CN110734209A - Operation method of industrial solid waste and sludge rotary kiln co-processing integrated device - Google Patents

Operation method of industrial solid waste and sludge rotary kiln co-processing integrated device Download PDF

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Publication number
CN110734209A
CN110734209A CN201911006919.0A CN201911006919A CN110734209A CN 110734209 A CN110734209 A CN 110734209A CN 201911006919 A CN201911006919 A CN 201911006919A CN 110734209 A CN110734209 A CN 110734209A
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sludge
flue gas
air
temperature
bag
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Inventor
俞其林
王凯军
张鸿涛
江力
俞林明
贾少华
裘华刚
俞聪儒
潘英杰
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ZHEJIANG HUANXING MACHINERY CO Ltd
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ZHEJIANG HUANXING MACHINERY CO Ltd
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00Treatment of sludge; Devices therefor
    • C02F11/12Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/13Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D50/00Combinations of methods or devices for separating particles from gases or vapours
    • B01D50/10Combinations of devices covered by groups B01D45/00, B01D46/00 and B01D47/00
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/48Sulfur compounds
    • B01D53/52Hydrogen sulfide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/54Nitrogen compounds
    • B01D53/56Nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/60Simultaneously removing sulfur oxides and nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/68Halogens or halogen compounds
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/76Gas phase processes, e.g. by using aerosols
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77Liquid phase processes
    • B01D53/78Liquid phase processes with gas-liquid contact
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/001Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
    • B01D2257/20Halogens or halogen compounds
    • B01D2257/206Organic halogen compounds
    • B01D2257/2064Chlorine
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
    • B01D2257/60Heavy metals or heavy metal compounds
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00Specific waste
    • F23G2209/12Sludge, slurries or mixtures of liquids

Abstract

The invention relates to kinds of cooperative treatment integrated devices, in particular to an operation method of kinds of industrial solid waste and sludge rotary kiln cooperative treatment integrated devices, which is a sludge spray drying (direct drying) + disc drying (indirect drying), rotary kiln and industrial leftover material (solid waste) cooperative incineration and flue gas purification system integrated device, and collects sludge drying and dry sludge, industrial leftover material (solid waste) cooperative incineration and flue gas purification in bodies, thereby achieving the purposes of recycling waste and reducing environmental pollution.

Description

Operation method of industrial solid waste and sludge rotary kiln co-processing integrated device
Technical Field
The invention relates to kinds of cooperative treatment integrated devices, in particular to an operation method of kinds of industrial solid waste and sludge rotary kiln cooperative treatment integrated devices.
Background
According to the prediction, the total sludge yield reaches 3000 million tons at the end of 2012, and the sludge yield reaches 6000 million tons until 2020, toxic and harmful substances such as organic substances, heavy metals, pathogenic microorganisms and the like contained in the sewage in the sludge of the sewage plant are contained, and the sludge has greater biological toxicity, in addition, in the aspect of , ten pieces of water released in 4 months in 2015 enters steps to promote sludge treatment, namely, the sludge generated by the sewage treatment facility is subjected to stabilization, harmless and resource treatment, the sludge which does not reach the standard is forbidden to enter cultivated land, illegal sludge stacking points are banned, the existing sludge treatment facility is basically transformed before the end of 2017, the ground-level and above municipal sludge treatment rate reaches more than 90% before the end of 2020, the reduction of landfill sites, the improvement of environmental awareness, the environmental standards are increasingly reduced, the environmental standards are strictly met, and the like, and the harmless treatment is the global harmless treatment.
At present, the moisture content of sludge after dehydration in most domestic sewage treatment plants is about 80%, the sludge is large in volume and extremely inconvenient to transport, and the final treatment (including landfill, incineration, building material utilization, land utilization and the like) of the sludge is extremely difficult, in addition aspects, the domestic garbage landfill pollution control standard (GB16889-2008) stipulates that the sludge of the municipal sewage plant can enter a landfill only when the moisture content is reduced to below 50% after the treatment, so that the deep dehydration treatment of times of dehydrated sludge is performed, and the reduction, stabilization and resource utilization of the sludge are urgently realized.
At present, the sludge deep dehydration technology applied to mainly comprises high-pressure plate-and-frame box type filter pressing and the like, the mechanical sludge deep dehydration technology can reduce the water content of sludge to 50%, but the economical efficiency is considered and the mechanical dehydration of sludge is difficult to reduce the water content of sludge by steps due to the existing condition restriction, in the occasion of reducing the water content requirement of sludge, a heat drying method is usually adopted to obtain lower water content of sludge, the high-pressure plate-and-frame box type filter pressing technology can reduce the water content of sludge to below 50%, so that the water content of municipal sludge and industrial sludge treated in sewage plants is 50% -80%.
In order to fundamentally and fully utilize the advantage of high heat value of industrial solid waste in some areas at present, a mode of incinerating the sludge and the industrial solid waste in a rotary kiln is selected, so that the principles of 'reduction, reutilization and resource' of the process circular economy are reflected to the maximum extent while the sludge and the industrial solid waste are recycled.
Disclosure of Invention
The invention mainly solves the defects in the prior art, and provides operation methods of industrial solid wastes and sludge rotary kiln cooperative treatment integrated devices which have compact structures, use wastes to prepare wastes and further reduce the environmental pollution of wastes by recycling leftover materials and .
The technical problem of the invention is mainly solved by the following technical scheme:
the industrial solid wastes mainly refer to leftover materials and the like of textile clothes, the components of the leftover materials and the like are single and are stable, the average water content is low, and inflammable substances (particularly inflammable substances with high heat value) are more, and the heat value is 6000-20000 kJ/kg., and the leftover materials and the like can be cooperatively treated with dried sludge only through simple pretreatment processes such as crushing, compacting and forming.
The sludge spray drying (direct drying) + disc drying (indirect drying) + rotary kiln and industrial leftover material (solid waste) collaborative incineration and flue gas purification system integrated device collects sludge drying and dry sludge, industrial leftover material (solid waste) collaborative incineration and flue gas purification in body, well solves the problem of recycling comprehensive utilization of sludge and industrial solid waste, achieves the purpose of treating sludge and industrial solid waste with double wastes, saves a large amount of energy, saves the treatment cost by 40% compared with natural gas auxiliary fuel, and has very good investment value.
The invention relates to an integrated device of sludge spray drying (direct drying), disc drying (indirect drying), rotary kiln and industrial leftover material (solid waste) collaborative incineration and flue gas purification systems, which collects sludge drying and dry sludge, industrial leftover material (solid waste) collaborative incineration and flue gas purification in body, compared with other treatment modes, the integrated device has the outstanding advantages that high-temperature heat treatment technologies are adopted, namely determined excess air and treated organic waste are subjected to oxidative decomposition reaction in an incinerator, toxic and harmful substances in the waste are oxidized and pyrolyzed at high temperature to be destroyed, the integrated device fully utilizes the self-heat value of dried sludge, dries the sludge to the moisture content of below 30%, the average low heat value of the sludge can reach above 1600kJ/kg, and the industrial solid waste mainly refers to textile clothing leftover material, has relatively single component stability, relatively low average moisture content and more combustible substances (especially high-heat value combustible substances), and can be used as energy for incineration by simple pretreatment, such as compaction and molding, and the like, wherein sludge is 6000-20000 kJ/kg..
