CN110052106B

CN110052106B - Comprehensive treatment system and method for three wastes of copper-containing industrial sludge

Info

Publication number: CN110052106B
Application number: CN201910407233.6A
Authority: CN
Inventors: 余志新; 李江枫
Original assignee: Kaiping Xinlong Recycling And Processing Factory Co ltd
Current assignee: Kaiping Xinlong Recycling And Processing Factory Co ltd
Filing date: 2019-05-15
Publication date: 2024-04-19
Anticipated expiration: 2039-05-15

Abstract

The invention relates to a comprehensive treatment system and method for three wastes of copper-containing industrial sludge, and belongs to the technical field of environmental protection. The processing apparatus includes: the copper-containing industrial sludge three-waste comprehensive treatment system is matched with the solid waste treatment equipment, the waste gas treatment equipment and the sewage treatment equipment, and can effectively carry out comprehensive treatment on solid, liquid and gas three phases of heavy metal-containing hazardous waste sludge, thereby achieving the purposes of reducing, harmlessly and recycling the hazardous waste sludge three-waste. And exhaust gas treatment is carried out through the pretreatment tower and the cooperative absorption tower (WLT tower), so that the desulfurization rate and the dust removal rate are improved, meanwhile, the severe smoke property is adjusted through the pretreatment tower, part of smoke dust and sulfur dioxide are removed in advance, the smoke temperature is reduced, the internal equipment of the subsequent WLT tower is protected, and the service life of the subsequent equipment is prolonged.

Description

Comprehensive treatment system and method for three wastes of copper-containing industrial sludge

Technical Field

The invention relates to the technical field of environmental protection, in particular to a comprehensive treatment system and method for three wastes of copper-containing industrial sludge.

Background

With the development of the age, people increasingly recognize the importance of environmental protection, and environmental protection has become one of important guarantee conditions for the sustainable development of countries and nations. However, some sludge is inevitably generated in modern industrial production, and industrial sludge can be classified into dangerous waste and general industrial waste according to management attributes, and the treatment of dangerous waste sludge is a difficult point and an important point in the industry.

At present, a comprehensive treatment process for the solid, liquid and gas three phases of the hazardous waste is not designed in the hazardous waste treatment industry, and the patent innovatively designs a set of process capable of effectively carrying out comprehensive treatment on the solid, liquid and gas three phases of the hazardous waste sludge containing heavy metals, so that the purposes of reducing, harmlessly and recycling the three wastes of the hazardous waste sludge are achieved.

Disclosure of Invention

Based on the above, it is necessary to provide a comprehensive treatment system and method for three wastes of copper-containing industrial sludge, by adopting the equipment and method, copper and nickel compounds in hazardous waste sludge are recycled by means of filter pressing, drying and smelting, and wastewater and waste gas containing heavy metal components generated in the production process are subjected to harmless treatment, recycling and standard-reaching emission.

A copper-containing industrial sludge three-waste comprehensive treatment system, comprising:

The solid waste treatment equipment comprises a filter press, a drying assembly, a brick making machine and a smelting furnace, wherein the filter press, the drying assembly, the brick making machine and the smelting furnace are sequentially arranged according to the process flow;

The waste gas treatment equipment comprises a multi-stage surface cooler, a first bag type dust collector, a second bag type dust collector, a pretreatment tower, an absorption tower and a wet electrostatic dust collector, wherein the pretreatment tower, the absorption tower and the wet electrostatic dust collector are sequentially communicated through pipelines, the first bag type dust collector and the second bag type dust collector are both communicated with the pretreatment tower, an exhaust pipeline of the drying assembly is connected with the first bag type dust collector, and an exhaust pipeline of the smelting furnace is communicated with the second bag type dust collector through the multi-stage surface cooler;

The sewage treatment equipment comprises a concentrate pond, a clear liquid pond, a primary sedimentation pond, an acid regulating pond, an oxidation pond, an alkali regulating pond, a coagulation pond, a flocculation pond, a sludge sedimentation pond, a sand filtering device, a carbon filtering device, a cotton core filter and a reverse osmosis device which are sequentially communicated through pipelines, wherein a reverse osmosis membrane is arranged in the reverse osmosis device to divide the reverse osmosis device into a concentrate cavity and a clear liquid cavity, the concentrate cavity is communicated with the concentrate pond, and the clear liquid cavity is communicated with the clear liquid pond; the primary sedimentation tank is communicated with a sewage discharge pipeline of the filter press, and the concentrated liquid tank is communicated with the primary sedimentation tank.

The copper-containing industrial sludge three-waste comprehensive treatment system is matched with solid waste treatment equipment, waste gas treatment equipment and sewage treatment equipment, can effectively carry out comprehensive treatment on solid, liquid and gas three phases of heavy metal-containing hazardous waste sludge, and achieves the purposes of reducing, harmlessly and recycling the hazardous waste sludge three-waste. And exhaust gas treatment is carried out through the pretreatment tower and the cooperative absorption tower (WLT tower), so that the desulfurization rate and the dust removal rate are improved, meanwhile, the severe smoke property is adjusted through the pretreatment tower, part of smoke dust and sulfur dioxide are removed in advance, the smoke temperature is reduced, the internal equipment of the subsequent WLT tower is protected, and the service life of the subsequent equipment is prolonged.

In one embodiment, the bottoms of the sludge sedimentation tank and the primary sedimentation tank are respectively provided with a sludge return pipeline which is communicated with the filter press;

And the reuse water tank is communicated with the absorption tower and the wet electrostatic precipitator through pipelines.

The waste gas treatment equipment further comprises a spraying slurry circulation system, wherein the spraying slurry circulation system comprises a calcium-based absorbent storage bin, a digestion device, a pulping pool and a circulation pool which are sequentially communicated through pipelines, the circulation pool provides fresh absorption slurry to the pretreatment tower and the absorption tower through a supply pipeline, and the fresh absorption slurry is communicated with the bottoms of the pretreatment tower and the absorption tower through a recovery pipeline to recover the absorption slurry.

The spraying slurry circulating system further comprises a sedimentation tank, an oxidation tank, calcium-based recovery filter pressing equipment and an oxidation fan, wherein the oxidation tank is communicated with the circulating tank and the sedimentation tank through pipelines, the oxidation fan is provided with an aeration pipe, and the aeration pipe extends into the oxidation tank; the bottom of the sedimentation tank is provided with a pipeline communicated with the calcium-based recovery filter pressing equipment.

The reuse water tank is respectively communicated with the digestion device and the circulating tank through pipelines.

In one embodiment, the solid waste treatment device further comprises an automatic feeding system, wherein the automatic feeding system comprises a movable material collecting box, a first mechanical arm, a second mechanical arm, a third mechanical arm, a fourth mechanical arm, a fifth mechanical arm, a sixth mechanical arm, a first conveyor belt, a second conveyor belt and a third conveyor belt; the outlet end of the filter cake of the filter press corresponds to the initial position of the material collecting box; one end of the first conveyor belt corresponds to the initial position of the collection box, the other end of the first conveyor belt corresponds to the drying assembly, the first mechanical arm is arranged between the initial position of the collection box and the first conveyor belt and used for grabbing the collection box on the first conveyor belt, and the second mechanical arm is arranged between the first conveyor belt and the drying assembly and used for grabbing the collection box on the drying assembly; one end of the second conveyor belt corresponds to the drying assembly, the other end of the second conveyor belt corresponds to the brick making machine, the third mechanical arm is arranged between the drying assembly and the second conveyor belt and used for grabbing the material collecting box on the second conveyor belt, and the fourth mechanical arm is arranged between the second conveyor belt and the brick making machine and used for grabbing and pouring the material in the material collecting box in the brick making machine; one end of the third conveyor belt corresponds to the brick making machine, the other end of the third conveyor belt corresponds to the smelting furnace, the fifth mechanical arm is arranged between the brick making machine and the third conveyor belt and used for grabbing materials after brick making on the third conveyor belt through the material collecting box, and the sixth mechanical arm is arranged between the third conveyor belt and the smelting furnace and used for grabbing and dumping the materials in the material collecting box in the smelting furnace.

At present, the dangerous waste treatment smelting process usually adopts manpower feeding and forklift transportation, and has heavier burden and dependence on workers, while the invention adopts automatic equipment to carry out material transportation, loading and unloading, thereby greatly reducing the manpower burden, ensuring that the drying and smelting processes are more coherent and quicker, and improving the smelting efficiency.

The drying assembly comprises a drying chamber, a raking mechanical arm, a temperature and humidity probe, an infrared sensor and a PLC control system; the drying chamber is divided into a bottom layer for containing fuel and an upper layer for containing drying materials; the temperature and humidity probes are arranged on the upper layer at intervals in the vertical direction, and the temperature and humidity probes are also arranged on a chamber door, an air supply opening and an exhaust port of the drying chamber; the PLC control system is electrically connected with the raking mechanical arm and controls the raking mechanical arm; the temperature and humidity probe is electrically connected with the PLC control system and transmits signals to the PLC control system; the infrared sensor is arranged at a preset height of the drying chamber and transmits a signal to the PLC control system.

The existing dangerous waste treatment drying process depends on manual operation and has great damage to workers, and the drying assembly for the drying process adopts automatic equipment, adopts a temperature and humidity probe and an infrared sensor as detection probes for real-time monitoring feedback, and adopts the automatic equipment for feeding, raking and material transportation, loading and unloading, so that the drying process is more coherent and quicker while the labor burden is reduced, and the influence on waste gas pollutant detection caused by the rise of the oxygen content of the flue gas due to the long-time opening of a drying chamber door is reduced.

The solid waste treatment equipment is also provided with a concentrated solution spraying system, the concentrated solution spraying system is arranged on cooling and spraying slag of the smelting furnace, and the primary sedimentation tank is communicated with the primary sedimentation tank through the concentrated solution spraying system.

In one embodiment, the sewage treatment equipment further comprises an automatic feeding system for automatic feeding, wherein the automatic feeding system comprises a reagent storage tank, a metering pump and a discharge back pressure valve, and the reagent storage tank is sequentially communicated with the metering pump and the discharge back pressure valve through pipelines;

The automatic feeding system further comprises a pulsation damper, a protection loop and a flow correction loop, wherein the pulsation damper is arranged on a pipeline between the reagent storage tank and the metering pump, the protection loop is communicated with the metering pump and the reagent storage tank, and a pressure gauge and a protection back pressure valve are arranged on the protection loop; one end of the flow correction loop is communicated with the reagent storage tank, and the other end of the flow correction loop is communicated with a pipeline between the metering pump and the reagent storage tank.

The acid regulating tank, the oxidation tank, the alkali regulating tank, the coagulation tank and the flocculation tank are all provided with the automatic feeding system.

