost completely degraded.

The sewage flowing out of the pipeline mixer 3 enters the water distribution device in the micro-electrolysis unit, flows into the main pipe 4-14-1 on the water distribution device, and flows out from the hole on the branch pipe 4-14-2. When it flows into the micro-electrolysis unit, the water level rises, and the sewage gradually contacts with each micro-electrolysis reaction layer. The sewage and the sheet-shaped filler 4-15-1, that is, the iron-carbon filler fully contacts. Under acidic conditions, the iron-carbon micro-electrolysis reaction occurs. The galvanic battery effect is formed between iron and carbon in wastewater, and the electrode potential difference is 1.2V. An electrochemical reaction occurs in an aqueous solution containing an acidic electrolyte, and the new ecological atoms [H] and Fe ²⁺ produced by the reaction can interact with many Oxidation-reduction reactions of the components can achieve the effects of reducing COD, increasing BOD, improving biodegradability (B/C) and decolorizing wastewater;

The added H ₂ O ₂ and the Fe ²⁺ produced by the iron-carbon micro-electrolysis reaction are mixed together, and under the acidic condition of pH less than 4, a Fenton reaction occurs to obtain OH with strong oxidation ability (oxidation electrode potential 2.80V) , so that the reaction of oxidizing and decomposing pollutants in wastewater has the advantages of rapid reaction, thorough oxidation, and no secondary pollution;

In summary, both the iron-carbon micro-electrolysis reaction and the Fenton reaction are carried out under acidic conditions, and the Fe ²⁺ produced during the iron-carbon micro-electrolysis process is one of the main agents for the Fenton reaction. Fenton oxidation technology is combined to form a new advanced oxidation technology for wastewater treatment - micro-electrolysis-Fenton oxidation technology. Under acidic conditions, Fe ²⁺ produced by iron-carbon micro-electrolysis reaction, and H ₂ added to wastewater O ₂ has a strong oxidation reaction, which reduces the dosage of Fe ²⁺ in the Fenton reaction and improves the device's ability to treat pollutants.

There are also some that are not oxygenated and aerated after Fenton oxidation, resulting in more Fe ²⁺ in the effluent, and the Fe(OH) ₂ formed after adding alkali is lighter in quality and difficult to precipitate, and the residual Fe ²⁺ in the wastewater develops color As a result, the chroma of the waste water is relatively high, and the visual perception is poor; the present invention neither directly aerates nor adds alkali, thus avoiding the occurrence of the above two situations.

E. After adding H ₂ O ₂ , the aeration device of the micro-electrolysis unit aerates for 10 to 15 minutes every 45 minutes; and in the commonly used micro-electrolysis-Fenton reaction device, most of the micro-electrolysis units add H Aeration starts after ₂ O ₂ , a large amount of oxygenation will convert Fe ²⁺ into Fe ³⁺ , and Fe ²⁺ is one of the main reagents for the Fenton reaction, which will slow down the Fenton reaction rate and reduce the oxidation effect of pollutants The present invention aerates after an interval of 45 minutes without converting Fe ²⁺ into Fe ³⁺ , and the Fe ²⁺ produced by iron-carbon micro-electrolysis can increase the Fenton reaction rate and enhance the oxidation effect of pollutants. The sediment after iron-carbon reaction, Fenton reaction and aeration, the impurities and sediment in the sewage all sink into the mud collecting bucket;

In addition, the iron sludge that falls off from the upper layer of the micro-electrolysis reaction layer may adhere to the surface of the micro-electrolysis reaction layer, so the micro-electrolysis unit is intermittently aerated to desorb the iron sludge on the surface of the micro-electrolysis reaction layer. Improve the reaction effect of micro-electrolysis-Fenton device.

The micro-electrolysis reaction layer is composed of a support plate and a modular packing 4-15, and the modular packing 4-15 is arranged side by side on the support plate, and the modular packing 4-15 is composed of a sheet-shaped packing 4-15-1 , PVC bracket 4-15-2, the PVC bracket 4-15-2 is a cuboid shape with a built-in slot, and the sheet filler 4-15-1 is vertically inserted into the slot;

The mass parts and mesh numbers of each component in the flake filler 4-15-1 are respectively:

Cast iron or pig iron filings: 55-60 parts, 50-60 mesh;

Coke powder: 30-35 parts, 60-70 mesh;

Copper powder: 5-10 parts, 50-60 mesh;

Binder: 3 to 5 parts;

The binder includes fine yellow sand and Portland cement, with a mass ratio of 1:2 to 3;

Its production steps are as follows:

The wire mesh with the size of 8*8*0.8 is used as the skeleton. After high-pressure pressing and molding, it is calcined at a high temperature with nitrogen filling at a temperature of 1050-1200°C, and the firing time is 4-5 hours. The appearance size of the finished sheet packing 4-15-1 is: 140mm (length)×140mm (width)×8mm (thickness).