The waste heat of the sludge incineration system and the heat demand of the drying system can be balanced in a most economic and environment-friendly way by selecting a combined mode of sludge drying, rotary kiln and industrial leftover material (solid waste) in cooperation with incineration and incineration. If the drying system has large heat demand and the waste heat provided by the incineration system is insufficient to dry the dewatered sludge to the self-sustaining combustion degree, an auxiliary heat source needs to be added, but the auxiliary heat source is relatively directly combusted, and the increase of the auxiliary (heat source) industrial leftover materials is greatly reduced. During operation, the heat source and the air inlet temperature can be adjusted at any time according to the temperature in the incinerator, energy consumption is saved to the maximum extent, and the adaptability of the incinerator to various heat value sludge is improved, which is a technical route formulated aiming at the project. The industrial solid wastes mainly comprise leftover materials of textiles and clothes and have the characteristics of low water content and high heat value, but the sizes are not uniform, so that the appearance of the waste entering the incinerator is reduced, the solid wastes must be crushed in advance, and the crushed wastes have uniform sizes and uniform textures due to the elimination of large gaps; the method is suitable for special incineration furnaces for industrial leftover materials (solid wastes), and the utilization rate of the method is improved in the incineration process. Therefore, the crusher is selected for pretreatment by combining the characteristics of the project. The drying tower is designed to have the sludge temperature of 50-60 ℃ and the sludge water content of about 20%. The exhaust temperature of tail gas is designed to be 90-110 DEG C
The process has the characteristics of realizing the reduction (the maximum can reach 92 percent) of the sludge, harmlessness, stabilization and reclamation. The main purpose of incineration is to incinerate the waste as much as possible and to turn the incinerated substances harmless and to minimize the volume reduction and to minimize the generation of new pollutants to avoid secondary pollution. In recent years, due to the adoption of a proper pretreatment process and an appropriate incineration means, the self-sufficiency of sludge heat energy is achieved, the increasingly strict environmental requirements can be met, and a treatment method taking incineration as a core is considered to be the most thorough, rapid and economical method for sludge treatment.
Through a spray drying system and a disc drying system, after drying treatment, the waste water enters a return rotary kiln to be treated with industrial solid waste incineration.
The process consists of the following processing systems:
1. sludge receiving system:
2. sludge spray drying (direct drying), disc drying (indirect drying) system,
3. Sludge incineration system:
4. flue gas processing system:
5. the wind power slag suction system comprises:
6. incineration residue ash collection system:
the process is briefly described as follows: the vehicle-mounted sludge enters a field, the water content of the vehicle-mounted sludge is 70% -80% and is poured into an underground receiving system, the vehicle-mounted sludge is lifted by a shaftless auger, a screw pump is conveyed into a large sludge storage tank through a filter, the sludge is conveyed into a high-level sludge tank through a plunger pump, and finally the sludge is conveyed into a spray drying tower after being lifted by the screw pump, atomized by a tower top nozzle and then is in downstream contact with high-temperature flue gas discharged from a secondary combustion chamber for drying. In the drying process, the temperature of inlet high-temperature flue gas is 500-550 ℃, the temperature of exhaust gas is about 110 ℃, the moisture content of dried sludge is reduced from 80% to 20%, and the temperature of sludge discharged from a drying tower is 50-60 ℃; then directly enters a rotary kiln incinerator for incineration. Because of adopting different sewage dehydration modes; and conveying part of wet sludge with the water content of 50-70% of the incoming sludge to a wet sludge pit through a vehicle, grabbing the wet sludge to a buffer hopper by a crane grab bucket, conveying the wet sludge below the buffer hopper into a disc dryer in a spiral adjustable manner, and indirectly heating the sludge by using saturated steam (the pressure is 0.5MPa. G saturated steam) output by a waste heat boiler as a heating medium. The heated steam condensate is pumped back to the boiler deoxygenation water tank through a condensate collection system for reuse.
And (3) discharging waste gas generated in the sludge drying process through a tail gas draught fan, and maintaining the micro-negative pressure operation of the dryer, auxiliary equipment and system pipelines. The extracted waste gas is subjected to two-stage treatment of dust removal and condensation, the waste gas condensate is brought into a sewage collection and treatment station, and the non-condensable gas is pumped to the rotary kiln by a tail gas fan.
The method comprises the steps of feeding dry sludge dried by a disc into a rotary kiln for incineration through a sludge conveying device, feeding the dry sludge into a barrel from the head of the barrel and slowly moving towards the tail along with the rotation of the barrel, feeding combustion-supporting air required for incineration, wherein part of the combustion-supporting air is extracted from a sludge bin deodorization system, part of the combustion-supporting air is ambient air and is blown into a combustion chamber through a blower for heating, the hot blast stove adopts a traditional direct combustion type (biomass and coal) hot blast stove, is optimized and modified, is suitable for feeding industrial solid waste materials such as textile leftover materials, and the like, feeding the leftover materials into a horizontal chain grate after entering a hopper through a feeding machine, so as to realize the processes of drying, pyrolysis, combustion and exhaustion and the like, feeding the leftover materials with a conventional direct combustion type (biomass and coal) hot blast stove into a sludge rotary kiln incineration system after high-temperature flue gas generated by combustion of burning, feeding the leftover materials into a kiln from the kiln, and a kiln head of the rotary kiln, feeding the rotary kiln, and a flue gas drying, discharging the flue gas, discharging the flue of a cyclone, the flue gas, discharging the flue gas, the drying, the flue gas, the drying, the flue gas, the drying.
The dry sludge settled by the cyclone dust collector, the dry fine sludge separated by the bag-type dust collector and the dry sludge discharged by the drying tower are sent into a rotary kiln for burning, the ash and slag discharged by the rotary kiln and a secondary combustion chamber are lifted by a sludge adjusting cylinder and a negative pressure air suction type lifter and then enter a slag storage tank, finally the slag storage tank is loaded and transported, the sewage discharged by the purifying tower is collected and then discharged into a sewage treatment system for treatment, and the whole system is operated in a negative pressure state, so the dust cannot be discharged.
In a word, the sludge treatment process adopts a sludge spray drying (direct drying) + disc drying (indirect drying), a rotary kiln and an industrial leftover material (solid waste) collaborative incineration and flue gas purification system integrated device, collects sludge drying and a process of dry sludge, industrial leftover material (solid waste) collaborative incineration and flue gas purification in bodies, well solves the problem of comprehensive utilization of sludge and industrial solid wastes, achieves the purpose of double waste treatment of sludge and industrial solid waste, can save a large amount of energy at the same time, saves the treatment cost by 40 percent compared with natural gas auxiliary fuel, has very good investment value, has the characteristics of realizing sludge reduction (up to 92 percent at most), harmlessness, stabilization and recycling, and adopts a proper pretreatment process and an incineration means to incinerate wastes as far as possible, change the incinerated substances into harmless substances and reduce the volume to the maximum extent, reduce the generation of new pollutants as far as possible, so as to avoid secondary pollution, achieves the maximization of the utilization of heat energy of sludge, can meet the more and more strict environmental requirements, and is considered as a rapid and economic treatment method which is the GB 6385 and is the most advanced as a rapid and thorough pollutant discharge standard.
Sludge feeding system:
is that water content of 70-80% is poured into underground receiving system, lifted by shaftless auger, screw pump is sent into large sludge storage tank by filter, then sludge is sent into high level mud tank by plunger pump, finally lifted by screw pump and sent into spray drying tower, and directly pumped into high level mud tank by plunger pump through sludge filter, and equipped with two control modes of manual and electric (central control room), the engineering sludge is loaded into sludge receiving tank , the effective depth of sludge receiving tank is 4.5m, a brick-mixed structure sealed room is built above the sludge receiving tank (tank), floor area is 70m2, filter screen is mounted above the receiving tank to screen out large impurity in sludge, besides, air exhaust ports are respectively arranged above the receiving tank (tank) and on the top of sludge low level storage tank, the air in the sludge receiving tank is pumped as combustion-supporting air of sludge incinerator, the storage tank area forms negative pressure to prevent the extracted air from being sent into combustion chamber, wherein the extracted air is oxidized in combustion process, and meets discharge standard GB of odor discharge limit of odor eliminating factory, and odor discharge standard No. 54-54 GB can be discharged in odor emission standard of factory.