And stirring systems for stirring liquid in the tanks are arranged in the primary sedimentation tank, the acid regulating tank, the oxidation tank, the alkali regulating tank, the coagulation tank, the flocculation tank and the sludge sedimentation tank.

In one embodiment, the exhaust gas treatment device further comprises a secondary combustion chamber, wherein the secondary combustion chamber is arranged between the exhaust pipeline of the drying assembly and the first bag type dust collector, and the secondary combustion chamber is further provided with a fuel spraying system for spraying fuel and a blast system for supporting combustion.

The waste gas treatment equipment further comprises a waste heat boiler and heating heat exchange equipment, wherein the waste heat boiler and the heating heat exchange equipment are sequentially communicated between the secondary combustion chamber and the first bag type dust collector, and a flue gas pipeline of the waste heat boiler is communicated with the drying chamber.

The waste heat boiler collects high-temperature flue gas heat and is reused in the drying chamber, so that the temperature of the high-temperature flue gas is reduced to 220-300 ℃ under the working condition of a subsequent bag type dust collector, and a set of anti-condensation heating heat exchange device is further arranged at an outlet of the secondary combustion chamber.

The waste gas treatment equipment further comprises a drying ash deposition cylinder for collecting ash raised by the drying assembly and a smelting ash deposition cylinder for raising ash raised by the smelting furnace, wherein the drying ash deposition cylinder is arranged on a pipeline between the drying assembly and the secondary combustion chamber, and the smelting ash deposition cylinder is arranged on a pipeline between the smelting furnace and the multistage surface cooler.

The settled ash has re-smelting value, but the settled ash can be re-smelted in a smelting furnace only by a brick making machine, because ash-shaped particles are in a fluidized state directly under the combustion environment of 1300-1500 ℃, the effective slag rate is low. Therefore, the settled ash is smelted again by brick making machine to increase slag rate, reduce oxygen content in flue gas, reduce fuel consumption and improve comprehensive treatment capacity.

In one embodiment, the pretreatment tower and the absorption tower are both tower bodies made of glass fiber reinforced plastics. The glass fiber reinforced plastic material is used in the flue gas treatment tower containing heavy metal components, so that the electrochemical corrosion problem of the tower body metal material generated when the carbon steel material tower is subjected to production load change (intermittent production) and periodic overhaul can be avoided.

The pretreatment tower is provided with a pretreatment spraying system, the pretreatment spraying system comprises a pretreatment reverse spraying layer and a pretreatment radial spraying layer, the pretreatment reverse spraying layer is arranged below the pretreatment radial spraying layer, a nozzle of the pretreatment reverse spraying layer faces to the bottom of the pretreatment tower, and a nozzle of the pretreatment radial spraying layer is parallel to the section direction of the pretreatment tower.

The pretreatment spraying system is provided with three pretreatment radial spraying layers and one pretreatment reverse spraying layer. It can be understood that the above-mentioned pretreatment radial spraying layer and pretreatment reverse spraying layer can also be flexibly set according to practical requirements, such as a first pretreatment radial spraying layer, a three-layer pretreatment reverse spraying layer, a second pretreatment radial spraying layer, a two-layer pretreatment reverse spraying layer, etc., but at least a first pretreatment radial spraying layer and a first pretreatment reverse spraying layer are required.

The absorption tower is provided with a main tower spraying system, the main tower spraying system comprises a main tower reverse spraying layer and a main tower radial spraying layer, the main tower reverse spraying layer is arranged below the main tower radial spraying layer, a nozzle of the main tower reverse spraying layer faces to the bottom of the absorption tower, and a nozzle of the main tower radial spraying layer is parallel to the section direction of the absorption tower;

the pretreatment spray system and the main tower spray system are communicated with the circulating pool, and recovery pipelines are arranged at the bottoms of the pretreatment tower and the absorption tower and are communicated with the circulating pool.

The main tower spraying system is sequentially provided with a first main tower radial spraying layer, a second main tower radial spraying layer, a third main tower radial spraying layer, a fourth main tower radial spraying layer and a layer of main tower reverse spraying layer from top to bottom.

It can be understood that the radial spraying layer of the main tower and the reverse spraying layer of the main tower can also be flexibly arranged according to practical requirements, such as a radial spraying layer of the first main tower, a reverse spraying layer of the third main tower, a radial spraying layer of the second main tower, a reverse spraying layer of the second main tower and the like, but at least one radial spraying layer of the first main tower and one reverse spraying layer of the first main tower are required.

The absorption tower is also provided with a first turbulent flow liquid film generator and a second turbulent flow liquid film generator, the first turbulent flow liquid film generator is arranged between the main tower reverse spraying layer and the main tower radial spraying layer, and the second turbulent flow liquid film generator is arranged between the second main tower radial spraying layer and the third main tower radial spraying layer.

In one embodiment, the absorption tower is further provided with a demisting system positioned at the top of the absorption tower, the demisting system comprises a demister and a demisting backwashing system, and the demisting backwashing system is provided with a nozzle for spraying water towards the demister and a water supply pipeline;

The demister comprises an upper demister and a lower demister which are sequentially arranged from top to bottom, the demisting backwashing system is provided with nozzles on the upper portion and the lower portion of the lower demister, and the demisting backwashing system is only provided with nozzles below the upper demister.

The wet electrostatic dust collector comprises a wet electric current equalizing device and a wet electric field module which are sequentially arranged along with the flow direction of flue gas, wherein the wet electric field module comprises an anode cylinder and a cathode wire, and the same pole distance in the wet electric field module is 250-400mm; the wet electrostatic precipitator is also provided with a wet electric backwashing system, and a nozzle of the wet electric backwashing system is arranged above the anode cylinder and the cathode line.

The waste gas treatment equipment further comprises an anti-corrosion chimney which is communicated with the flue gas outlet end of the wet electrostatic precipitator and used for discharging and purifying flue gas.

The invention also discloses a closed-loop treatment method for hazardous waste sludge, which adopts the copper-containing industrial sludge three-waste comprehensive treatment system, and comprises the following steps:

the solid waste treatment process comprises the following steps:

and (3) filter pressing: carrying out filter pressing on dangerous waste sludge to be treated in a filter press to remove water so as to obtain a filter cake;

And (3) drying: adding carbon powder and quicklime into the filter cake, uniformly mixing, and drying in a drying assembly;

Brick making: the dried material is used for making bricks in a brick making machine;

smelting: pouring bricks subjected to brick making into a smelting furnace for smelting to obtain a smelting product;

The waste gas treatment process comprises the following steps:

bag type dust removal: the waste gas generated in the drying step is sent to the first bag type dust collector for dust removal, and the waste gas generated in the smelting step is cooled by a multi-stage surface cooler and then sent to the second bag type dust collector for dust removal;

Pretreatment: delivering the flue gas dedusted by the first bag type dust collector and the second bag type dust collector to a pretreatment tower, and treating the flue gas by taking lime slurry as fresh absorption slurry;

Wet desulfurizing: the pretreated flue gas is conveyed to an absorption tower, and lime slurry is used as fresh absorption slurry to treat the flue gas;

And (3) electrostatic dust removal: the flue gas after wet desulfurization is conveyed to a wet electrostatic precipitator, and is purified in an electrostatic precipitation mode and then discharged;

The sewage treatment process comprises the following steps:

primary sedimentation: introducing the wastewater generated in the filter pressing step and other sources of wastewater into the primary sedimentation tank, and carrying out solid-liquid separation treatment on the wastewater by utilizing gravity sedimentation;

Acid regulation: the upper layer sewage after solid-liquid separation in the primary sedimentation tank enters an acid regulating tank, sulfuric acid and ferrous sulfate are added, and an acidic environment and ferrous ions are provided for the subsequent oxidation process;

oxidizing: the sewage after acid adjustment enters an oxidation tank, hydrogen peroxide is added, so that the hydrogen peroxide produces hydroxyl free radicals under the catalysis of ferrous ions, and organic matters in the sewage are oxidized and decomposed into micromolecular matters under the acidic condition;

Alkali regulation: the oxidized sewage enters an alkali regulating tank, sodium hydroxide is added, the pH value of the sewage is regulated to be neutral or alkalescent, and the sewage reacts with a metal-flushing compound in the sewage to generate heavy metal sediment;

And (3) coagulation: the sewage after alkali adjustment enters a coagulation tank, and polyaluminium chloride is added to form a precipitate of colloid in the sewage;

Flocculation: the coagulated sewage enters a flocculation tank, polyacrylamide is added, so that colloid in the sewage is destabilized, and the colloid is mutually collided and coagulated to form a precipitate;

And (3) sludge precipitation: the flocculated sewage enters a sludge sedimentation tank, and solid-liquid separation is carried out on the sewage through gravity sedimentation;

Sand filtering: the sewage after the sludge precipitation enters a sand filter device for filtration;

Carbon filtration: filtering the sewage after the sewage sand filtration in a carbon filter device;

cotton core filtration: the sewage after carbon filtration enters a cotton core filter device for filtration;

reverse osmosis: and (3) filtering the sewage after being filtered by the cotton core by a reverse osmosis membrane to obtain concentrated liquid and recyclable clear liquid which are required to be returned to the primary sedimentation step, and finishing sewage treatment.

In one embodiment, the treatment equipment is adopted, and the settled sludge generated in the primary sedimentation step is extracted to the filter pressing step for treatment;

Extracting settled sludge generated in the sludge settling step to the filter pressing step for treatment;

And conveying clear liquid generated in the reverse osmosis step to the wet desulfurization and electrostatic dust removal step for use, and conveying concentrated liquid generated in the reverse osmosis step to the bag type dust removal step for use by the concentrated liquid spraying system and then refluxing to the primary sedimentation step for treatment.

In one embodiment, with the above treatment apparatus, the exhaust gas treatment process further includes a spray slurry circulation process, and the spray slurry circulation process includes the following steps:

preliminary digestion: reacting the calcium-based absorbent with water in a digestion device to digest;

Secondary digestion: allowing the primarily digested slurry to enter the pulping tank for secondary digestion to obtain fresh absorption slurry;

and (3) recycling: fresh absorption slurry enters a circulating pool for storage, enters the pretreatment tower and the absorption tower for spraying through a pipeline, and the sprayed absorption slurry flows back to the circulating pool.

In the waste gas treatment process, the density of the fresh absorption slurry is 1030-1100kg/m ³, and the time of primary digestion and secondary digestion is 3-5h.

With the above processing apparatus, the spray slurry circulation process includes the steps of:

Slurry treatment: and (3) extracting fresh absorption slurry in the circulating tank, entering an oxidation tank, oxidizing outside the tank in the oxidation tank, oxidizing calcium sulfite into calcium sulfate insoluble substances through aeration of an oxidation fan, blowing SO ₂ with the aeration air quantity of 1moL into the surface state dry air with the volume of 0.2-0.8 m ³/h, introducing the slurry after the aeration reaction into a sedimentation tank for sedimentation for solid-liquid separation, and extracting the obtained solid sludge to the filter pressing step for treatment.