Due to the addition of copper, it forms a larger potential difference than traditional iron-carbon fillers, and has the characteristics of no passivation, no fragmentation, and no agglomeration during use; the number of sheet-like filler units in the modular filler 4-15 can be viewed The water quality of the wastewater can be flexibly grasped and appropriately increased or decreased; the support plate is made of glass fiber reinforced plastic gratings and bears heavy loads.

The shape of the traditional iron-carbon fillers used is generally spherical, granular, ring-shaped or small flakes. They are generally formed by physical pressing and have not been solidified by high-temperature firing. They are easy to soften, loosen, and be compacted during use. After long-term operation, the fillers The surface is easy to fall off to form a passivation film, and some suspended particles such as iron-carbon mud are gradually deposited on the surface of the filler at the bottom, which blocks the effective contact between the filler and the wastewater, resulting in a reduction in the wastewater treatment effect; the present invention adopts this form of layer separation, Avoiding the deposition of suspended particles on the surface of the filler, so that the iron-carbon filler can effectively and fully contact the wastewater, and improve the wastewater treatment effect;

In traditional iron-carbon micro-electrolysis reactors, the fillers are generally in a landfill state. When in use, they are piled together without a relatively fixed structural support. After long-term operation, the size of the fillers becomes smaller, and the porosity between the fillers decreases; the upper layer contains more iron and is heavier. The filling gradually sinks, crushing the smaller filling in the lower layer and causing uneven distribution of filling in the pool, forming a cut-off or dead water area, which not only affects the flow state of wastewater, but also affects the effect of micro-electrolysis, resulting in a decrease in treatment efficiency and making subsequent replacement of filling difficult. increase; even if all the waste water in the reactor is emptied to clean up, if the exposure time is longer, the whole packing layer may be all agglomerated, causing the whole reactor to be scrapped; the present invention arranges multi-layer micro-electrolysis reaction layers in the micro-electrolysis unit, The layers are separated, and each layer is supported by a support plate. There are multiple sets of modular packing 4-15 arranged side by side on the support plate. The modular packing 4-15 is composed of sheet packing 4-15-1, PVC Bracket 4-15-2, the PVC bracket 4-15-2 is a cuboid shape with a built-in card slot, the sheet filler 4-15-1 is inserted vertically into the card slot, long-term operation, no There is a phenomenon of filler sinking, resulting in uneven distribution, and the formation of cut-off or dead water areas, and there is no agglomeration or the reactor is scrapped. The micro-electrolysis efficiency is stable and efficient. After a period of operation, the micro-electrolysis reaction layer can be Take it out, the PVC bracket 4-15-2 can be recycled, and continue to use after replacing the filler, which is convenient for operation, saves costs, improves the utilization rate of the filler, and improves the sewage treatment effect;

The overall dimensions of the PVC bracket 4-15-2 are: 150mm (length) × 150mm (width) × 150mm (height), there are slots reserved inside, and a maximum of 6 pieces of sheet packing 4-15-1 can be inserted; A certain gap is left between the fillers 4-15-1, which is beneficial for the waste water to pass through and the iron sludge formed by the reaction to fall into the mud collecting hopper at the bottom of the pool.

In the commonly used iron-carbon micro-electrolysis-Fenton reaction device, the micro-electrolysis fillers are stacked together as a layer. Due to the limited load-bearing capacity of the support plate, the thickness of the filler layer is generally small. After the wastewater passes through the micro-electrolysis layer, it continues to push upward. In the micro-electrolysis unit, the micro-electrolysis reaction layer cannot be contacted again, and the micro-electrolysis effect is limited; the present invention sets a multi-layer micro-electrolysis reaction layer in the micro-electrolysis unit, and the layers are separated, and each layer is supported by a support plate. Modular filler 4-15, the upward push flow of wastewater can contact with multi-layer micro-electrolysis reaction layer, which increases the contact time between wastewater and filler, the treatment efficiency is better than traditional micro-electrolysis filler, and the treatment effect is stable.