Two shaftless packing augers are arranged in a sludge receiving tank, the sludge is lifted to a screw pump on the side of the sludge receiving tank by the shaftless packing augers and then is respectively lifted to two sludge receiving tanks by the two screw pumps, the sludge receiving tanks are provided with two sets, the height of each sludge receiving tank is 18m, the radius of each sludge receiving tank is 10.5m, the storage capacity of each sludge receiving tank is 1500m3, two plunger pumps with hydraulic stations are arranged on the periphery of each sludge receiving tank, the plunger pump is , the sludge of the sludge receiving tanks is lifted to a high-level sludge storage tank in a factory building by the plunger pumps, a sludge filter is arranged on a pipeline, large particles in the sludge are screened out in a step, the high-level sludge storage tank mainly provides feeding sludge for a drying tower, and two control modes of manual operation and electric operation (a central control room) are simultaneously adopted, the capacity3
Four DN400 pipelines are arranged below the high-level sludge storage tank and are controlled by a manual valve , the sludge respectively falls into 4 screw pump receiving ports, the lifted sludge is sent into a spray drying tower and atomized by a tower top nozzle, the pipelines before the sludge atomization are respectively provided with a tower top flowmeter, each tower is provided with 4 atomizing nozzles, the consumption of compressed air at each nozzle is 7m3/min, the pressure is 0.45MPa, the compressed air is conveyed to the tower top by an air compressor room main pipe and is divided into 4 strands at the atomizing nozzles, and a pressure transmitter is arranged on an air pipe and is connected with a control room computer to adjust the amount of the compressed air entering the tower so as to achieve the optimal atomization effect.
2. Sludge drying system:
the drying tower of the engineering has the diameter of the drying tower from phi 10m to phi 15m, and the effective height of the drying process is 25 m. Each tower is provided with 4-10 atomizing nozzles, and the spraying angle of each nozzle is adjustable between 50 ℃ and 80 ℃; the amount of compressed air at each nozzle is 7m3Min, pressure 0.45Mpa, sludge treatment capacity of each nozzle 4m3H is used as the reference value. Auxiliary equipment such as an atomizing system, an air distribution system and the like are arranged in the drying tower, the atomizing system is used for forming the sludge into granular droplets with the particle size of 30-500 mu m, and the sludge is naturally granulated after drying; the air distribution system has the function of enabling air distribution in the drying system to be uniform, and improving the heat utilization efficiency while more effectively drying the sludge. The air quantity source of the air distribution system is high-temperature flue gas generated by the incineration system. The compressed air is delivered to the top of the tower through a header pipe and is divided into 4 strands at the atomizing spray head, and a pressure transmitter is arranged on an air pipe and is connected with a control room computer for adjusting the air consumption.
The temperature of the high-temperature flue gas entering the top of the spray drying tower is 550 ℃, the pressure is-500 Pa, and the high-temperature flue gas is output from the outlet of the waste heat boiler. An air supplementing system and a main air valve are arranged on the tower inlet flue gas pipeline and used for adjusting the air quantity: the thermocouple is arranged on the high-temperature flue gas pipeline to measure the temperature, the thermocouple and the pressure transmitter are arranged on the mixed flue gas pipeline, all temperature and pressure monitoring is connected with a computer in a control room, the temperature and pressure changes are monitored in time, the opening degree of the cold air valve and the opening degree of the main air valve are adjusted, cold air comes from the treated gas of the inner chimney, and the gas taking has the advantages of energy conservation and low oxygen content. The temperature of the sludge discharged from the drying tower is 50-60 ℃, and the water content of the discharged sludge is about 20%.
The drying tower is made of heat-resistant stainless steel SUS310S and 2205, the heat-insulating material is an aluminum silicate fiberboard, the heat-insulating thickness is determined according to different temperature partitions, the maximum thickness of the heat-insulating thickness is 250, the minimum thickness is 100, and the heat-insulating material is externally provided with a 304 stainless steel outer skin. The design does not consider the control of the drying tower on the oxygen content because the volatile gas quantity generated in the drying process and the dust concentration in the tower are both very low and are far lower than the explosive limit of combustible gas and dust concentration. The water content of the sludge with the water content of 80 percent is reduced to 20 percent after drying.
The spray drying is to disperse the dewatered sludge with the water content of about 80 percent into fine particles like fog through the action of an atomizer, (increase the heat transfer surface area, accelerate the drying), contact with the incineration high-temperature flue gas, remove most of water instantly, and dry the solid matters in the materials, the drying process is rapid, the heat utilization rate is high, the incineration high-temperature flue gas is used for directly drying the atomized sludge, the heat loss of a complex heat exchanger is avoided, the heat utilization efficiency can be improved to more than 80 percent, the effective atomization and the drying are rapid, the problems of blockage and abrasion are avoided through the effective atomization of the sludge, the dried sludge particles are uniform and reasonably distributed (60-120 meshes), the incineration is facilitated, the spray drying tower is safe and stable, the drying degree of the sludge particles is regulated and controlled, the safety is ensured (the dust explosion is avoided), the flue gas temperature is rapidly reduced from 550 ℃ (less than 1.5s) to below 200 ℃, the regeneration of dioxin and the precursor thereof can be prevented, the volatile organic gas is generated in the rapid drying process, and heavy metals and the like can be adsorbed in the atomized sludge, so that the drying tower has the flue gas pretreatment function, the.
The spray drying has the following process characteristics:
(1) the system has high thermal efficiency:
desiccation means the evaporation of water, which heats up from ambient temperature (say 20℃.) to boiling point (about 100℃.), and requires about 80kcal of heat per liter of water, and then changes from liquid to vapor phase, and also absorbs a significant amount of heat, which requires about 539kcal (normal atmospheric pressure) per liter of water, so that a minimum of 620kcal of heat is required to evaporate each liter of water. In a common sludge drying process, such as a fluidized bed low-temperature drying process adopted at a Shanghai stone cave, the working temperature is controlled to be about 85 ℃ for safety, heat absorption of 65kcal is required when each liter of water is heated from 20 ℃ to 85 ℃, heat consumption of 548kcal is required when the water is vaporized at 85 ℃, and the sum of the two is 613 kcal.
In the spray drying tower, the inlet temperature of the high-temperature flue gas can reach 550 ℃, the exhaust temperature of the waste gas is about 110 ℃, and the dust content in the waste gas is much lower than the safety control limit value, so that the heat utilization efficiency of the spray drying tower is greatly improved compared with a fluidized bed adopting an indirect drying process.
(2) High drying speed and high strength. The surface area of the fog drops is increased after passing through the nozzle, the required drying time is short, and the overall drying strength can reach 12-15 kg/(m3 h).
(3) The temperature of the droplets during drying is low. In the high-temperature air flow, the temperature of the material with the wet surface does not exceed the wet bulb temperature of the drying medium, and meanwhile, the spray drying is suitable for drying the sludge because the drying is rapid and the temperature of the final product is low.
(4) The dried sludge has good dispersibility and fluidity. Since the drying process is carried out in air, the dried product can maintain substantially the same spherical shape as the droplets.
(5) Simple structure, operation control is convenient.
However, in this way, it is often difficult to effectively prevent the sludge from adhering to the bottom of the bed due to the change of the properties of the sludge raw material or the change of the operating environment, which not only increases the investment cost of the system, but also increases the power consumption of the system, thereby resulting in a large amount of operating cost.
The spray drying system adopts a novel special two-fluid atomized sludge system, and the atomized sludge system is left together with the high-temperature flue gas, and the tower diameter and the tower height are adjusted by optimizing the structure of the drying system according to the characteristics of the sludge and the contact condition of the atomized sludge and the high-temperature flue gas, so that the phenomenon of sludge wall adhesion is avoided. The service life of the drying tower can be prolonged, the drying tower can keep continuous operation for a long time, and the investment and the operation cost of a drying incineration plant are reduced.
(6) The drying process is carried out in a closed drying tower, the internal space is negative pressure, the leakage and flying of the dried product and toxic and harmful gas in a workshop are avoided, air pollution can be effectively prevented, and the production environment is improved.
(7) Is suitable for continuous and large-scale production, spray drying can be operated for 24h all day, and the highest single machine processing capacity can reach 320-500t/d (the water content is calculated by 80%).
(8) The spray drying system adopts direct drying and has no heat exchange surface, so that the equipment wear is small, the sludge sand content in the sludge in China is high, the wear phenomenon is serious, and the problem of can be well solved by adopting spray drying.