And conveying clear liquid generated in the reverse osmosis step to the primary digestion and recycling step for water supplementing.

In one embodiment, the above treatment device is adopted, in the solid waste treatment process, the filter cake is placed in the material collecting box, and the material is fed and thrown to the drying component, the brick making machine and the smelting furnace sequentially through an automatic feeding system.

In one embodiment, the above processing device is adopted, in the drying step, a temperature and moisture probe is adopted to detect the temperature and moisture content of the drying chamber, a group of data samples are carried out every 10-20 minutes, and the detection probe feeds back to a PLC control system through an electric signal to monitor the drying degree in the drying chamber; after drying for 2-3 hours, carrying out raking treatment by utilizing a steel rake structure of a manipulator through a raking mechanical arm, so that the dried materials are heated more uniformly, and meanwhile, adding a filter cake through a second mechanical arm; and carrying out raking and feeding once in 20-30 minutes, feeding until the drying chamber reaches the maximum accommodating capacity, and stopping feeding when the dry material level reaches the set height of the infrared sensor.

In one embodiment, in the sewage treatment process, in the step of adjusting the acid, the pH value of the sewage is adjusted to 3-4;

in the alkali adjustment step, the pH value of the sewage is adjusted to 7.5-8;

in the reverse osmosis step, the reverse osmosis membrane has a rejection pore size of 0.0001 microns.

In one embodiment, the treatment device is adopted, discharging is started when the pressure of the discharging back pressure valve reaches 1mPa, and the discharging is started when the pressure of the protecting back pressure valve reaches a preset value, so that the protecting loop is communicated.

In one embodiment, the above treatment device is adopted, and the exhaust gas treatment process further includes a secondary combustion step, wherein the exhaust gas generated in the drying step is sent to the secondary combustion chamber, natural gas and/or diesel oil are sprayed in the secondary combustion chamber, combustion is carried out at 1000-1100 ℃ by an oxidation fan to burn out CO, carbon powder and dioxin in the exhaust gas, the oxygen content of the exhaust gas is reduced, and then the exhaust gas is sent to the first bag-type dust collector for dust removal.

In one embodiment, the treatment device is adopted, in the pretreatment step, fresh absorption slurry is sprayed at a flow rate of 50-60L/min and a pressure of 1-2 bar, and the sum of spraying coverage areas of the nozzles is 200-300% of the radial cross-sectional area of the pretreatment tower.

In one embodiment, with the above treatment apparatus, in the wet desulfurization step, the radial spray layer sprays fresh absorption slurry at a flow rate of 150 to 250L/min and a pressure of 1 to 2bar, the reverse spray layer sprays fresh absorption slurry at a flow rate of 100 to 150L/min and a pressure of 1 to 2bar, and the spray flow rate of the radial spray layer is smaller than the spray flow rate of the reverse spray layer; and the sum of the spray coverage areas of the spray nozzles is 200-300% of the radial cross-sectional area of the absorption tower.

Compared with the prior art, the invention has the following beneficial effects:

The comprehensive treatment system of the three wastes of the copper-containing industrial sludge aims at the discharge of the three wastes of sludge, sewage, waste gas and the like with high heavy metal content, and the solid waste treatment equipment, the waste gas treatment equipment and the sewage treatment equipment are matched, so that the process of comprehensively treating the solid, liquid and gas three phases of the heavy metal-containing hazardous waste sludge can be effectively realized, and the purposes of reducing, harmlessly and recycling the hazardous waste sludge three wastes are achieved. And exhaust gas treatment is carried out through the pretreatment tower and the cooperative absorption tower (WLT tower), so that the desulfurization rate and the dust removal rate are improved, meanwhile, the severe smoke property is adjusted through the pretreatment tower, part of smoke dust and sulfur dioxide are removed in advance, the smoke temperature is reduced, the internal equipment of the subsequent WLT tower is protected, and the service life of the subsequent equipment is prolonged.

The treatment equipment has remarkable benefits for the comprehensive treatment of copper-containing sludge and hazardous waste solid, liquid and gas of surface treatment waste generated in the industries of metal surface treatment, heat treatment processing, glass manufacturing, electronic element manufacturing and the like.

The invention relates to a closed-loop treatment method for hazardous waste sludge, which is used for removing harmful components such as dioxin, heavy metals, smoke dust, sulfur dioxide and the like in smoke gas which is treated by subsequent waste gas and has heavy metal components due to special components such as copper, nickel and the like in the process of treating hazardous waste sludge, is a special smoke gas component which is not shaped by a specific treatment process in industry, and innovatively removes the harmful components such as dioxin, heavy metals, smoke dust, sulfur dioxide and the like by a whole set of desulfurization and dust removal comprehensive waste gas treatment process and meets the emission standards.

The invention also creates a set of mature industrial sewage treatment flow aiming at the sewage containing heavy metal components, so that the sewage generated by the hazardous waste sludge and the waste gas treatment is subjected to innocent treatment and is circularly used for the procedures of water supplementing, cooling and spraying back flushing of an auxiliary system for waste gas treatment, thereby achieving the purpose of zero discharge of the sewage, being circularly used for equipment cleaning and site flushing in daily production and reducing the water burden of factories.

Drawings

FIG. 1 is a schematic diagram of a connection relationship of processing devices in an embodiment;

FIG. 2 is a schematic process flow diagram of a treatment method according to an embodiment;

FIG. 3 is a schematic diagram showing the structures of a pretreatment column and an absorption column in the embodiment;

FIG. 4 is a schematic view of a reverse spray layer structure in an embodiment;

FIG. 5 is a schematic view of a radial spray layer structure in an embodiment;

FIG. 6 is a schematic diagram of a turbulent liquid film generator in an embodiment;

FIG. 7 is a schematic diagram of a demister according to an embodiment;

FIG. 8 is a schematic diagram of part I of the method of FIG. 7;

FIG. 9 is a schematic diagram of connection relation of an automatic feeding system in an embodiment;

Wherein: 1100. a filter press; 1200. a drying assembly; 1210. a drying chamber; 1300. brick making machine 1400. Smelting furnace; 1410. a concentrated solution spraying system; 1510. a material collecting box; 1521. a first mechanical arm; 1522. a second mechanical arm; 1523. a third mechanical arm; 1524. a fourth mechanical arm; 1525. a fifth mechanical arm; 1526. a sixth mechanical arm; 1527. a raking mechanical arm; 1531. a first conveyor belt; 1532. a second conveyor belt; 1533. a third conveyor belt;

A secondary combustion chamber; 2110. a waste heat boiler; 2200. a multi-stage surface cooler; 2310. a first bag collector; 2311. heating heat exchange equipment; 2320. a second bag collector; 2400. a pretreatment tower; 2410. preprocessing a reverse spraying layer; 2420. pretreating a radial spraying layer; 2500. an absorption tower; 2510. the main tower reversely sprays the layer; 2521. a first main tower radial spray layer; 2522. a second main tower radial spraying layer; 2523. a third main tower radial spray layer; 2524. a fourth main tower radial spray layer; 2531. a first turbulent liquid film generator; 2532. a second turbulent liquid film generator; 2541. a demister; 2542. a defogging backwashing system; 2600. wet electrostatic dust collector; 2700. an anti-corrosion chimney; 2810. a calcium-based absorbent bin; 2820. a digestion device; 2830. a pulping pool; 2840. a circulation tank; 2850. a sedimentation tank; 2860. an oxidation tank; 2870. an oxidation blower; 2910. drying the ash deposition cylinder; 2920. smelting an ash precipitation cylinder;

A gas-water separator; 3210. a primary sedimentation tank; 3220. an acid regulating tank; 3230. an oxidation pond; 3240. an alkali regulating pool; 3250. a coagulation pool; 3260. a flocculation tank; 3270. a sludge sedimentation tank; 3310. sand filtering device; 3320. a carbon filter device; 3330. a cotton core filter; 3340. a reverse osmosis device; 3341. a recycling pool; 3342. a concentrate pool; 3400. an automatic feeding system; 3410. a reagent storage tank; 3420. a metering pump; 3430. a discharge back pressure valve; 3440. a pulsation damper; 3450. a pressure gauge; 3460. protecting the back pressure valve.

Detailed Description

In order that the invention may be readily understood, a more complete description of the invention will be rendered by reference to the appended drawings. Preferred embodiments of the present invention are shown in the drawings. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.

It will be understood that when an element is referred to as being "connected" to another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "in communication with" another element, it can be directly in communication with the other element or intervening elements may also be present.

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The term "and/or" as used herein includes any and all combinations of one or more of the associated listed items.

Examples

The invention discloses a comprehensive treatment method of three wastes of copper-containing industrial sludge, which adopts treatment equipment disclosed by the invention, and is shown in figure 1, and comprises three modules, namely solid waste treatment equipment, waste gas treatment equipment and sewage treatment equipment; the treatment method is shown in figure 2 and comprises three major processes of solid waste treatment process, waste gas treatment process and sewage treatment process; the detailed description is as follows.

1. And (5) solid waste treatment.

The solid waste treatment equipment comprises a filter press 1100, a drying assembly 1200, a brick making machine 1300 and a smelting furnace 1400, wherein the filter press, the drying assembly, the brick making machine and the smelting furnace are sequentially arranged according to the process flow.

The solid waste treatment device of the present embodiment further includes an automatic feeding system, where the automatic feeding system includes a movable aggregate box 1510, a first mechanical arm 1521, a second mechanical arm 1522, a third mechanical arm 1523, a fourth mechanical arm 1524, a fifth mechanical arm 1525, a sixth mechanical arm 1526, a first conveyor belt 1531, a second conveyor belt 1532, and a third conveyor belt 1533; the outlet end of the filter cake of the filter press corresponds to the initial position of the material collecting box; one end of the first conveyor belt corresponds to the initial position of the collection box, the other end of the first conveyor belt corresponds to the drying assembly, the first mechanical arm is arranged between the initial position of the collection box and the first conveyor belt and used for grabbing the collection box on the first conveyor belt, and the second mechanical arm is arranged between the first conveyor belt and the drying assembly and used for grabbing the collection box on the drying assembly; one end of the second conveyor belt corresponds to the drying assembly, the other end of the second conveyor belt corresponds to the brick making machine, the third mechanical arm is arranged between the drying assembly and the second conveyor belt and used for grabbing the material collecting box on the second conveyor belt, and the fourth mechanical arm is arranged between the second conveyor belt and the brick making machine and used for grabbing and pouring the material in the material collecting box in the brick making machine; one end of the third conveyor belt corresponds to the brick making machine, the other end of the third conveyor belt corresponds to the smelting furnace, the fifth mechanical arm is arranged between the brick making machine and the third conveyor belt and used for grabbing materials after brick making on the third conveyor belt through the material collecting box, and the sixth mechanical arm is arranged between the third conveyor belt and the smelting furnace and used for grabbing and dumping the materials in the material collecting box in the smelting furnace.