F. The aeration device at the bottom of the oxidation flocculation unit aerates continuously, and the air-water ratio is 6-15:1; the sewage with Fe ²⁺ in the micro-electrolysis unit flows into the center of the oxidation flocculation unit through the outlet pipe on the outlet tank. In the water pipe, the umbrella-shaped diffuser at the bottom of the central water inlet pipe enters the bottom of the oxidation flocculation unit; the inlet of the aeration device at the bottom of the oxidation flocculation unit is continuously aerated with an air-to-water ratio of 6 to 15:1, and the Fe ²⁺ in the wastewater is After oxidation to Fe ³⁺ , remove the chroma of sewage;

G. When the wastewater level reaches the outlet tank, the pH online monitor in the outlet tank monitors the pH value of the wastewater. When the pH is less than 6, the NaOH induction dosing pump is automatically turned on, and the NaOH solution is added to the central water inlet pipe to generate The floc Fe(OH) ₃ further entrains pollutants and settles into the mud collecting bucket;

Adding NaOH to the effluent after micro-electrolysis-Fenton reaction and continuously oxygenating can play the following roles: oxidize the residual Fe ²⁺ in the wastewater to Fe ³⁺ , remove the color of Fe ²⁺ , and avoid the effluent from returning to color Phenomenon; to further oxidize and decompose organic matter in wastewater; to form flocs under alkaline conditions, and aeration plays a stirring role.

H. After the oxidation flocculation unit is treated, the wastewater flows from the outlet pipe at the bottom of the right side of the outlet tank into the center inlet pipe of the sedimentation unit, and enters the bottom of the sedimentation unit for further precipitation. In the mud collecting hopper, the water level of the treated wastewater gradually rises and enters the next process through the outlet pipe in the sedimentation unit;

I. When the mud collecting bucket of any unit in the micro-electrolysis unit, oxidation flocculation unit and sedimentation unit is full of sediment, open the corresponding mud discharge pipe to discharge mud;

J. When the modular filler in the micro-electrolysis unit is used up, or when it is out of service for maintenance, turn off the sewage inlet pump ₁ and the H2O2 dosing pump ₂ , and turn on the water pump installed on the outlet pipe of the micro-electrolysis unit. All the wastewater in the micro-electrolysis unit is sent to the oxidation flocculation unit, close the valve on the outlet pipe connected to this micro-electrolysis unit, open the valve on the outlet pipe connected to another micro-electrolysis unit, sewage inlet pump and _{H2O 2} dosing pumps to ensure continuous and uninterrupted sewage treatment.

K. Remove the water outlet tank in the micro-electrolysis unit with the sewage inlet pump 1 and H ₂ O ₂ dosing pump 2 closed, take out the micro-electrolysis layers in the micro-electrolysis unit in turn, and then put in new micro-electrolysis layers in turn, The outlet tank is placed on the micro-electrolysis unit for the next time the micro-electrolysis unit being used is out of service for maintenance or when the modular filler 4-15 is used up.

The multi-stage micro-electrolysis-Fenton reflection device of the present invention can be used in small-scale sewage treatment systems as well as large-scale urban sewage treatment systems. It only needs to design structural dimensions with different parameters and technical characteristics according to different application occasions.

Example 2

A printing and dyeing factory has high-concentration production wastewater, the wastewater production volume is about 300t/d; pH3.3-4.6, average value 3.9; COD5000-9200mg/L, average value 7300mg/L; B/C<0.15, wastewater biodegradability is poor . A multi-stage micro-electrolysis-Fenton reaction device with modular iron-carbon filler is proposed, as shown in Figure 1-4, its structure and use method are the same as in Example 1, wherein, H ₂ O ₂ dosing tube 2-2 The distance between the position connected with the sewage inlet pipe and the pipeline mixer 3 is 301 mm, the number of micro-electrolysis reaction layers is ₃ layers, and the diameter of the sludge discharge pipe is 201 mm. After adding H2O2, the micro _- electrolysis unit The aeration device aerates for 10 minutes every 45 minutes, 200 sets of modular fillers 4-15 are arranged side by side on the support plate, and the number of sheet-shaped fillers 4-15-1 in each layer of micro-electrolysis reaction layer is 600 pieces .