(9) The investment and operation cost is low
Relatively speaking, the spray drying system has a simple structure, the investment cost is only 40% -50% of that of the traditional fluidized bed drying system, the high-efficiency sludge atomization system and the hot air distribution device are adopted, small-particle wet sludge can be fully mixed with high-temperature flue gas, and dry sludge particles only need to flow down along the tower under the action of gravity in the system, so that the power consumption is much lower, the power consumption of the system is only about 40kW/t wet sludge (80% of water content), and the operation cost of the system is effectively reduced.
(10) Small floor area
The spray drying system adopts vertical multilayer arrangement, occupies small area and is very suitable for sludge incineration projects beside sewage plants.
The sludge drying process is the mainstream process for sludge treatment in developed cities in China at present (particularly in cities with scarce land resources). The quality of the drying process directly influences whether the whole sludge drying system can continuously, stably and reliably operate and the treatment cost. The spray drying and disc drying process is the mainstream drying process of sludge in China, and the combined application of the two drying processes is very suitable for treating sludge with the water content of 50-80%. The process system is simple, the number of equipment is small, the number of fault points is small, the operation is stable, and the maintenance and the overhaul are convenient. In addition, the running workshop adopting the system has no problems of dust, stink and the like, and the field working environment is good.
The super-disc dryer adopts a steam indirect heat exchange mode, water is evaporated more quickly by stirring materials, the dryer is suitable for semi-drying and full-drying of the materials, a main body of the dryer consists of cylindrical shells, hollow shafts and groups of hollow discs welded on the shafts, a heat medium flows through the hollow discs and indirectly transmits heat to sludge through the discs, the sludge passes between the super-disc and the shells, receives heat transmitted by the super-disc and evaporates water, and generated water vapor is gathered in a dome above the super-disc and is taken out of the dryer by a small amount of ventilation.
For sludge with low water content, such as sludge of wool washing wastewater, the sludge is dehydrated and dehydrated at low temperature to form granular sludge with the water content of about 50-70%, the sludge cannot be pumped due to no fluidity and can not directly enter a spray drying system, the wet sludge is transported to a wet sludge pit through a vehicle, is grabbed to a buffer hopper by a crane grab bucket, is transported to a disc dryer through a wet sludge screw under the buffer hopper in an adjustable manner, and indirectly heats the sludge by using saturated steam (0.5MPa.G saturated steam) as a heating medium. The heated steam condensate is pumped back to the boiler deoxygenation water tank through a condensate collection system for reuse. The dry sludge passes through a screw conveyer and then enters a chute
The material inlet finally enters the rotary kiln and sludge from the spray drying tower is mixed at for incineration.
The equipment is characterized in that:
because the single-shaft disc combined hollow shaft is adopted for heat transfer, a can manufacturing process is introduced during the body manufacturing, the reliability of the body is improved, and the manufacturing cost is reduced. The characteristics are summarized as follows:
1. an air supply port is arranged, so that the tail gas emission is smoother, and the system load is reduced;
2. the reliability is high, the continuous operation is good, the operation can be performed day and night, and the method is suitable for drying materials with large treatment capacity for a long time;
3. the oxygen content, the temperature and the dust amount are low during operation, and the safety is good;
4. the left surface and the right surface of each vertical disc of the horizontal disc dryer transfer heat, so that the heat transfer area is large, the structure is compact, and the overall dimension is small;
5. the auxiliary equipment is less, and the system is simple;
6. the sludge in the dryer is wet sludge, and in order to prevent the sludge from being bonded on the turnplate, a fixed longer scraper is arranged on the inner wall of the shell and extends into a gap between the turnplates, so that the functions of stirring the sludge and cleaning the turnplate surface are achieved;
7. a low-temperature heat source (less than or equal to 180 ℃) is adopted for heating, so that the sludge on the disc cannot be overheated when the disc is stopped;
8. the required auxiliary air is less, and tail gas treatment equipment is small;
9. the horizontal disc dryer can be applied to a semi-drying process and can also be applied to a full-drying process;
10. adopting a steam heat transfer medium;
11. the cover on the upper part of the machine body can be completely opened, so that the maintenance is convenient;
12. the maintenance is less, the continuous operation is good, the operation can be performed day and night, and the operation in 8000 hours every year is ensured;
13. the emergency starting can be realized in a power failure state, and the operation is stable;
14. the structure is firm and durable.
3. Sludge incineration system:
an incineration system: and (3) after spray drying and rotary disc drying, feeding the dried sludge with the water content of 20-30% into a rotary kiln for incineration through a stokehole feeding screw respectively, burning industrial solid waste in a hot air furnace, and directly feeding flue gas into an incinerator through the hot air furnace for incineration in cooperation with the sludge.
The hot blast stove in the process incineration system adopts a traditional direct-fired (biomass and coal-fired) hot blast stove type, equipment optimization and transformation are carried out, the hot blast stove is suitable for feeding industrial solid wastes such as textile leftover materials and the like, the leftover materials enter a hopper through a feeding machine and then are added into a horizontal chain grate to realize the processes of drying, pyrolysis, combustion, burnout and the like, leftover materials with fixed thickness in the hot blast stove are combusted in a hearth to generate high-temperature flue gas to enter a sludge incineration system, the temperature of the hot blast stove can be controlled according to process requirements, burnout slag is discharged from the other end of the chain grate to a slag extractor and is sent out through an automatic slag extractor, a combustion hearth is built by using high-temperature-resistant refractory materials, and the whole combustion system is electrically.
The sludge burning system adopts a rotary incinerator-rotary kiln, hot blast stoves (industrial leftover materials) are integrated to the kiln head of the rotary kiln, high-temperature flue gas generated by combustion of the hot blast stoves is mixed with flue gas generated by combustion of dried sludge in the rotary kiln, carbon powder/dust and high-temperature coal gas brought by the flue gas enter a secondary combustion chamber for sufficient combustion and polymerization and settlement, high-temperature hot flue gas (about 750-1000 ℃) subjected to secondary combustion enters a waste heat boiler, waste heat is recovered by the waste heat boiler, the waste heat enters a drying tower as a drying heat source of wet sludge, finally the waste flue gas enters a tail gas treatment system, a kiln head, a body, a kiln tail, a transmission mechanism and the like of the rotary kiln are divided into a kiln head, a set of multifunctional burners and a combustion-supporting air for transmission, the rotary kiln is sealed by a traction rope sealing system, the kiln head sealing device of the incinerator is sealed by a push-resistant graphite block, the sealing ring gear is used for protecting a kiln hood of a fire-resistant material, waste collecting and a waste material leakage collecting device is arranged at the lower part of a rotary kiln hood, the kiln body, the rotary kiln body, the kiln is sealed by a television set of a tail gear box, a tail gear ring gear, a tail gear box, a tail gas conveying belt gear box is connected with a tail gas conveying belt gear, a tail gas conveying belt wheel, a tail gas conveying belt wheel, a tail gas conveying belt wheel, a tail belt wheel.
3.1 incineration system composition:
the sludge incineration system consists of the following main devices:
a rotary incinerator: incinerator body, gear drive mechanism, refractory lining, wind distributor, etc.;
hot blast stove: the hot blast stove comprises a hot blast stove body, a feeding system, a slag discharging system, an air distribution system and the like;
ignition and auxiliary combustion equipment: ignition burner, ignition burner fan, spiral slag conveyor and the like;
a second combustion chamber: a second combustion chamber body, a refractory lining and the like;
a combustion air system: including blowers and the like;
① Rotary incinerator, which is the most important part of incineration plant and where all the incineration reactions that determine the discharge result take place, consists of sludge distributor and hearth, the sludge distributor is to make the air contact with the sludge to the maximum in the load range of incinerator, the sludge distributor adopts bar grating structure to divide the sludge into small flows to generate good sludge flow distribution, make the sludge flow contact with high temperature air to the maximum for full and fast combustion, and make the solid in the incinerator flow to the slag outlet smoothly.
② the incinerator hearth is heat insulation hearth, the inner wall is wear resistant and high temperature resistant material, the fire resistant layer is outside heat insulation material, the outmost layer is steel welding cylinder to ensure the hearth sealing, the incinerator head is mounted with start-up burner, secondary air nozzle, necessary measuring instrument, and explosion proof on the incinerator smoke outlet pipeline, the fire resistant and heat insulation material ensures the room temperature, the outer wall temperature of the incinerator is not higher than 50 ℃.