1. And (5) press filtration.

In the hazardous waste sludge aimed at by the embodiment, the moisture and ash content are high, the moisture is generally between 70% and 80%, the copper content is 2% to 15%, and the nickel content is 0.1% to 1.1%.

The main components in the hazardous waste sludge of this example are shown in the following table.

TABLE 1 major component (dry basis) of sludge containing high copper and nickel

TABLE 2 solid surface treatment wastes Main chemical composition (Dry basis)

The sludge containing high copper and nickel is derived from industries such as glass manufacturing, common nonferrous metal smelting, electronic element manufacturing and the like, and mainly comprises waste bath liquid, bath slag and wastewater treatment sludge generated by copper plating by a metal plating method by using copper sulfate, dust collection slag, filter pressing slag and wastewater treatment sludge generated by copper pyrometallurgy flue gas purification, waste copper etching liquid generated in the production process of a circuit board, waste liquid and wastewater treatment sludge generated by copper oxidation treatment by using acid, waste etching liquid and wastewater treatment sludge generated in the etching process of a copper plate and the like.

The solid surface treatment waste is derived from the metal surface treatment and heat treatment processing industry and mainly comprises waste residues and wastewater treatment sludge generated by sensitization treatment by stannous chloride, zinc chloride and ammonium chloride; waste bath solution, bath slag and waste water treatment sludge generated in electroplating processes such as zinc plating, cadmium plating, nickel plating, gold plating, copper plating, black chromium plating and the like, waste corrosion solution, waste washing solution, waste bath solution, bath slag and waste water treatment sludge generated in chemical polishing processes of acid (alkali) washing, degreasing, rust removing, washing, phosphating, light emitting and chemical polishing of metal and plastic surfaces, waste bath solution, bath slag and waste water treatment sludge generated in plating stripping processes, waste bath solution, bath slag and waste water treatment sludge generated in corrosion resistance coating, chemical hardening of corrosion resistance layers, roughening of plastic surfaces and the like are performed by using chromium compounds. The two are mainly reflected in the source difference of the raw materials and the proportion difference of specific metal components, but the proportion difference of the metal components of the two is changed due to the fact that the raw materials are not fixed.

The dangerous waste sludge is manually conveyed to the side of a filter press from a storage area through a forklift, the sludge is first subjected to filter pressing through a high-pressure filter press, the average water content of the sludge is 70% and is then subjected to filter pressing to a filter cake with the water content of 50%, the water content of the filter cake after filter pressing is generally 50%, the filter cake belongs to alkaline substances, the pH value is between 6.70 and 9.77, the color is brownish black, brown, brownish black, greenish black and the like, the metal content of copper and the like in the filter cake is about 1% -9%, and the filter cake mainly exists in the form of Cu (OH) ₂、Ni(OH)₂.

The filter-pressing process generates filter-pressing water of 2000t/a (about 9.6 t/d), and the filter-pressing water is sent to sewage treatment equipment for treatment through a sewage discharge pipeline and then is used for the operations of auxiliary water supplementing, back flushing, equipment cleaning and the like of fresh absorption slurry in the waste gas treatment equipment.

2. And (5) drying.

The filter cake containing 11% -14% of copper and 0.3% -0.6% of nickel obtained by the filter pressing process is loaded by a 0.8X0.5X0.5m ³ aggregate box, is conveyed to a drying chamber 1210 of a drying assembly to be dried at a speed of 0.5m/s through a first mechanical arm (six-axis mechanical arm) and a first conveyor belt, and is uniformly mixed with filter cake, carbon powder and quicklime according to a ratio of about 10:1:1, wherein the granularity of the carbon powder is required to be 0.5-1 mm, the granularity of the quicklime is required to be 1-2 mm, and the aim of mixing a higher quicklime proportion is to digest and release heat to improve the temperature and the condensation speed of the materials, have better wet solubility to enable the dry materials to be more stable and higher in quality, and the calcium desulfurization and smelting procedures of waste gas treatment are facilitated to provide calcium ion supplement. The drying room is divided into an upper layer and a lower layer, wood dust serving as fuel is paved on the bottom layer, a sludge filter cake is paved on the upper layer after uniform mixing, and after the wood dust on the bottom layer is ignited, a bin door of the drying room is closed for a drying procedure.

The drying assembly comprises a drying chamber, a raking mechanical arm 1527, a temperature and humidity probe, an infrared sensor and a PLC control system; the drying chamber is divided into a bottom layer for containing fuel and an upper layer for containing drying materials; the temperature and humidity probes are arranged on the upper layer at intervals in the vertical direction, and the temperature and humidity probes are also arranged on a chamber door, an air supply opening and an exhaust port of the drying chamber; the PLC control system is electrically connected with the raking mechanical arm and controls the raking mechanical arm; the temperature and humidity probe is electrically connected with the PLC control system and transmits signals to the PLC control system; the infrared sensor is arranged at a preset height of the drying chamber and transmits a signal to the PLC control system.

In the drying step, firstly, blowing is carried out at the bottom of a drying chamber through a drum oxidation fan; the temperature of the drying room is kept at 500-600 ℃, a temperature and moisture content of the drying room is detected by adopting a temperature and moisture probe, the distribution points of the temperature and moisture probe are 8 corners, a room door, an air supply opening, an air exhaust opening and a dry material layer in the drying room, and a group of data samples are taken every 1-1.5 m and every 15 minutes. The detection probe feeds back to the PLC control system through the electric signal, and the stoving degree in the stoving room is monitored. After drying for 2-3 hours, raking the materials by utilizing a steel rake structure of a manipulator through a raking mechanical arm, so that the dried materials are heated more uniformly, and meanwhile, 2-3 boxes of filter cakes are added through a second mechanical arm. And carrying out raking and feeding for about 20-30 minutes, feeding until the maximum accommodating amount of the drying chamber reaches 15t, and stopping feeding when the dry material level reaches the set height of the infrared sensor.

The drying process lasts for two days, the filter cake is dried and dehydrated in one day, and the dry materials are placed and cooled in one day. The feeding and discharging of the drying chamber and the material transportation are carried out by means of a second mechanical arm, a third mechanical arm (six-axis mechanical arm) and a second conveyor belt, and the automatic operation enables the drying process to be more coherent and rapid. And the oxidation blower is closed in the process of raking and charging, so that the increase of the oxygen content of the flue gas is reduced.

The main purpose of the drying procedure is as follows: the water content of the material is reduced, so that the material is sintered into uniform compact bodies.

In the drying process, part of calcium oxide consumes sulfur dioxide in the flue gas to generate calcium sulfate so that the subsequent smelting process is smoothly carried out, and the reaction equation is as follows:

CaO+SO ₂ (under high temperature conditions) →2CaSO ₃+O₂→2CaSO₄

The drying procedure obtains the dry material with 23 to 26 percent of copper, 0.8 to 1.1 percent of nickel and 10 percent of water content.

3. And (5) brick making.

The dry materials are placed in a material collecting box and conveyed to a brick making machine for material feeding through a third mechanical arm, a fourth mechanical arm and a second conveyor belt, and the brick making machine presses the dry materials into small bricks with the dimensions of 250 multiplied by 110 multiplied by 50mm ³ by high pressure.

In the brick making process, a proper amount of slag former is added, wherein the main components of the slag former are 5% silicate, 25% SiO ₂ and 70% CaO, and the slag former is used for slag formation in the subsequent smelting process, and the addition amount is that the weight ratio of SiO ₂ to CaO in the smelting raw materials is 1:3.

4. Smelting.

After the brick making process is finished, the collection box filled with small bricks is clamped to a third conveyor belt through a fifth mechanical arm (six-axis mechanical arm), the collection box is conveyed to the side of a smelting furnace at the speed of 0.5m/s, and then bricks in the collection box are poured into the smelting furnace through the sixth mechanical arm (six-axis mechanical arm) to carry out the smelting process.

The smelting process adopts a pyrometallurgy process with simple flow and few intermediate links.

The method comprises the following steps: the brick is reduced at high temperature in a furnace, coke is added into the furnace as fuel and reducing agent, and a certain amount of slag former is supplemented at the same time, so that the ratio of SiO ₂ to CaO is 1:3.

The furnace temperature in the smelting process is about 1300 ℃. The bricks run from top to bottom, the bottom tuyere is a melting zone, and the bricks reach the tuyere zone to be melted. Air is blown in through the air port, coke is combusted in the air port area, generated high-temperature reducing smoke gas runs from bottom to top and reversely runs with the brick to perform heat exchange, so that the brick is gradually heated to complete various reduction smelting processes. Along with the continuous melting of the brick, the slag and the molten copper are discharged, the charge level is continuously lowered, and the charge is continuously supplemented, so that the top charge of the furnace is kept at a constant level.

The solid waste treatment equipment is also provided with a concentrated solution spraying system, the concentrated solution spraying system is arranged on cooling and spraying slag of the smelting furnace, and the primary sedimentation tank is communicated with the primary sedimentation tank through the concentrated solution spraying system. And cooling and spraying the smelted slag by the concentrated solution spraying system, and enabling the recovered concentrated solution to enter a primary sedimentation tank for treatment.

The smelting process principle is as follows:

Under the action of high temperature, caSO ₄ in the material is decomposed to generate sulfur dioxide, cu (OH) ₂、Ni(OH)₂ and the like in the material are generated to be oxidized, the sulfur dioxide is preferentially reacted with the metal oxide to produce sulfide (copper matte), and when the sulfur dioxide is insufficient, the metal oxide is directly reduced into metal by carbon.

A. Generation of SO ₂ in the material:

2CaSO ₄ +C (under high temperature condition) →2CaO+2SO ₂+CO₂

B. The metal hydroxide in the material is decomposed into metal oxide

M (OH) ₂ (under high temperature conditions) →MO+H ₂ O (gas)

C. The SO ₂, if present, preferentially reacts with the metal oxide to form sulfide (blister copper)

4CuO+2SO ₂+4C→2Cu₂ S (blister copper) +4CO ₂

6NiO+4SO₂+7C→2Ni₃S₂+7CO₂

D. in the absence of SO ₂, the metal oxide is directly reacted with carbon to form a metal element

2CuO+C→2Cu+CO₂

2NiO+C→2Ni+CO₂

E. as in the above c and d, other metal oxides are reduced by the following reaction with solid carbon

PbO+C→Pb+CO

2PbO+C→2Pb+CO₂

When the iron oxide in the material is reduced to metallic iron in the presence of high concentration of CO, but when the oxide or sulfide of lead in the material is present, the oxide or sulfide is replaced by iron, the reaction is:

PbO+Fe→Pb+FeO

PbS+Fe→Pb+FeS

2Cu+FeS→Cu₂S+Fe

FeO, silicon and calcium slag, which has lighter specific gravity, float above the metal hearth and are discharged at fixed time to obtain the slag glassy solid solution.