The outlet of the H ₂ O ₂ dosing pipe 2-2 in the sewage inlet pipe is cut along the opposite side of the water flow direction, and the cutting surface forms an angle of 45° with the water flow direction; the central water inlet pipe has a diameter of D, and an umbrella-shaped diffuser is installed at the bottom. The corner of the diffuser is 30°, and the length of the bottom is 1.2D; the mass parts and mesh numbers of the components in the sheet packing 4-15-1 are respectively:

Cast iron or pig iron filings: 55 parts, 50 mesh;

Coke powder: 30 parts, 60 mesh;

Copper powder: 5 parts, 50 mesh;

Binder: 3 parts;

The binder includes fine yellow sand and Portland cement, with a mass ratio of 1:2; after high-pressure pressing, it is fired in a furnace filled with nitrogen at a high temperature, at a temperature of 1050°C, and the firing time is 4 hours.

The number of branch pipes 4-14-2 is 8 pairs and 16 in total, and there are two holes forming a pair on each branch pipe 4-14-2, totaling 7 pairs.

The waste water is pumped into the device from the bottom, the hydraulic retention time is controlled to 60min, the dosage of hydrogen peroxide is 4.0mL/L, the aeration is performed for 10 minutes every 45 minutes, and the air-water ratio is 6:1; continuous aeration in the oxidation flocculation reactor , the gas-water ratio is 6:1, the water quality of the treated effluent is: pH 6.7, COD 3160mg/L, COD removal rate 56.7%, B/C=0.36, the biodegradability of wastewater has been greatly improved, and the reaction during use The improved iron-carbon filler in the device did not appear to be clogged, broken or hardened, and the integrated device was in good condition.

Example 3

High-concentration pesticide production wastewater from a factory in Jiangsu, the wastewater production volume is about 90t/d; pH1.8-3.2, average value 2.6; COD4200-6500mg/L, average value 5100mg/L; B/C<0.15, the biodegradability of wastewater is relatively low Poor, a multi-stage micro-electrolysis-Fenton reaction device with modular iron-carbon filler is proposed, as shown in Figure 1-4, its structure and method of use are the same as in Example 1, wherein the H ₂ O ₂ dosing tube 2 -2 The distance between the position connected with the sewage inlet pipe and the pipeline mixer 3 is 500mm, the number of micro-electrolysis reaction layers is ₆ layers, and the diameter of the sludge discharge pipe is 300mm. After adding H2O2, micro _- electrolysis The aeration device of the unit is aerated for 15 minutes at intervals of 45 minutes, and 150 groups of modular fillers 4-15 are arranged side by side on the support plate, and the quantity of sheet-like fillers 4-15-1 in each layer of micro-electrolysis reaction layer is 900 tablets.

The outlet of the H ₂ O ₂ dosing pipe 2-2 in the sewage inlet pipe is cut along the opposite side of the water flow direction, and the cutting surface forms an angle of 60° with the water flow direction; the central water inlet pipe has a diameter of D, and an umbrella-shaped diffuser is installed at the bottom. The corner of the diffuser is 30°, and the length of the bottom is 1.5D; the mass parts and mesh numbers of the components in the sheet packing 4-15-1 are respectively:

Cast iron or pig iron filings: 60 parts, 60 mesh;

Coke powder: 35 parts, 70 mesh;

Copper powder: 10 parts, 60 mesh;

Binder: 5 parts;

The binder includes fine yellow sand and Portland cement, with a mass ratio of 1:3; after high-pressure compression molding, it is fired in a furnace filled with nitrogen at a high temperature at a temperature of 1200°C, and the firing time is 5 hours.

The number of branch pipes 4-14-2 is 10 pairs, 20 in total, and each branch pipe 4-14-2 has two holes forming a pair, altogether 9 pairs.

The waste water is pumped into the device from the bottom, the hydraulic retention time is controlled to be 120min, the dosage of hydrogen peroxide is 3.0mL/L, aeration is performed for 15 minutes every 45 minutes, and the gas-water ratio is 10:1; continuous aeration is carried out in the oxidation flocculation reactor , the air-water ratio is 12:1, the treated effluent quality is: pH 6.4, COD 1780mg/L, COD removal rate 65.10%, B/C=0.39, and the biodegradability of wastewater has been greatly improved. During use, the improved iron-carbon filler in the reactor did not appear to be clogged, broken or compacted, and the integrated device was in good condition.