③ ignition and auxiliary combustion equipment, the incinerator is equipped with ignition burner, combustion-supporting is diesel oil, when the incinerator is started, the ignition burner is needed to raise the incinerator temperature to 850 deg.C, the sludge is put in, when the incinerator is normally operated, the oil supply amount is adjusted or the incinerator is stopped operating according to the change of the heat value and solid content of the sludge.
④ air burning system, the air quantity needed by sludge burning is times of air and secondary air, times of air is supplied by auxiliary burner, the high temperature air from burner is distributed uniformly on the cross section of the whole furnace bed to generate full contact with small stream of mud to dry the residual water in the mud quickly and raise the temperature of the mud to burn it, the secondary air is fed by air pipe installed on the furnace end to supplement the air needed by the mud burning completely and form strong turbulence in the suspension burning space to maintain the best burning condition and control the formation of CO and NO X.
⑤ A facility for storing and transporting slag, wherein the slag of an incinerator flows from the furnace end to the furnace end along with the rotation of the incinerator, the slag is cooled by water spraying, and the slag is transported to a slag pot through a pneumatic transport system, wherein if the slag generated in the incineration process is identified as -shaped solid waste, the slag is temporarily stored in the slag pot and then is transported to a brick factory for making bricks or a nearby cement factory for producing cement or bricks.
The incinerator is characterized in that:
the strip-shaped grating mud distributing structure device is adopted to ensure that the fluidized mud entering each area of the incinerator is fully contacted with high-temperature air. The rotary furnace has large heat storage capacity, can reduce the influence of the fluctuation of the moisture and the heat value of the sludge on the combustion, and ensures that the sludge with low heat value is more stably combusted. The combustion temperature is uniform, the NOx generation amount is low, the excess air coefficient is small, and the efficiency is high.
The sludge is sent into the incinerator by the sludge spreader, so the sludge has strong combustion stability.
The hearth pressure of the incinerator is automatically controlled by a draught fan with a variable frequency motor, and the starting time is short.
Hot-blast stove (industrial leftover material) technical parameter book
The process is analyzed according to the material source, the materials entering the hot blast stove mainly comprise spinning leftover materials, the water content entering the stove is calculated by 20 percent, and the reduced heat value of industrial solid waste is 14.7MJ/kg as the design basis.
Load of the hot blast stove: 400 ten thousand large cards
Design of in-furnace industrial solid waste (textile garment scrap): 4167kg/h
Solid content in the furnace industry: 80 percent of
Ash scorching and reducing rate: < 5%
Incinerator load variation range: 70 to 110 percent
3.2 technical parameters of rotary incinerator
The project is analyzed according to the material source, the sludge entering the rotary kiln is mixed and matched with municipal and industrial sludge, the water content entering the kiln is calculated as 20%, and the reduced heat value of the sludge is 8.9MJ/kg as the design basis.
The incinerator can ensure the sludge to be completely incinerated, the temperature of the flue gas in the hearth is above 650 ℃, the temperature is above 850 ℃ after the flue gas enters the second combustion chamber, and the retention time is not less than 2.5 seconds.
Size: outer diameter/inner diameter phi 3700/phi 3000 length L is 21.5m
Designing the amount of dry sludge in a single furnace: 5208kg/h
The rotating speed is 0.2 to 2rp/min
The inclination is 2.5%
Designing the solid content of the sludge in the furnace: 80 percent of
Ash scorching and reducing rate: < 5%
Incinerator load variation range: 70 to 110 percent
4. The dried sludge ignition flame system comprises:
the dried sludge ignition flame system adopts a natural gas burner, and the equipment is characterized by complete combustion and no black smoke. The hot blast stove generates 500-1000 ℃ flame, the dried sludge is heated to the ignition temperature (about 300 ℃) and is made to spontaneously combust, and combustion-supporting air is fed by the high-pressure fan through a pipeline. Natural gas heating value 8500kcal/m 3. The specification of the hot blast stove is 600 ten thousand kilocalories per hour. Fan parameters: the air quantity 8306m3/h full pressure 11377pa power is 45 kw.
The process adopts a burner based on a low-nitrogen combustion technology, and the burner is a burner based on the low-nitrogen combustion technology in consideration of the fact that when natural gas is used as a standby auxiliary fuel and is used for unstable leftover material supply. It has the following characteristics:
1) the burner can give the most reasonable air-fuel ratio based on any furnace load point;
2) the burner can control the combustion air excess coefficient <1.15 based on any furnace load point;
3) the burner should have a high combustion efficiency;
4) the burner adopts a staged gas technology, is different from other burners, and is provided with two staged gas pipelines, wherein the gas flow of the two staged gas pipelines is respectively controlled, so that a better low-nitrogen effect is achieved, and the flame shape can be properly adjusted according to different hearths;
5) the adoption of the internal flue gas circulation technology ensures that the combustor can utilize the backflow flue gas in the hearth to further reduce the nitrogen oxides by .
5. Burning rotary kiln
And (4) feeding the dried sludge subjected to spray drying into a sludge incinerator for incineration through a slant feeding pipe by a chain conveyor. And (4) conveying the dried sludge subjected to disc drying into a rotary kiln for incineration through sludge conveying equipment.
The process adopts a horizontal rotary incinerator. The rotary incinerator is characterized in that high-temperature air from a hot blast stove is blown into the incinerator from a furnace end, so that the temperature of dried sludge is quickly raised and dried continuously, the dried sludge is completely combusted at the high temperature of 900 ℃, high-temperature flue gas generated by combustion is introduced into a secondary combustion chamber, then the high-temperature flue gas is distributed by cold air and enters a drying tower to be used as a drying heat source of wet sludge, and finally waste flue gas enters a tail gas treatment system.
The dried sludge is fed into the inclined tube through the dried sludge chain conveyor and then slides into the rotary kiln, and rotates from high end to low end in the rotary kiln. And (3) igniting the sludge after sliding into the rotary kiln and walking for 3-4 m, burning the sludge after walking for 21m, dropping the sludge into a slag discharging hopper after burning, and conveying the sludge to a slag suction system through a sludge adjusting cylinder.
The diameter of the rotary kiln is 3.7m, the length of the rotary drum is 21m, the inclination is 1-1.5 degrees, the rotating speed is 1-2 r/min, and the residence time of sludge in the kiln is adjustable within 20-60 min.
The air inlet of the rotary kiln is divided into two paths, paths of hot blast stoves supply heat flame, the temperature is 500-1000 ℃, paths of ambient air for adjusting the oxygen content in the kiln, and the exhaust temperature of the rotary kiln is above 850 ℃.
5.1 composition of the incineration system:
the sludge incineration system consists of the following main devices:
a rotary incinerator: the incinerator comprises an incinerator body, a gear transmission mechanism, a refractory lining layer, a mud distributing device and the like;
ignition and auxiliary combustion equipment: ignition burners, ignition burner fans, etc.;
a combustion air system: including blowers and the like.
(1) A rotary incinerator: incinerators are the most important part of an incineration plant, where all the incineration reactions that determine the outcome of the emissions take place. The incinerator consists of a sludge distributing device and a hearth. The function of the sludge distribution device is to make the air contact with the sludge to the maximum extent within the load range of the incinerator. The sludge distributor adopts a strip-shaped grating structure and is used for dividing the sludge into small flows to generate good sludge flow distribution, so that the sludge flow contacts high-temperature air to the maximum extent, the sludge is fully and quickly combusted, and the solid in the furnace can smoothly flow to a slag outlet. The mud distributing device has the characteristics of heat resistance, high-temperature gas corrosion resistance, simple structure, easy maintenance and small abrasion.
(2) The incinerator hearth adopts a heat insulation hearth, the inner wall adopts wear-resistant and high temperature-resistant materials, the outer side of the fire-resistant layer is made of heat insulation materials, the outermost layers are made of steel welded cylinders to ensure the sealing of the hearth, a starting burner, a secondary air nozzle and necessary measuring instruments are installed at the head of the incinerator, and an explosion-proof is reserved on a flue gas outlet pipeline of the incinerator.