CaO+SiO ₂ (under high temperature conditions) →CaSiO ₃ (slag) +CO ₂

The added slag former reacts, molten calcium silicate (CaSiO ₃) becomes slag with light specific gravity, floats on the molten copper, can reduce the contact of the molten copper with the atmosphere, improves the quality of finished products, and simultaneously part of harmful substances such as sulfur, phosphorus, gas, impurities and the like can enter the slag to be taken away when the slag is removed.

FeS and Cu ₂S、Ni₃S₂ are combined into a mixture of blister copper and matte, the blister copper and the matte have larger specific gravity, are deposited below a hearth, are discharged at fixed time, and are layered after being cooled, so that the blister copper and the matte are obtained.

And smelting to obtain coarse copper with copper content of 90%, nickel content of 2.5%, copper matte with copper content of 45%, and nickel content of 7.5%, pouring and cooling to obtain the final product, and transporting the final product into a finished product collecting box through a belt conveyor to a storage room for storage.

2. And (5) waste gas treatment.

The exhaust gas treatment device comprises a multi-stage surface air cooler 2200, a first bag-type dust remover 2310 and a second bag-type dust remover 2320, and comprises a pretreatment tower 2400, an absorption tower 2500, a wet electrostatic precipitator 2600 and an anti-corrosion chimney 2700 which are sequentially communicated through pipelines, wherein the first bag-type dust remover and the second bag-type dust remover are both communicated with the pretreatment tower, an exhaust pipeline of the drying assembly is connected with the first bag-type dust remover, and an exhaust pipeline of the smelting furnace is communicated with the second bag-type dust remover through the multi-stage surface air cooler.

The main technical indexes of the raw exhaust gas in this embodiment are shown in the following table.

TABLE 3 Main technical index of original flue gas

Index (I)	Unit (B)	Parameters (parameters)	Parameters (parameters)
				Number of production lines	——	Smelting furnace	Drying furnace
Flow rate of flue gas	Nm³/h	13000	24000
				Exhaust gas temperature	℃	110	170
Flow rate of flue gas	Am³/h	17762	38945
				Measured oxygen content	——	≤13.0％	≤13.0％
Original SO ₂ concentration conversion value	mg/Nm³	3000～25000	≤4000
				Raw smoke concentration calculation value	mg/Nm³	＜200	＜200
Nickel and its compounds	mg/Nm³	＜50	＜50
				Copper and its compound	mg/Nm³	＜200	＜600

1. And (5) bag type dust removal.

In the solid waste treatment process of the embodiment, a gas collecting hood is arranged at a feed inlet, a discharge outlet (or a copper outlet) and a slag discharging outlet of the drying assembly and the smelting furnace, and the gas collecting hood is communicated with the first bag type dust collector and the second bag type dust collector through exhaust pipelines after collecting escaping flue gas.

And in the exhaust gas treatment equipment, the device also comprises a drying ash deposition cylinder for collecting the ash raised by the drying assembly and a smelting ash deposition cylinder for raising the ash of the smelting furnace, wherein the drying ash deposition cylinder is arranged on a pipeline between the drying assembly and the secondary combustion chamber, and the smelting ash deposition cylinder is arranged on a pipeline between the smelting furnace and the multistage surface cooler. And collecting the settled fly ash to a brick making process for brick making and then smelting again.

The waste gas treatment equipment further comprises a secondary combustion chamber 2100, a waste heat boiler and a heating heat exchange device, wherein the secondary combustion chamber is arranged between the exhaust pipeline of the drying assembly and the first bag type dust collector, and the secondary combustion chamber is further provided with a fuel spraying system for spraying fuel and a blast system for supporting combustion. The waste gas treatment equipment further comprises a waste heat boiler and heating heat exchange equipment, wherein the waste heat boiler and the heating heat exchange equipment are sequentially communicated between the secondary combustion chamber and the first bag type dust collector, and a flue gas pipeline of the waste heat boiler is communicated with the drying chamber.

In the drying process, the smoke temperature of the outlet flue is about 170-200 ℃, and the temperature of the drying process is 500-600 ℃, so that the low-temperature combustion of oxyhydrogen compounds can be combined with chloride to generate dioxin severe poison, a secondary combustion chamber is arranged in the outlet flue of the drying chamber, the volume of the secondary combustion chamber is about 0.18m ³, the secondary combustion chamber is used for carrying out blowing combustion by spraying natural gas and diesel oil and a blowing oxidation fan, the secondary combustion is carried out, the residence time is 2-3 seconds, the daily oil consumption is about 12kg, the combustion temperature is about 1000-1100 ℃, unburned components such as carbon powder and the like in the smoke are removed, and the extremely toxic gas dioxin is burned.

The multistage surface cooler is used for cooling the flue gas through heat exchange of external cold air.

The high-temperature flue gas at 800-900 ℃ of the outlet flue of the smelting process enters the pipeline of the multi-stage surface cooler, and the temperature of the flue gas is reduced to 100-120 ℃ through heat exchange in the multi-stage surface cooler.

The two-combustion-chamber outlet flue and the multi-stage surface air cooler outlet flue are respectively connected into the first bag type dust collector and the second bag type dust collector for flue gas dust removal treatment, the bag type dust collectors are provided with 500-700 filter bags and flower plates for isolating raw flue gas and clean flue gas, the dust concentration in the flue gas and the content of particulate matters such as heavy metal solid compounds can be reduced by 98% through dust filtration formed by the filter bags and the smoke dust, most of heavy metal solid compounds are captured by the bag type dust collectors, and the heavy metal entering the water circulation of the desulfurizing tower is negligible and cannot cause secondary pollution of the water circulation.

The dust and heavy metal solid compounds filtered by the filter bag are collected into a dust hopper of the dust remover through a soot blowing system, and bricks are smelted again after the solid compounds are treated or collected by qualified government departments.

2. And (5) pretreatment.

And then, the flue gas of the first bag type dust collector and the flue gas of the second bag type dust collector are converged through a flue and then are connected into a pretreatment tower.

The pretreatment tower is provided with a pretreatment spray system, as shown in fig. 3, the pretreatment spray system comprises a pretreatment reverse spray layer 2410 and a pretreatment radial spray layer 2420, the pretreatment reverse spray layer is arranged below the pretreatment radial spray layer, a nozzle of the pretreatment reverse spray layer faces the bottom of the pretreatment tower, and a nozzle of the pretreatment radial spray layer is parallel to the section direction of the pretreatment tower. Specifically, the pretreatment spraying system is provided with three pretreatment radial spraying layers and one pretreatment reverse spraying layer.

The smoke temperature at the inlet of the pretreatment tower is 100-130 ℃, the tower body is made of glass fiber reinforced plastic materials with corrosion resistance and high temperature resistance, a four-layer spray structure, one-layer reverse spray and three-layer radial spray are provided, the spray liquid is lime slurry, fresh absorption slurry is sprayed at the flow rate of 50-60L/min and the pressure of 1-2 bar, the spray head is a 316 spiral spray nozzle, and the spray coverage area of the spray head slurry (namely the sum of spray coverage areas of the spray nozzles is the radial cross section area of the absorption tower) can reach 200-300%.

The pretreatment tower is used for adjusting the smoke property of a subsequent absorption tower (a WLT three-phase turbulent flow cylinder high-efficiency desulfurization and dust removal tower), removing part of smoke dust by lime slurry mist, reducing the concentration of about 40 percent of sulfur dioxide in the smoke, reducing the temperature of the smoke from 100-120 ℃ to 50-65 ℃, preventing malignant smoke from accelerating the loss of the WLT three-phase turbulent flow cylinder high-efficiency desulfurization and dust removal tower, and carrying out dust removal and dust removal in cooperation with the WLT tower.

3. Wet desulfurizing.

The flue gas is then pretreated in a pretreatment tower and enters an absorption tower, wherein the temperature of the flue gas is about 50-65 ℃.

The glass steel is enclosed to the tower body material of absorption tower, is equipped with main tower spraying system, as shown in fig. 3, main tower spraying system includes the reverse spray layer of main tower and the radial spray layer of main tower, the reverse spray layer of main tower set up in the radial spray layer below of main tower, the nozzle on the reverse spray layer of main tower is towards the absorption tower bottom, the nozzle on the radial spray layer of main tower is on a parallel with the cross-section direction of absorption tower.

The main tower spraying system is sequentially provided with a main tower reverse spraying layer 2510, a first main tower radial spraying layer 2521, a second main tower radial spraying layer 2522, a third main tower radial spraying layer 2523 and a fourth main tower radial spraying layer 2524 from bottom to top.

In the five-layer spraying structure, one layer of reverse spraying (a main tower reverse spraying layer) is shown in fig. 4, four layers of radial spraying (a first main tower radial spraying layer to a fourth main tower radial spraying layer) are shown in fig. 5, fresh absorption slurry is sprayed by the radial spraying layer at the flow rate of 150-250L/min and the pressure of 1-2 bar, fresh absorption slurry is sprayed by the reverse spraying layer at the flow rate of 100-150L/min and the pressure of 1-2 bar, the spray head is a 316 spiral spray nozzle, and the atomization spraying coverage area (namely the sum of spray coverage areas of the spray nozzles is the radial cross section area of the absorption tower) can reach 200% -300%.

The absorption tower is also provided with a first turbulent flow liquid film generator 2531 and a second turbulent flow liquid film generator 2532, the first turbulent flow liquid film generator is arranged between the main tower reverse spraying layer and the main tower radial spraying layer, and the second turbulent flow liquid film generator is arranged between the second main tower radial spraying layer and the third main tower radial spraying layer.

The two layers of turbulent flow liquid film generators (rotating wheel type liquid film generating devices) are utilized to partition treated smoke, and specifically, the rotating vane type structure of the turbulent flow liquid film generator can change the flow direction of the smoke, equalize the flow of the smoke, fully mix and react with spraying liquid, the number of blades of the generating device is 10-15, the inclination is 20-40 degrees, and the blades are fixedly arranged by a core column with an elliptical head as shown in figure 6.

The absorption tower is also provided with a demisting system positioned at the top of the absorption tower, the demisting system comprises a demister 2541 and a demisting backwashing system 2542, in the embodiment, the demister is composed of a plurality of high-temperature-resistant and flame-retardant polyphenylene sulfide plates, and as shown in fig. 7-8, the demisting backwashing system is provided with a nozzle and a water supply pipeline which spray water towards the demister.