Example 4

A high-concentration coking wastewater in Zhejiang, the wastewater production volume is about 420t/d, the measured wastewater quality in the adjustment tank is about: pH4.5, chroma 1200, COD5860mg/L, B/C<0.15. A multi-stage micro-electrolysis-Fenton reaction device with modular iron-carbon filler is proposed, as shown in Figure 1-4, its structure and use method are the same as in Example 1, wherein, H ₂ O ₂ dosing tube 2-2 The distance between the position connected with the sewage inlet pipe and the pipeline mixer 3 is 800mm, the number of micro-electrolysis reaction layers is ₅ layers, and the diameter of the sludge discharge pipe is 500mm. After adding H2O2, the micro _- electrolysis unit The aeration device aerates for 13 minutes every 45 minutes, 180 sets of modular fillers 4-15 are arranged side by side on the support plate, and the number of sheet-like fillers 4-15-1 in each layer of micro-electrolysis reaction layer is 1800 pieces .

The outlet of the H ₂ O ₂ dosing pipe 2-2 in the sewage inlet pipe is cut along the opposite side of the water flow direction, and the cutting surface forms an angle of 50° with the water flow direction; the central water inlet pipe has a diameter of D, and an umbrella-shaped diffuser is installed at the bottom. The corner of the diffuser is 30°, and the length of the bottom is 1.4D; the mass parts and mesh numbers of the components in the sheet packing 4-15-1 are respectively:

Cast iron or pig iron filings: 58 parts, 55 mesh;

Coke powder: 34 parts, 67 mesh;

Copper powder: 7 parts, 56 mesh;

Binder: 4 parts;

The binder includes fine yellow sand and Portland cement, with a mass ratio of 1:2.8; after high-pressure pressing, it is fired in a furnace filled with nitrogen at a high temperature, at a temperature of 1100°C, and the firing time is 4.5 hours.

The number of branch pipes 4-14-2 is 9 pairs and 18 in total, and each branch pipe 4-14-2 has two holes forming a pair, altogether 8 pairs.

Control the hydraulic retention time to 90 minutes, the dosage of hydrogen peroxide is 6.0mL/L, aerate for 15 minutes every 45 minutes, and the air-water ratio is 15:1; continuous aeration in the oxidation flocculation reactor, the air-water ratio is 15:1 , The quality of the treated effluent is: pH 6.8, COD 1840mg/L, COD removal rate 68.6%, B/C=0.37, and the biodegradability of wastewater has been greatly improved. During use, the improved iron-carbon filler in the reactor did not appear to be clogged, broken or compacted, and the integrated device was in good condition.

Claims (9)

1. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler, including wastewater influent pump (1), H₂O₂Add dress To put and pipe-line mixer (3), it is characterised in that it also includes light electrolysis-Fenton's reaction device, wherein, the wastewater influent pump (1) it is arranged on sewage water inlet pipe, sewage water inlet pipe and the H₂O₂After throwing device connection, H₂O₂Throwing device with it is described Pipe-line mixer (3) is connected, and described pipe-line mixer (3) is connected by pipeline with the light electrolysis-Fenton's reaction device；

The light electrolysis-Fenton's reaction device includes four units, wherein having two light electrolysis units, an oxidizing, flocculating unit With a precipitation unit, two light electrolysis units connect after being connected with oxidizing, flocculating unit, oxidizing, flocculating unit and precipitation unit Connection, described precipitation unit side are provided with outlet pipe, and described precipitation unit bottom is provided with discharge pipeline；The light electrolysis unit Bottom be provided with discharge pipeline；

Be provided with NaOH automatic medicament feeding systems above the oxidizing, flocculating unit, NaOH automatic medicament feeding systems by NaOH solution storage tank, NaOH chemical feed pipes and NaOH sensing dosing pump compositions, the bottom of described NaOH solution storage tank connects with NaOH chemical feed pipes, described NaOH chemical feed pipes be provided with NaOH sensing dosing pumps, described NaOH chemical feed pipes are stretched into the water inlet pipe of center, center water inlet pipe It is arranged on the central axis of oxidizing, flocculating unit, the water outlet at the top of the Upper vertical insertion oxidizing, flocculating unit of center water inlet pipe PH on-line computing models are provided with groove, in effluent trough, described pH on-line computing models are connected with NaOH sensing dosing pumps, effluent trough Bottom right side is provided with outlet pipe, and center water inlet bottom of the tube is provided with umbrella shape diffuser, and the bottom of oxidizing, flocculating unit, which is provided with, to expose Device of air, sludge hopper is provided with below aerator, is provided with discharge pipeline below sludge hopper, in the oxidizing, flocculating unit Outlet pipe connected with the center water inlet pipe in precipitation unit.

2. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 1, its feature exist In the H₂O₂Throwing device includes H₂O₂Storage tank (2-1), H₂O₂Chemical feed pipe (2-2) and H₂O₂Dosing pump (2)；Described H₂O₂Storage The bottom of groove (2-1) and H₂O₂Chemical feed pipe (2-2) connects, described H₂O₂Chemical feed pipe (2-2) is provided with H₂O₂Dosing pump (2).

3. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 2, its feature exist In the H₂O₂Vertical line of the chemical feed pipe (2-2) along sewage water inlet pipe is inserted into the center position of cross section, H₂O₂Chemical feed pipe (2- 2) outlet in sewage water inlet pipe, to be cut along water (flow) direction reverse side, cutting face and water (flow) direction be at 45 °~60 ° of angles, H₂O₂ The distance between opening position that chemical feed pipe (2-2) connects with sewage water inlet pipe and pipe-line mixer (3) are more than 300mm.

4. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 1, its feature exist In, the bottom of the light electrolysis unit is provided with discharge pipeline, and discharge pipeline is connected with sludge hopper, and aerator is provided with sludge hopper, Water-distributing device is provided with above aerator, is provided with 3-6 layer micro-electrolysis reaction layers above water-distributing device, on micro-electrolysis reaction layer Side is provided with effluent trough, and effluent trough bottom right side is provided with outlet pipe, plane where plane, water-distributing device where aerator with Plane where micro-electrolysis reaction layer is parallel to each other, and described water-distributing device is connected by pipeline with described pipe-line mixer (3), Described outlet pipe connects with the center water inlet pipe in oxidizing, flocculating unit.

5. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 1, its feature exist In the central axis of the precipitation unit is provided with center water inlet pipe, center water inlet pipe Upper vertical insertion precipitation unit top Effluent trough in, the side bottom of effluent trough connects with outlet pipe, and center water inlet pipe, which passes through, is arranged on swash plate in precipitation unit, Center water inlet bottom of the tube is provided with umbrella shape diffuser, and precipitation unit bottom is provided with sludge hopper, spoil disposal is provided with below sludge hopper Pipe；

The center water inlet pipe, a diameter of D, bottom set umbrella shape diffuser, 30 ° of diffuser corner, bottom lengths for (1.2~ 1.5) D, the sludge hopper front view are shaped as upside-down trapezoid, and the spoil disposal pipe diameter is not less than 200mm.

6. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 4, its feature exist In described aerator is identical with water-distributing device structure, is made up of main (4-14-1), branch pipe (4-14-2), branch pipe (4- Main (4-14-1) both sides 14-2) are symmetrically and evenly arranged on, branch pipe (4-14-2) is vertical with main (4-14-1), branch pipe Hole is provided with (4-14-2) surface, vertical line two is evenly distributed in 45 ° of angles with branch pipe (4-14-2) cross section vertical direction Side, the main (4-14-1) of described aerator are connected with the air compressor machine of peripheral hardware.

7. a kind of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 4, its feature exist In the micro-electrolysis reaction layer is made up of supporting plate and module type filler (4-15), and module type is set side by side with supporting plate and is filled out Expect (4-15), described module type filler (4-15) is made up of laminal filter (4-15-1), PVC brackets (4-15-2), described PVC brackets (4-15-2) are cuboid-type, built-in neck, and described laminal filter (4-15-1) is inserted vertically into neck, every layer 600~1800 laminal filters (4-15-1) are shared on micro-electrolysis reaction layer.