(3) Ignition and auxiliary combustion equipment: the incinerator is provided with an ignition burner, and natural gas is used for supporting combustion. When the incinerator is started, the ignition burner is required to raise the temperature of the incinerator and then the sludge begins to be put into the incinerator, and when the incinerator is in normal operation, the amount of natural gas is adjusted according to the change of the heat value and the solid content of the sludge.
(4) The air quantity required by sludge incineration is times of air and secondary air, times of air is supplied by an auxiliary burner, high-temperature air from the burner is uniformly distributed on the cross section of the whole hearth and is fully contacted with a small stream of sludge to the maximum extent, residual moisture in the sludge is quickly dried, the temperature of the sludge is raised, and the sludge is incinerated.
(5) Slag storage and transport equipment: the furnace slag of the incinerator flows from the furnace end to the furnace tail end along with the rotation of the incinerator, flows to a slag collecting hopper, passes through a slag discharging machine, is combined with the furnace slag discharged from the second combustion chamber, is lifted to a slag storage bin through a negative pressure air suction type lifting system, and is finally transported outside through an automobile.
5.2 the rotary kiln incinerator has the characteristics that:
1. the strip-shaped grating mud distributing structure device is adopted to ensure that the fluidized mud entering each area of the incinerator is fully contacted with high-temperature air. The material raising plate is added, so that the sludge can be fully combusted, and the internal coking can be eliminated.
2. The rotary furnace has large heat storage capacity, can reduce the influence of the fluctuation of the moisture and the heat value of the sludge on the combustion, and ensures that the sludge with low heat value is more stably combusted.
3. The combustion temperature is uniform, the NOx generation amount is low, the excess air coefficient is small, and the efficiency is high.
4. The sludge is sent into the incinerator by the sludge spreader, so the sludge has strong combustion stability.
5. The hearth pressure of the incinerator is automatically controlled by an induced draft fan provided with a variable frequency motor.
5.3 Equipment Specifications
(1) And (3) rotary kiln:
quantity: 1 seat
Effective size: phi 3.7X 21m
The material is as follows: g20 main body boiler steel, kiln head 310S, kiln tail 310S, lining fireproof mullite plastic material, heat preservation pouring material
6. A second combustion chamber:
in order to ensure that harmful gas is burnt out and reaches the emission standard, the gas burned in the rotary kiln enters a secondary combustion chamber. The secondary combustion chamber adopts a vertical structure, the thickness of a heat-insulating wall body is 0.58m, so that the temperature of the secondary combustion chamber is not lower than 850 ℃, and the gas flowing time is not less than 2.5 seconds so as to decompose and control the generation of dioxin.
When the sludge heat value is low and the incineration heat value is insufficient, so that the temperature of a secondary combustion chamber cannot reach 850 ℃, a 300 ten thousand kilocalories per hour natural gas combustion system is arranged at the bottom side of the secondary combustion chamber, a combustion-supporting fan is provided with an air volume of 4328m3/h full pressure 10770pa power of 22kw for supplementing heat when the temperature is insufficient, in order to control dioxin-like substances, a 3T technology is adopted to inhibit the generation of the dioxin-like substances, gas generated by volatilization and pyrolysis in the incineration process forms high-temperature rotary backflow-shaped flame above 850 ℃ in the incinerator, the retention time of flue gas in a high-temperature area is more than or equal to 2s, the thorough incineration of organic matters and pyrolysis gas is realized, the generation of dioxin is avoided from the source, in order to remove the dioxin and heavy metals in the flue gas, the concentration of harmful substances such as the dioxin and heavy metals in the flue gas reaches the required emission index, an auxiliary purification measure for injecting activated carbon is added in the flue gas purification system, the activated carbon is applied adsorbent, the principle that the adsorbed large specific surface area (the specific surface area of the activated carbon is about 5000 mass of the activated carbon, and the flue gas is uniformly contacted with the turbulent flow, and the flue gas purification efficiency is about 10000.
6.1 waste heat recovery system:
after the smoke is fully combusted in the front-end rotary kiln and the secondary combustion chamber, the smoke temperature is higher than 850 ℃, a waste heat boiler is arranged at the top of the secondary combustion chamber, the smoke enters the waste heat boiler for waste heat recovery, and the exhaust temperature of the waste heat boiler is 550 ℃. The design and the construction of the waste heat boiler consider high utilization rate and long-term continuous operation, and fully consider high-temperature corrosion of the flue gas; the high-temperature area (850-500 ℃) of the waste heat boiler adopts a membrane wall radiation heating mode, and a flue inlet of the waste heat boiler is not allowed to be provided with a heat exchange pipe for directly blowing flue gas, so that high-temperature corrosion is avoided.
In order to fully recover the combustion waste heat, a boiler (160 ℃, 0.6MPa) matched with the incinerator is arranged for a heat source for drying the disc, and the waste heat is recovered to the maximum extent on the premise of realizing sludge reduction. The steam of most steam is connected into the disc drier as heating medium, the indirect heating sludge and steam system is provided with a steam collecting box for distributing steam for each process, and the steam collecting box and the boiler drum are respectively provided with safety valves. An emergency waterproof pipe is arranged on a steam drum of the waste heat boiler. The control of the boiler adopts automatic control and has control means of steam drum water level three-impulse adjustment and recording, steam pressure adjustment and recording, water level alarm, steam pressure alarm and the like.
The waste heat boiler comprises a boiler body and other parts, as well as a flue, a flue interface, an -time valve , instruments and the like in the range of each system, in order to prevent solid fly ash from fouling convection heating surfaces and influencing the heat transfer effect of each heating surface, fixed soot blowers are arranged on a calandria and the boiler body, and soot blowing is regularly carried out through an automatic control system to ensure the cleanness and the heat transfer effect of the convection heating surfaces.
Due to the stirring and rolling of the rotary kiln, a large amount of dust is clamped in the generated flue gas, and soot blowing and cleaning are needed in the operation process of the waste heat boiler so as to ensure efficient heat transfer and stable steam generation.
Technical parameters of the waste heat boiler are as follows:
rated evaporation capacity 2t/h
Rated operating pressure (gauge pressure)
Saturated steam temperature deg.C
The temperature of the feed water is 114 DEG C
The temperature of a smoke inlet is 850 DEG C
The temperature of a smoke outlet is 550 DEG C
Boiler resistance 1500Pa
Inlet dust concentration 5000mg/Nm 3
The outlet dust concentration is 500mg/Nm
7. Flue gas processing system:
7.1 flue gas treatment (purification) process:
the engineering adopts a waste gas treatment process of 'cyclone dust collector, two-stage bag dust collector, activated carbon adsorption, ozone denitration and deodorization, three-stage spray tower washing, whitening and demisting'. The process technology is designed aiming at the problem that the particle size of smoke dust contained in the generated waste gas is large in the sludge drying and incineration process, and is characterized by large operation flexibility, high removal rate of harmful substances and dust, low consumption of reactants, good deacidification effect, low emission concentration of heavy metal and dioxin, treatment of the discharged waste water in a sewage treatment system, easy control of system operation, low comprehensive cost and the like.
The waste gas discharged from the bottom of the spray drying tower contains dust, a small amount of volatile organic compounds, CO, HCl, SO2, NOx, heavy metal compounds and other toxic and harmful substances. The waste gas discharged from the drying tower firstly enters a cyclone dust collector, then enters two bag-type dust collectors arranged in series, is discharged into three spraying towers for washing after passing through a main induced draft fan of the system, an ozone feeding pipeline is arranged on a connecting air pipe between the bag-type dust collectors and a purification tower, and finally is washed, desulfurized and denitrated through the spraying towers, and then the demisted and purified flue gas is discharged to the high altitude through a chimney after being monitored on line; the emission index can be far lower than the GB18485-2014 limit requirement and reaches the European Union 2010/75/EC standard.