In this embodiment, the demister is a double-layer folded plate demister, and is installed at the top of the absorption tower, so as to separate mist droplets entrained by clean flue gas and part of ultrafine dust. However, it can be understood that the demister can also select tube bundles, ridge type and the like according to different working conditions, and the outlet with the diameter larger than 15 μm carries mist drops which are less than or equal to 50mg/Nm ³ (dry basis). And the demister material adopts the reinforced flame-retardant polyphenylene sulfide plate, and can bear high-speed water flow scouring, in particular high-speed water flow scouring caused by manual flushing. The demister flushing water system can comprehensively flush the demister, and the demister is prevented from being blocked. The spray ranges of adjacent nozzles should overlap partially to ensure a 100% flush effect. The pressure of the flushing water should be monitored and controlled, and the main pipe of the flushing water should be arranged so that each nozzle basically runs at the average water pressure, and the demister back flushing system supplements water by the clean water in the reuse water tank.

And the upper demister and the lower demister arranged in the system can remove sediment of the demister, and the demister can be automatically flushed or manually flushed according to a given or changeable program during operation.

The pretreatment tower and the absorption tower are matched, and a calcium desulfurization process is used, so that the desulfurization rate can reach more than 98%. The spray mass transfer mode in the tower adopts the organic combination of radial spraying, reverse spraying and a liquid film generator, on one hand, radial atomization spraying mainly captures fine dust during desulfurization, and the dust removal capacity of the desulfurization tower is enhanced; on the other hand, two spraying processes are simultaneously used in the same tower body, and compared with a single spraying process, the slurry circulation quantity is obviously reduced. The atomization spraying, the liquid film generating device and the demister are matched to carry out secondary dust removal, so that fine particulate matters and aerosol components in the flue gas are removed, and the dust removal rate is about 30% -50%.

In both pretreatment and wet desulfurization, the most important fresh absorption slurry is lime slurry, which is provided by the following spray slurry circulation system.

The spray slurry circulation system comprises a calcium-based absorbent bin 2810, a digestion device 2820, a pulping tank 2830 and a circulation tank 2840 which are sequentially communicated through pipelines, wherein the circulation tank provides fresh absorption slurry to the pretreatment tower and the absorption tower through a supply pipeline, and is communicated with the bottoms of the pretreatment tower and the absorption tower through a recovery pipeline to recover the absorption slurry.

The spraying slurry circulating system further comprises a sedimentation tank 2850, an oxidation tank 2860 and an oxidation fan 2870, wherein the oxidation tank is communicated with the circulating tank and the sedimentation tank through pipelines, the oxidation fan is provided with an aeration pipe, and the aeration pipe extends into the oxidation tank; and a pipeline is arranged at the bottom of the sedimentation tank and is communicated with the filter press.

In the spray slurry circulation system, slurry raw material calcium-based absorbent is stored in a vertical calcium-based absorbent storage bin of about 70m ³, the calcium-based absorbent storage bin is opened and closed through a gate valve, a star-shaped discharge valve controls blanking, the calcium-based absorbent in the calcium-based absorbent storage bin enters a digestion device to digest, the digestion device supplements water through clear liquid in a reuse water tank, calcium hydroxide slurry generated by the reaction of the calcium-based absorbent and water enters a pulping device to carry out secondary digestion, tempering, cooling and pulping residence time of about 4 hours. Stirring devices are arranged in the digestion and pulping devices, so that the digestion rate is increased, the temperature is reduced, the slurry is refined, and the rotating speed of the stirring shafts is about 40r/min. Fresh absorbent slurry having a density of about 1030-1100 kg/m ³ was obtained.

And then lime slurry (namely fresh absorption slurry) in the pulping device enters a circulating tank through a water pump, the circulating tank is used as an intermediate carrier for storing, updating and recycling the fresh absorption slurry, water supplementing is carried out through clear liquid in the recycling tank and reflux liquid of the wet electrostatic precipitator, spray liquid supplementing is carried out through a pretreatment tower, a reflux pipe of the absorption tower and a pipeline of the pulping tank, and spray liquid updating is carried out through quantitative extraction of slurry in the tank by an oxidation device outside the tank.

The detailed process is as follows: slurry in the circulating pool is pumped to each spraying layer of the pretreatment tower and the absorption tower by a slurry pump for spraying, and the available old spraying liquid containing calcium bisulfide and unreacted calcium hydroxide after the spraying reaction returns to the circulating pool for recycling through a return pipe of the pretreatment tower and the absorption tower, and back flushing water in the wet electrostatic precipitator returns to the circulating pool for water supplementing through the return pipe. And the slurry in the circulating pool quantitatively enters the oxidation device for updating through the slurry pump, so that the quality of the slurry is prevented from being influenced. Stirring devices are arranged in the circulating tanks, and the purpose is to refine slurry, prevent deposition blockage and enable the rotating speed of a stirring shaft to be about 30r/min.

The slurry entering the oxidation device is oxidized outside the oxidation tank through a Roots oxidation fan and an aerator pipe, the air quantity of the oxidation fan is 30m ³/h, calcium bisulfide is oxidized into calcium sulfate insoluble substances through air blowing, and the slurry mainly containing calcium sulfate enters a sedimentation tank for solid-liquid separation.

The sedimentation tank prevents the sediment and blockage of the bottom calcium sulfate slurry by a stirring device, and the rotating speed of a stirring shaft is about 10r/min. The slurry in the sedimentation tank is pumped to a special calcium-based recovery filter pressing device for treatment by a slurry pump.

The main chemical reaction formula of the calcium-gypsum wet desulfurization process is as follows:

SO₂+H₂O→H₂SO₃

Ca(OH)₂+H₂SO₃→CaSO₃+2H₂O

CaSO₃·1/2H₂O+SO₂+1/2H₂O→Ca(HSO₃)₂

Ca(HSO₃)₂+Ca(OH)₂→2Ca SO₃·1/2H₂O+H₂O

CaSO ₃·1/2H₂O+1/2O₂+3/2H₂O→CaSO₄·2H₂ O (by-product)

At the moment, the temperature of the flue gas is about 40-50 ℃, the humidity of the flue gas is about 90-95%, and the concentration of smoke dust is less than or equal to 20g/m ³.

4. And (5) electrostatic dust collection.

The flue gas after wet desulfurization enters a wet electrostatic precipitator through a flue to carry out final dust removal.

The wet electrostatic dust collector comprises a wet electric current equalizing device and a wet electric field module which are sequentially arranged along with the flow direction of flue gas, wherein the wet electric field module comprises an anode cylinder and a cathode wire, and the same pole distance in the wet electric field module is 250-400mm; the wet electrostatic precipitator is also provided with a wet electric backwashing system, and nozzles of the wet electric backwashing system are arranged above the anode cylinder and the cathode wire and can flush the anode cylinder and the cathode wire.

The flue gas is subjected to flow equalization through a wet electric flow equalization device, enters a wet electric field module, high-voltage electricity discharges through a cathode wire to charge smoke dust in the flue gas, the homopolar distance is preferably 250-400 mm, the charged smoke dust moves to an anode cylinder in a directional mode under the action of coulomb force, the anode cylinder is used as a dust collecting pole to collect the smoke dust, a back flushing system is arranged above the anode cylinder to spray the smoke dust, the inner wall of the anode cylinder is fixed to form a water film, heavy metal-containing smoke dust and aerosol-state pollutants attracted to the anode cylinder are flushed, the dust removal rate is about 60%, the back flushing system supplements water through clear liquid in a reuse pool, and wet electric back flushing spray liquid enters a circulating pool through a back flushing pipe to be used as supplementing water to be utilized without discharging.

After the above treatment, main technical indexes of the flue gas in this embodiment are shown in the following table.

TABLE 4 main technical index of treated flue gas

Project name	Parameters (parameters)	Remarks
			Exhaust gas temperature	℃	≈50
Measured oxygen content	——	≤13.0％
			Conversion value of SO ₂ concentration after purification	㎎/Nm³	≤80
Smoke concentration conversion value after purification	㎎/Nm³	≤50
			Nickel and its compounds	㎎/Nm³	≤1
Copper and its compound	㎎/Nm³	≤4

The waste gas treatment equipment further comprises an anti-corrosion chimney which is communicated with the flue gas outlet end of the wet electrostatic precipitator and used for discharging and purifying flue gas. Finally, the purified flue gas which is processed by the whole set of equipment and is stable and up to the standard is discharged into the atmosphere through an anti-corrosion chimney.

3. And (5) sewage treatment.

In the embodiment, the wastewater generated in the solid waste treatment process and the waste gas treatment process is not discharged, and is subjected to innocent treatment through the wastewater treatment process after being collected, and is circularly used for the water supplementing, cooling and spraying back flushing processes of the waste gas treatment auxiliary system, so that the purpose of zero discharge of the wastewater is achieved, and the wastewater is circularly used for equipment cleaning and site flushing in daily production, and the water burden of a factory is reduced.

The sewage treatment equipment comprises a gas-water separator 3100, a concentrated solution tank 3342 and a clear solution tank 3341, and comprises a primary sedimentation tank 3210, an acid regulating tank 3220, an oxidation tank 3230, an alkali regulating tank 3240, a coagulation tank 3250, a flocculation tank 3260, a sludge sedimentation tank 3270, a sand filtering device 3310, a carbon filtering device 3320, a cotton core filter 3330 and a reverse osmosis device 3340 which are sequentially communicated through pipelines, wherein a reverse osmosis membrane is arranged in the reverse osmosis device to divide the reverse osmosis device into a concentrated solution cavity and a clear solution cavity, the concentrated solution cavity is communicated with the concentrated solution tank, and the clear solution cavity is communicated with the clear solution tank; the primary sedimentation tank is communicated with a sewage discharge pipeline of the filter press, and the concentrated liquid tank is communicated with the primary sedimentation tank through the concentrated liquid spraying system.

In this embodiment, the sewage treatment apparatus further includes an automatic feeding system 3400 for automatic feeding, as shown in fig. 9, where the automatic feeding system includes a reagent tank 3410, a metering pump 3420, and a discharge back pressure valve 3430, where the reagent tank is sequentially connected to the metering pump and the discharge back pressure valve through a pipeline.

The automatic feeding system further comprises a pulsation damper 3440, a protection loop and a flow correction loop, wherein the pulsation damper is arranged on a pipeline between the reagent storage tank and the metering pump, the protection loop is communicated with the metering pump and the reagent storage tank, and a pressure gauge 3450 and a protection back pressure valve 3460 are arranged on the protection loop; one end of the flow correction loop is communicated with the reagent storage tank, and the other end of the flow correction loop is communicated with a pipeline between the metering pump and the reagent storage tank.