8. a kind of application method of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler, step are：

A. a kind of multistage light electrolysis-Fenton's reaction device of described module type iron carbon filler is built according to claim 1；

B. discharge pipeline is reviewed and validate to be closed；

C. valve, wastewater influent pump (1) and the H closed on an outlet pipe connected with light electrolysis unit₂O₂Dosing pump (2), makes Light electrolysis unit in light electrolysis-Fenton's reaction device only has one and can be used in sewage disposal；

D. valve, wastewater influent pump (1) and the H on the outlet pipe that another is connected with light electrolysis unit are opened₂O₂Dosing pump (2), The light electrolysis unit in light electrolysis-Fenton's reaction device is only had one and can be used in sewage disposal；Open H₂O₂Dosing pump (2) H is added into sewage₂O₂；

E. H is added₂O₂After end, the aerator of light electrolysis unit was aerated 10~15 minutes at interval of 45 minutes；

F. the aerator continuous aeration of oxidizing, flocculating unit bottom, gas-water ratio 6~15：1；Fe is carried in light electrolysis unit²⁺ Sewage flowed into by the outlet pipe on effluent trough in the center water inlet pipe of oxidizing, flocculating unit, by center intake bottom of the tube umbrella Shape diffuser enters the bottom of oxidizing, flocculating unit；By the aerator entrance of oxidizing, flocculating unit bottom, continuous aeration, air water Than 6~15：1, by Fe in waste water²⁺It is oxidized to rear Fe³⁺, remove the colourity of sewage；

G. when waste water level is reached in effluent trough, the pH on-line computing models in effluent trough, the pH value of waste water is monitored, when pH is less than 6 When automatically turn on NaOH sensing dosing pump, NaOH solution is added in the water inlet pipe of center, generation floccule Fe (OH)₃, enter one Step sweeps along pollutant to be deposited in sludge hopper；

H. waste water is flowed into the center water inlet of precipitation unit by the outlet pipe of effluent trough bottom right side after oxidizing, flocculating cell processing Guan Li, precipitation unit bottom is entered, is further precipitated, swash plate stops that the sediment in waste water further precipitates, and sinks Form sediment in sludge hopper, the waste water level after processing gradually rises is discharged by the outlet pipe in precipitation unit, at subsequent processing Reason；

I. when being full of sediment in the sludge hopper of any cell in light electrolysis unit, oxidizing, flocculating unit and precipitation unit, beat Discharge pipeline carries out spoil disposal corresponding to opening；

J. when the module type filler (4-15) in light electrolysis unit has used, or stop transport when safeguarding, close wastewater influent pump (1) and H₂O₂Dosing pump (2), the suction pump opened on the outlet pipe of light electrolysis unit all send the waste water in light electrolysis unit Enter in oxidizing, flocculating unit, the valve closed on the outlet pipe connected with this light electrolysis unit, open and another light electrolysis list Valve, wastewater influent pump (1) and H on the outlet pipe of member connection₂O₂Dosing pump (2), it is ensured that sewage disposal is continuously uninterruptedly entered OK；

K. remove and close wastewater influent pump (1) and H₂O₂Effluent trough in the light electrolysis unit of dosing pump (2), by light electrolysis list Micro-electrolysis reaction layer in member is taken out successively, then is sequentially placed into new micro-electrolysis reaction layer, and effluent trough is positioned over into light electrolysis list In member, enabled when in case the light electrolysis unit being used next time is stopped transport, maintenance or module type filler (4-15) have used.

A kind of 9. user of multistage light electrolysis-Fenton's reaction device of module type iron carbon filler according to claim 8 Method, it is characterised in that the micro-electrolysis reaction layer is made up of supporting plate and module type filler (4-15), is set up in parallel in supporting plate There are 600~1800 module type fillers (4-15), described module type filler (4-15) is held in the palm by laminal filter (4-15-1) and PVC Frame (4-15-2) forms, and described PVC brackets (4-15-2) are cuboid-type, built-in neck, described laminal filter (4-15- 1) it is inserted vertically into neck；

The mass fraction of each component and mesh number are respectively in described laminal filter (4-15-1)：

Cast iron or pig scrap：55~60 parts, 50~60 mesh；

Coke blacking：30~35,60~70 mesh；

Copper powder：5~10,50~60 mesh；

Binding agent：3~5；

Binding agent includes fine sand and portland cement, mass ratio 1:2~3；

After high pressure is compressing, enter stove nitrogen charging high-temperature calcination shaping, temperature is：1050~1200 DEG C, the firing time is：4~5 Hour.