The bag-type dust remover adopts the Danish Jinerkang dust removal technology, and has the advantages of automatic timing back blowing, good dust removal effect, ash discharge of a flat-bottom scraper, circular tangential air inlet of a shell and external filtration type design, and the dust removal efficiency is 99.9 percent. Dust in tail gas discharged by the spray tower can be effectively removed by using a bag-type dust collector for dust removal; an active carbon injection port is arranged on a flue gas pipeline between the two bag-type dust collectors, and the active carbon injection device injects powdery active carbon into the flue; so as to adsorb harmful substances in the flue gas, such as dioxin, heavy metals and the like. Passing through a rear bag-type dust collector; and (3) independently collecting and managing part of dioxin substances and heavy metal compounds adsorbed on the dust as hazardous wastes. Tail gas discharged by the bag-type dust collector enters the spraying tower through a system induced draft fan; an ozone feeding point is arranged on an air pipe behind the bag-type dust collector; decomposing organic odor in the tail gas by ozone, purifying the tail gas, oxidizing NO into high-valence NOX, and purifying the tail gas; the tail gas after the advanced oxidation deodorization process enters from the lower side of the spray tower, and the gas is firstly subjected to alkaline washing by three spray towers, SO that dust and dissolved substances in the gas can be removed, and acidic substances such as HCl, H2S, SO2, NOx and the like in the waste gas can be absorbed. The alkali liquor is NaOH and is pumped to a high-level alkali storage tank by an alkali liquor pump, the liquid level is automatically controlled, then the alkali liquor is added to a spray tower from the high-level alkali storage tank, the spray tower spray is pumped to a purification tower nozzle by a plastic lining pump, and the spray tower sprays from top to bottom in sections. And the waste liquid generated by spraying is returned to a sewage treatment plant for centralized treatment through a sewage pipeline.
7.2 white smoke abatement procedure (white removal):
the process selects a Japanese HINO-TEC technical device, mainly utilizes gas-gas heat exchange, flue gas enters a white smoke abatement device through a dehydration spray tower, the flue gas is cooled through a HINO-PILE plate heat exchanger, a large amount of moisture is condensed, simultaneously, a large amount of heat energy is released during moisture condensation to heat ambient dry air, then, the heated dry air is mixed with the flue gas after cooling and dehydration, so that the absolute humidity of the mixed flue gas is greatly reduced, the dew point temperature of the exhausted flue gas is not reached within a short time after the exhausted flue gas is exhausted, and the purpose of abating the white smoke is achieved.
And finally, demisting and dehydrating the tail gas by a tail gas treatment system, and enabling the demisted and dehydrated tail gas to enter an inner chimney. An on-line flue gas monitoring system (self-care of Party A) is installed on an inner chimney to monitor the index of the exhaust component in real time to meet the requirement of GB18485-2014 limit, and the specific steps are shown in the following table:
monitoring items Standard limit value Remarks for note
Smoke dust (mg/m)3) 20 Measuring device
Sulfur dioxide (mg/m)3) 80 Measuring device
Nitrogen oxides (mg/m)3) 250 Measuring device
Dioxin (TEQng/m)3) 0.1 Non-measurable, sample-taking and inspection
Note: the engineering process design reaches the European Union 2010/75/EC standard.
The height of the flue gas discharge port is 45m, and a gas online monitoring system instrument is arranged before discharge according to the standard requirement.
The aspect of storage tank odor treatment considers that: the engineering is provided with a sludge receiving bin and a storage system. In order to prevent odor from diffusing, the sludge receiving bin and the storage system are used for exhausting air, and the odor-containing gas is used as combustion air of the hot blast stove. The exhaust gas satisfies the maximum emission limit of the emission Standard for malodorous pollutants (GB14554-93) by the thermal decomposition of the odor.
The odor emitted by other unorganized plants can meet the secondary emission standard of the factory boundary specified in the emission standard of malodorous pollutants (GB 14554-93).
In the operation of the system, sewage is generated, the tail gas is mainly used for treating desulfurization spraying sewage, the demister is used for condensing and whitening sewage, ground washing sewage and worker domestic sewage, and the total amount is about 120 plus 150t/d, and the sewage enters a pipe network of a sewage treatment plant for centralized treatment through a sewage pump.
7.3 heating and ventilating system:
the heat supply system comprises a hot blast stove, an air inducing device and a flue gas pipeline, wherein the air inducing device comprises two parts, the part introduces air to the hot blast stove to be used as combustion-supporting air, the air is combusted and preheated by the hot blast stove and then is sent into the rotary incinerator, the second part introduces flue gas discharged by the sludge incinerator into the sludge drying system, a heat source of the drying system mainly comes from 650 ℃ waste heat flue gas discharged by the sludge incinerator and formed by air distribution of the flue gas with the temperature of more than 850 ℃ and cold air, and the 650 ℃ waste heat flue gas is distributed by a corresponding hot air distribution system and then enters the top of the spray drying tower, namely the downstream direct heating mode adopted by the drying process of.
7.4 flue gas cleaning System Process description
The process is a subsequent flue gas treatment matched project, the design treatment air quantity is about 3.1 ten thousand square standard dry gas quantity, and the flue gas temperature is 110 +/-10 ℃. The incineration flue gas is treated by the system to reach the national emission standard.
The flue gas purification system refers to all equipment and facilities which are arranged for meeting the requirements of flue gas purification and enable the flue gas to flow from the flue gas outlet of the drying tower to the outlet of the flue pipe chimney. The tail gas treatment process adopts a combined process of a cyclone dust collector, a two-stage bag dust collector, activated carbon injection, ozone denitration and deodorization, washing of a purification tower and whitening and demisting.
The flue gas temperature of a flue gas outlet of a drying tower is about 110 ℃, the flue gas firstly enters a cyclone dust collector, an electric star-shaped valve is arranged at the bottom of the cyclone dust collector and is used for discharging settled dry sludge, a pressure transmitter and a thermometer are arranged at an outlet of the cyclone dust collector and are used for monitoring the circulation condition of the flue gas, and the flue gas after passing through the cyclone dust collector enters a bag-type dust collector.
The bag-type dust collector is provided with a back-blowing device, the filter bag in the bag-type dust collector is back-blown regularly by utilizing compressed air, and dust attached to the surface of the filter bag is blown off by instantly back-blowing excessive air, so that the bag-type dust collection efficiency is improved.
In order to remove nitrogen oxides in the flue gas, ozone is introduced into a flue gas pipe at the rear part of the second-stage bag-type dust collector, so that organic odor in the flue gas is removed and fully reacts with the NOx in the flue gas, and the aim of denitration is fulfilled.
Flue gas exhausted by a bag-type dust collector enters a wet spraying system, the wet spraying system is provided with three spraying towers in total, -level spraying towers are filled with alkali liquor to treat acid gas, the lower parts of , second-level and third-level spraying towers are mutually communicated, circulating alkali liquor at the lower parts is used for supplementing alkali and water according to actual conditions, the flue gas sprayed by -level is washed, alkali liquor adding ports are prepared for the second-level and third-level spraying, and when -level spraying deacidification effect is insufficient, -level spraying is carried out for deacidification, dust removal and temperature reduction, so that the overall treatment effect is ensured.
The method comprises the steps of removing harmful components and trace dust in flue gas through a spraying system, ensuring that the flue gas is discharged after reaching the standard, in order to ensure the deacidification effect and facilitate the tail gas in the running state to be discharged after reaching the standard, -stage spraying tower is provided with two spraying ports, 8 spray nozzles are arranged in each spraying port, stages of pumps (atomizing alkaline washing pumps) arranged behind a high-level alkaline tank are conveyed to an alkaline liquor nozzle in the middle of -stage spraying tower to atomize NaOH solution into fine liquid drops, the NaOH solution is uniformly distributed in the spraying tower and fully contacts flue gas with the maximum surface area, high-valence NOx, SO2 and other acid gases after being oxidized by ozone are fully reacted and removed, an alkaline liquor feeding system is used for keeping the pH value of the circulating solution about 8-9, the liquid-alkaline concentration is ensured, the removal rate of NOx, SOX and the like can reach more than 80%, -stage spraying tower is provided with two centrifugal pumps, is provided with , alkaline spraying liquid is provided with a centrifugal pump, alkaline spraying liquid spray nozzles at the bottom of the spraying tower, alkaline spray tower is used for delivering alkaline spray liquid spray mist removal, the alkaline spray mist removal tower bottom of the tail gas, the tail gas dust removal tower, the tail gas is carried out, the tail gas removal tower is carried out by a spiral spray mist removal device, the centrifugal pump is carried out, the centrifugal pump is carried out the centrifugal pump, the centrifugal pump is carried out the centrifugal pump.