The acid regulating tank, the oxidation tank, the alkali regulating tank, the coagulation tank and the flocculation tank are all provided with the automatic feeding system. And stirring systems for stirring the liquid in the tanks are arranged in the primary sedimentation tank, the acid regulating tank, the oxidation tank, the alkali regulating tank, the coagulation tank, the flocculation tank and the sludge sedimentation tank.

The main pollutants in the wastewater are heavy metals such as 85-95 mg/L COD (the amount of the reducing organic matters to be oxidized) and copper with the concentration of 1-2 mg/L suspended matters. And most of the smoke dust containing heavy metals in the waste gas can be captured by a bag type dust collector with the dust removal rate reaching 98%, and the heavy metals entering the subsequent water circulation can be ignored.

In this example, the main components in the industrial wastewater are shown in the following table.

TABLE 5 main components of industrial wastewater

Note that: ND indicates no detection.

1. And (5) primary sedimentation.

The filter-pressing water of the filter press enters a primary sedimentation tank after passing through a gas-water separator 3100, the sewage is subjected to solid-liquid separation treatment primarily by utilizing gravity sedimentation, the bottom layer insoluble particulate slurry can be pumped to the filter press to be dehydrated and then used as solid waste raw materials, the purpose of removing insoluble particulate matters in the sewage is achieved, the primary sedimentation tank is provided with a stirring system to prevent sediment from caking and blocking, and the rotating speed of a stirring shaft is about 10r/min.

It will be appreciated that other industrial waste water and other sources of sewage may also be treated in the sewage treatment apparatus of this embodiment by entering the primary sedimentation tank through the drainage lines of the apparatus, the plant.

2. Regulating acid.

The upper sewage of the primary sedimentation tank overflows or passes through a water pump, enters an acid regulating tank, and is added with proper amounts of sulfuric acid and ferrous sulfate through an automatic feeding system, so that the pH value of the sewage is reduced from 10-12 to 3-4, an acidic environment and ferrous ions are provided for the subsequent preparation of Fenton reagent, the acid regulating tank is provided with a stirring system to uniformly mix the reagent and the sewage, the reaction time is shortened, the rotating speed of a stirring shaft is about 15r/min, and the stirring shaft and a stirring paddle are made of glass fiber reinforced plastics with strong corrosion resistance.

The automatic feeding system mainly comprises a reagent storage tank, a metering pump for controlling the addition amount of the reagent, a pulsation damper for protecting the metering pump from reducing fluid impact, a discharge back pressure valve for opening discharge when the pressure of the discharge back pressure valve reaches 1mPa, pressure in a pipeline is ensured, a protection back pressure valve for opening liquid return when the pressure of the pipeline is overlarge to form a protection loop, and a flowmeter for correcting flow.

3. And (5) oxidizing.

The sewage in the acid regulating tank overflows or passes through a water pump and enters the oxidation tank. The oxidation pond is added with a proper amount of hydrogen peroxide strong oxidant through an automatic feeding system to generate hydroxyl free radicals with high reactivity so as to oxidize and degrade organic pollutants. H ₂O₂ generates hydroxyl radicals (. OH) under the catalytic action of Fe ²⁺, also known as Fenton's reagent.

Because the hydroxyl radical (OH) has strong oxidizing property and electrophilic addition property, most of organic matters in the wastewater can be oxidized and decomposed into micromolecular matters in an acidic environment with the pH value of 3-4, so that the aim of reducing organic pollutant COD in oxidized water and organic matter components forming microorganisms is fulfilled.

Too high a pH will inhibit the formation of hydroxyl radicals (. OH) and precipitation of ferric hydroxide, too low a pH, ferric iron will not be reduced to ferrous iron, resulting in a hindered catalytic reaction, suitably a pH of 3-4.

And the oxidation tank is provided with a stirring system to uniformly mix the reagent and the sewage, so that the reaction time is shortened, and the rotating speed of a stirring shaft is about 15r/min.

The reaction formula of the Fenton reagent for generating hydroxyl free radicals is as follows:

Fe²⁺+H⁺+H₂O₂＝Fe³⁺+H₂O+(·OH)

4. And (5) regulating alkali.

The sewage in the oxidation pond overflows or passes through a water pump and enters the alkali regulating pond. The alkali regulating tank is added with a proper amount of sodium hydroxide solution through an automatic feeding system, so that the pH value of sewage is increased from 3-4 to 7.5-8, and the corrosion and damage of the follow-up equipment caused by the strong acid environment are prevented.

And simultaneously, hydroxide radicals react with heavy metal compounds such as copper sulfate and the like to generate heavy metal precipitates such as copper hydroxide and the like. The alkali regulating tank is provided with a stirring system to uniformly mix the reagent and the sewage, so that the reaction time is shortened, the blocking of sediment is prevented, and the rotating speed of a stirring shaft is about 15r/min.

The reaction formula of the hydroxide and the copper sulfate is as follows:

2NaOH+CuSO₄＝Cu(OH)₂↓+NaSO₄

5. And (5) coagulation.

The sewage in the alkali-adjusting tank overflows or passes through a water pump and enters the coagulation tank. The coagulation tank is added with a proper amount of polyaluminium chloride (PAC for short) through an automatic feeding system. The colloid in the sewage or the sludge can be quickly formed into precipitate by the aid of the colloid or the hydrolysate of the colloid, so that the precipitate of heavy metals and other particles in the sewage can be conveniently separated, and the pH range suitable for the reaction is 7.5-8. The coagulation tank is provided with a stirring system to uniformly mix the reagent and the sewage, so that the reaction time is shortened, the blocking of sediment is prevented, and the rotating speed of a stirring shaft is about 15r/min.

6. And (5) flocculation.

Sewage in the coagulation tank overflows or passes through a water pump and enters the flocculation tank. And a proper amount of polyacrylamide (PAM for short) is added into the flocculation tank through an automatic feeding system. After the coagulant is added into raw water, the coagulant is fully mixed with water, most of colloid impurities in the water lose stability, destabilized colloid particles collide with each other in a flocculation tank and are coagulated, and finally flocs which can be removed by a precipitation method are formed, and the pH range suitable for the reaction is 7.5-8. The flocculation tank is provided with a stirring system to uniformly mix the reagent and the sewage, so that the reaction time is shortened, the blocking of sediment is prevented, and the rotating speed of a stirring shaft is about 15r/min.

7. And (5) sludge precipitation.

Sewage in the flocculation tank overflows or passes through a water pump and enters a sedimentation sludge tank. And (3) carrying out water-liquid separation on heavy metal and other sediments in the sewage through gravity sedimentation. The sludge deposited at the bottom is pumped to a filter press by a slurry pump to carry out filter pressing concentration, a filter cake obtained by filter pressing enters a drying procedure in solid waste treatment, and filtrate enters a primary sedimentation tank of a wastewater treatment center again and is not discharged. The sedimentation sludge tank is provided with a stirring system to prevent sediment from caking and blocking, and the rotating speed of a stirring shaft is about 5r/min.

8. And (5) sand filtering.

The sewage on the upper layer of the sedimentation sludge pool overflows or passes through a water pump and enters a sand filtering device for filtering treatment.

9. And (5) carbon filtration.

And (5) filtering the sewage after the sewage sand filtration in a carbon filter device.

10. And (5) filtering by a cotton core.

The sewage after carbon filtration enters a cotton core filter device for filtration treatment, the cotton core filter is physically filtered, a stainless steel shell is adopted, and PP cotton is used as a filter core to filter large particles so as to protect a subsequent reverse osmosis device.

The deep filtration is carried out through sand filtration, carbon filtration and cotton core filtration to remove fine particles with turbidity of more than 1 degree, so that suspended particles which cannot be completely removed or are newly generated in pretreatment are prevented from entering a reverse osmosis system, and a high-pressure pump and a reverse osmosis membrane are protected.

11. Reverse osmosis.

The sewage after being filtered by the cotton core enters a reverse osmosis device and is filtered by a reverse osmosis membrane.

The filtrate after deep filtration enters an RO water treatment system through a high pressure pump, the filtrate passes through a reverse osmosis membrane under the action of high pressure, the solvent permeates from high concentration to low concentration, and the reverse osmosis membrane can intercept substances larger than 0.0001 micron, so that the purpose of separating, purifying and concentrating the filtrate is achieved.

The reverse osmosis water treatment system can remove organic matters, soluble salts to 98 percent and colloid in the filtrate. Through reverse osmosis membrane treatment, the concentration of clear liquid suspended substances is about 4mg/L, COD, the concentration of clear liquid suspended substances is about 15mg/L, pH, the concentration of suspended substances is reduced to 7-8 mg/L, the concentration of hexavalent chromium is reduced to 0.004mg/L, the concentration of heavy chromium is reduced to 0.004mg/L, the concentration of copper is reduced to 0.001mg/L, the concentration of zinc is reduced to 0.07mg/L, the concentration of mercury is reduced to 0.02mg/L, the concentration of arsenic is reduced to 0.1mg/L, and all heavy metal contents can reach the standard and be discharged.

The clear liquid enters a reuse water tank to be discharged after reaching standards, and is used for equipment cleaning and waste gas treatment, such as a demister back flushing system of an absorption tower, a back flushing system of an anode cylinder and a cathode line of a wet electrostatic precipitator, a digestion device of a spraying slurry circulating system and a circulating tank. And the concentrated solution trapped by the reverse osmosis membrane is pumped to a concentrated solution pool through a water pump and is used for cooling and spraying by a multi-stage surface cooler and then returns to the sedimentation tank for treatment without being discharged.

4. And (5) calculating material balance.

The input and output of various materials and elements for the closed loop treatment method of hazardous waste sludge of this example were calculated and the results are shown in the following table.

TABLE 6 input-output balance table for materials

TABLE 7 sulfur balance table

TABLE 8 copper element balance table

TABLE 9 Nickel element balance table

The material balance results show that the equipment and the treatment process of the embodiment can realize the comprehensive treatment of three wastes of industrial sludge.

The technical features of the above-described embodiments may be arbitrarily combined, and all possible combinations of the technical features in the above-described embodiments are not described for brevity of description, however, as long as there is no contradiction between the combinations of the technical features, they should be considered as the scope of the description.

The above examples illustrate only a few embodiments of the invention, which are described in detail and are not to be construed as limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the invention, which are all within the scope of the invention. Accordingly, the scope of protection of the present invention is to be determined by the appended claims.

Claims

1. A copper-containing industrial sludge three-waste comprehensive treatment system is characterized by comprising:

The sewage treatment equipment comprises a concentrate pool, a reuse pool, a primary sedimentation pool, an acid regulating pool, an oxidation pool, an alkali regulating pool, a coagulation pool, a flocculation pool, a sludge sedimentation pool, a sand filtering device, a carbon filtering device, a cotton core filter and a reverse osmosis device which are sequentially communicated through pipelines, wherein the reverse osmosis device is provided with a reverse osmosis membrane to divide the reverse osmosis device into a concentrate cavity and a clear liquid cavity, the concentrate cavity is communicated with the concentrate pool, and the clear liquid cavity is communicated with the reuse pool; the primary sedimentation tank is communicated with a sewage discharge pipeline of the filter press, and the concentrated liquid tank is communicated with the primary sedimentation tank;

the bottoms of the sludge sedimentation tank and the primary sedimentation tank are respectively provided with a sludge return pipeline communicated with the filter press;

the reuse water tank is communicated with the absorption tower and the wet electrostatic precipitator through pipelines;

The waste gas treatment equipment further comprises a spraying slurry circulation system, wherein the spraying slurry circulation system comprises a calcium-based absorbent storage bin, a digestion device, a pulping pool and a circulation pool which are sequentially communicated through pipelines, the circulation pool provides fresh absorption slurry to the pretreatment tower and the absorption tower through a supply pipeline, and the fresh absorption slurry is communicated with the bottoms of the pretreatment tower and the absorption tower through a recovery pipeline to recover the absorption slurry;

the spraying slurry circulating system further comprises a sedimentation tank, an oxidation tank, calcium-based recovery filter pressing equipment and an oxidation fan, wherein the oxidation tank is communicated with the circulating tank and the sedimentation tank through pipelines, the oxidation fan is provided with an aeration pipe, and the aeration pipe extends into the oxidation tank; the bottom of the sedimentation tank is provided with a pipeline communicated with the calcium-based recovery filter pressing equipment;

The recycling water tank is respectively communicated with the digestion device and the circulating tank through pipelines;

The solid waste treatment equipment is also provided with a concentrated solution spraying system, the concentrated solution spraying system is arranged for cooling and spraying slag of the smelting furnace, and the concentrated solution tank is communicated with the primary sedimentation tank through the concentrated solution spraying system;

The waste gas treatment equipment further comprises a drying ash deposition cylinder for collecting ash raised by the drying assembly and a smelting ash deposition cylinder for raising ash raised by the smelting furnace, and further comprises a secondary combustion chamber, wherein the drying ash deposition cylinder is arranged on a pipeline between the drying assembly and the secondary combustion chamber, and the smelting ash deposition cylinder is arranged on a pipeline between the smelting furnace and the multistage surface cooler;

The pretreatment tower is provided with a pretreatment spray system, the absorption tower is provided with a main tower spray system, the pretreatment spray system and the main tower spray system are communicated with the circulating pool, and the bottoms of the pretreatment tower and the absorption tower are provided with recovery pipelines which are communicated with the circulating pool.

2. The copper-containing industrial sludge three-waste comprehensive treatment system according to claim 1, wherein the solid waste treatment device further comprises an automatic feeding system, and the automatic feeding system comprises a movable collection box, a first mechanical arm, a second mechanical arm, a third mechanical arm, a fourth mechanical arm, a fifth mechanical arm, a sixth mechanical arm, a first conveyor belt, a second conveyor belt and a third conveyor belt; the outlet end of the filter cake of the filter press corresponds to the initial position of the material collecting box; one end of the first conveyor belt corresponds to the initial position of the collection box, the other end of the first conveyor belt corresponds to the drying assembly, the first mechanical arm is arranged between the initial position of the collection box and the first conveyor belt and used for grabbing the collection box on the first conveyor belt, and the second mechanical arm is arranged between the first conveyor belt and the drying assembly and used for grabbing the collection box on the drying assembly; one end of the second conveyor belt corresponds to the drying assembly, the other end of the second conveyor belt corresponds to the brick making machine, the third mechanical arm is arranged between the drying assembly and the second conveyor belt and used for grabbing the material collecting box on the second conveyor belt, and the fourth mechanical arm is arranged between the second conveyor belt and the brick making machine and used for grabbing and pouring the material in the material collecting box in the brick making machine; one end of the third conveyor belt corresponds to the brick making machine, the other end of the third conveyor belt corresponds to the smelting furnace, the fifth mechanical arm is arranged between the brick making machine and the third conveyor belt and used for grabbing the brick-making materials on the third conveyor belt through a material collecting box, and the sixth mechanical arm is arranged between the third conveyor belt and the smelting furnace and used for grabbing and pouring the materials in the material collecting box into the smelting furnace;

3. The comprehensive treatment system for three wastes of copper-containing industrial sludge according to claim 1, wherein the sewage treatment equipment further comprises an automatic feeding system for automatic feeding, the automatic feeding system comprises a reagent storage tank, a metering pump and a discharge back pressure valve, and the reagent storage tank is sequentially communicated with the metering pump and the discharge back pressure valve through pipelines;

The automatic feeding system further comprises a pulsation damper, a protection loop and a flow correction loop, wherein the pulsation damper is arranged on a pipeline between the reagent storage tank and the metering pump, the protection loop is communicated with the metering pump and the reagent storage tank, and a pressure gauge and a protection back pressure valve are arranged on the protection loop; one end of the flow correction loop is communicated with the reagent storage tank, and the other end of the flow correction loop is communicated with a pipeline between the metering pump and the reagent storage tank;

the acid regulating tank, the oxidation tank, the alkali regulating tank, the coagulation tank and the flocculation tank are all provided with the automatic feeding system;

4. The comprehensive treatment system for copper-containing industrial sludge three wastes according to claim 2, wherein the secondary combustion chamber is arranged between the exhaust pipeline of the drying assembly and the first bag type dust collector in the waste gas treatment equipment, and is further provided with a fuel spraying system for spraying fuel and a blast system for supporting combustion;

5. The comprehensive treatment system for three wastes of copper-containing industrial sludge according to claim 1, wherein the pretreatment tower and the absorption tower are both tower bodies made of glass fiber reinforced plastics;

The pretreatment spraying system comprises a pretreatment reverse spraying layer and a pretreatment radial spraying layer, wherein the pretreatment reverse spraying layer is arranged below the pretreatment radial spraying layer, a nozzle of the pretreatment reverse spraying layer faces to the bottom of the pretreatment tower, and the nozzle of the pretreatment radial spraying layer is parallel to the section direction of the pretreatment tower;

the pretreatment spraying system is provided with three pretreatment radial spraying layers and one pretreatment reverse spraying layer;

the main tower spraying system comprises a main tower reverse spraying layer and a main tower radial spraying layer, wherein the main tower reverse spraying layer is arranged below the main tower radial spraying layer, a nozzle of the main tower reverse spraying layer faces to the bottom of the absorption tower, and the nozzle of the main tower radial spraying layer is parallel to the section direction of the absorption tower;

the main tower spraying system is sequentially provided with a first main tower radial spraying layer, a second main tower radial spraying layer, a third main tower radial spraying layer, a fourth main tower radial spraying layer and a layer of main tower reverse spraying layer from top to bottom;

The absorption tower is also provided with a first turbulent flow liquid film generator and a second turbulent flow liquid film generator, the first turbulent flow liquid film generator is arranged between the main tower reverse spray layer and the main tower radial spray layer, and the second turbulent flow liquid film generator is arranged between the second main tower radial spray layer and the third main tower radial spray layer;

The absorption tower is also provided with a demisting system positioned at the top of the absorption tower, the demisting system comprises a demister and a demisting backwashing system, and the demisting backwashing system is provided with a nozzle and a water supply pipeline which are oriented to water spraying of the demister.

6. The comprehensive treatment system for three wastes of copper-containing industrial sludge according to claim 5, wherein the demister comprises an upper demister and a lower demister which are sequentially arranged from top to bottom, the demisting and backwashing system is provided with nozzles above and below the lower demister, and the demisting and backwashing system is provided with nozzles only below the upper demister;

The wet electrostatic dust collector comprises a wet electric current equalizing device and a wet electric field module which are sequentially arranged along with the flow direction of flue gas, wherein the wet electric field module comprises an anode cylinder and a cathode wire, and the same pole distance in the wet electric field module is 250-400mm; the wet electrostatic precipitator is also provided with a wet electric backwashing system, and a nozzle of the wet electric backwashing system is arranged above the anode cylinder and the cathode wire;

7. A closed loop treatment method for hazardous waste sludge, which is characterized in that the copper-containing industrial sludge three-waste comprehensive treatment system as claimed in any one of claims 1 to 6 is adopted, and the method comprises the following steps:

the solid waste treatment process comprises the following steps:

The waste gas treatment process comprises the following steps:

The sewage treatment process comprises the following steps:

8. The closed loop treatment method for hazardous waste sludge according to claim 7, wherein the treatment equipment according to claim 2 is adopted, and the settled sludge produced in the primary settling step is extracted to the press filtration step for treatment;

The clear liquid generated in the reverse osmosis step is conveyed to the wet desulfurization and electrostatic dust removal step for use, and the concentrated liquid generated in the reverse osmosis step is conveyed to a concentrated liquid spraying system for use and then flows back to the primary sedimentation step for treatment;

the waste gas treatment process further comprises a spraying slurry circulation process, and the spraying slurry circulation process comprises the following steps of:

and (3) recycling: fresh absorption slurry enters a circulating pool for storage, enters the pretreatment tower and the absorption tower for spraying through a pipeline, and the sprayed absorption slurry flows back to the circulating pool;

in the waste gas treatment flow, the density of the fresh absorption slurry is 1030-1100kg/m < 3 >, and the time of primary digestion and secondary digestion is 3-5h;

the spraying slurry circulation process comprises the following steps:

Slurry treatment: extracting fresh absorption slurry in the circulating tank, entering an oxidation tank, oxidizing outside the tank in the oxidation tank, oxidizing calcium sulfite into calcium sulfate insoluble substances through aeration of an oxidation fan, introducing the slurry after the aeration reaction into a sedimentation tank for sedimentation for solid-liquid separation, and extracting the obtained solid sludge to the filter pressing step for treatment, wherein the aeration air quantity of the oxidation fan is 25-35m < 3 >/h;

9. The closed-loop treatment method for hazardous waste sludge according to claim 7, wherein the treatment equipment according to claim 2 is adopted, the filter cake is placed in the material collecting box in the solid waste treatment process, and the drying component, the brick making machine and the smelting furnace are sequentially fed and thrown through an automatic feeding system;

In the drying step, a temperature and moisture probe is adopted to detect the temperature and moisture content of a drying chamber, a group of data sampling is carried out every 10-20 minutes, the detection probe feeds back to a PLC control system through an electric signal, and the drying degree in the drying chamber is monitored; after drying for 2-3 hours, carrying out raking treatment by utilizing a steel rake structure of a manipulator through a raking mechanical arm, so that the dried materials are heated more uniformly, and meanwhile, adding a filter cake through a second mechanical arm; and carrying out raking and feeding once in 20-30 minutes, feeding until the drying chamber reaches the maximum accommodating capacity, and stopping feeding when the dry material level reaches the set height of the infrared sensor.