8. Cyclone system:
8.1 System:
the cyclone dust collector is used as a middle channel of a drying tower and a tail gas treatment system, and is used for enabling a dust-containing airflow to rotate, separating dust particles from the airflow by means of centrifugal force and collecting the dust particles on the wall of the drying tower and the tail gas, and enabling the dust particles to fall into an ash bucket by means of gravity.
8.2 principle of operation
An electric star-shaped valve is arranged at the bottom of the cyclone dust collector, and when the cyclone dust collector operates normally, the manual gate valve keeps an open state. The smoke from the drying tower is carried with dust and passes through the cyclone dust collector, the dust particles are separated from the air flow by means of centrifugal force and collected on the wall of the cyclone dust collector, then the dust particles fall into the dust hopper by means of gravity, and enter the bottom of the dust collector, and the dry mud and dust particles are conveyed into a bottom dry mud conveying system through a star-shaped discharge valve continuously running at the bottom of the tower.
9. A bag dust removal system:
9.1 System:
the 9.1.1 bag-type dust collector adopts a circular design, and has tangential air inlet and no dead angle. The key point of the system is that an electrical control system with reasonable design is adopted, 84 pulse jet pipes are subjected to pulse back blowing in sequence, and high-quality PPS + pure PTFE membrane filter bags are selected as the filter bags, so that the dust removal effect reaches that the dust is less than or equal to 10mg/Nm 3. Meanwhile, in the operation process of the filter system, under normal load, the maximum pressure difference in the back blowing process is kept below 800Pa, the operation is reliable, the back blowing and dust removing performance of the filter bag is excellent, the bottom of the dust remover is flat, and the dust at the bottom is cleaned in real time by adopting a rotary scraper system, so that the dust accumulation is avoided. The dust remover has good sealing performance in the whole structure, is fully covered by heat preservation, and avoids the occurrence of local corrosion.
9.1.2 mainly include pulse blowback device, filter dust pelletizing system, active carbon dosing system etc. every sack upper portion and lower part all set up maintenance , the sack of being convenient for is maintained and is overhauld, this flue gas processing system sets up two sack cleaners altogether, two sack cleaners are established ties in normal operation, flue gas import is equipped with trip valve , in order to prevent the trouble overtemperature, powdered activated carbon sprays the import of second grade sack through active carbon injection apparatus, fully mix with the flue gas in the flue, pollutants such as heavy metal in the flue gas, dioxin are adsorbed by the active carbon and get into the sack cleaner along with the flue gas, heavy metal, dioxin and dust by the active carbon adsorption are separated in the sack cleaner, collect the processing according to danger waste.
9.1.3 the device has now been made homemade with its innovative application by Huanjiang Huanxing machines Limited. The innovation points are mainly as follows:
(1) under the control of a reasonable electrical system, the parallel multi-path pulse injection pipes are adopted to randomly and sequentially perform back blowing, so that the injection effect is obvious;
(2) the box type pulse is changed into the line pulse, each filter bag is subjected to back blowing, a unique Venturi blowing pipe is designed, and the back blowing and dust removing effects are improved;
(3) the temperature of the flue gas at the inlet of the dust collector must be strictly controlled below 110-140 ℃ to avoid the dewing and damage of the cloth bag; the length of the filter bag is designed to be 8 meters, air enters tangentially, the filter bag is a high-quality PPS + pure PTFE film-coated filter bag, dust particles can not penetrate through the film due to the extremely fine fiber tissue of the film, so that the dust emission is close to zero level, and the dust cleaning performance is excellent due to the characteristics of no dust adhesion, hydrophobicity, stable chemical performance and the like of the PTFE film, so that the bag pasting phenomenon is avoided;
(4) the diameter of the bag cage is designed to be 134mm, the circle distance is 165mm, the longitudinal diameter is 12, the head part is provided with Venturi blowback pipes and the like, the double corrosion prevention process of carbon steel and KC is adopted, and the bag cage is divided into three sections to facilitate installation, disassembly and cleaning;
(5) the bottom of the dust remover is flat, and the dust is discharged mechanically by adopting a rotary scraper, so that the dust at the bottom is cleaned in real time (mechanically and forcibly discharged).
(6) The dust remover has good sealing performance in the whole structure, is provided with two overhauls , and is fully covered by heat preservation, thereby avoiding the occurrence of local corrosion.
(1) Pulse blowback device:
9.1.4 air bags are arranged on two sides above each cloth bag for storing compressed air, and a pressure transmitter is arranged on each air bag for monitoring the pressure of the compressed air in the air bag. Under normal conditions, the pressure of the bag air bag is kept at about 0.4 Mpa. Each air bag is provided with a pulse injection pipe, and the opening and closing of each injection pipe are controlled by an electromagnetic valve. Each path of injection pipe is responsible for back blowing of the filter bag below the injection pipe. The injection pipe is provided with an injection port above each filter bag and is aligned to the center of each filter bag.
9.1.5 the jet pipe is pulse reverse blowing by time interval through reasonable electric control system, the time interval of reverse blowing can be set by control system, the electromagnetic valve on the jet pipe keeps normally closed, when cleaning ash, the electromagnetic valve opens the pulse valve, the compressed air is pulse blown by ash cleaning control device according to set time interval, the compressed air passes through each pulse valve in order according to extremely short time and induces air which is several times of the jet air volume through the nozzle on the jet pipe to enter the filter bag, forming air wave, making the filter bag generate sharp expansion and impact vibration from the bag mouth to the bottom, causing strong ash cleaning action, blowing off the dust from the back of the filter bag, increasing the effective filtering area and effectively reducing the smoke passing resistance.
9.1.6 the pressure transmitters are arranged on the upper cabin and the lower cabin of the cloth bag, and the pressure difference condition of the cloth bag can be displayed through the pressure difference between the two pressure transmitters. During operation of the filtration system, the maximum pressure differential will remain below 800pa under normal load. If the pressure difference of the cloth bag becomes large, the time interval of back flushing of the cloth bag can be properly shortened, the back flushing frequency is increased, when the pressure difference is within a reasonable range, the back flushing frequency is reduced as much as possible, the quantity of external cold air entering the cloth bag is reduced, the phenomenon that the cloth bag is invalid due to water vapor condensation caused by local low temperature of smoke in the cloth bag is reduced, and meanwhile, the online monitoring data of a smoke discharge port is influenced.
(2) A filtering and dust removing system:
1) the filtering and dust removing system mainly comprises a filter bag and a mesh cage, and the mesh cage is divided into three sections and is connected with a middle part in a buckling mode so as to be convenient to install. The inside of the filter bag is provided with a mesh cage framework which is used for supporting the filter bag and ensuring the effective filtering area of the filter bag.
2) In order to facilitate installation and maintenance, the cloth bag net cage is designed to be installed in sections. The filter bag is fixed on the cloth bag card by a buckle, and the mesh cage is arranged at the inner side of the filter bag and is placed on the cloth bag card.
3) Each filter bag net cage is independent, and when a filter bag or a net cage in a cloth bag is damaged and needs to be replaced, the filter bag net cage can be replaced independently without dismantling the rest filter bag net cages.
(3) A residue collection system:
1) the ash collecting system consists of a cloth bag scraper and a star-shaped discharge valve.
2) The flat design in sack bottom, the lime-ash that is intercepted by the filter bag falls into the sack bottom, is carried to the ash hole by the scraper compulsory, and the star type discharge valve is installed to the ash hole, and scraper and star type discharge valve are normally opened in normal operating, ensure that the lime-ash in the sack in time discharges.
3) When the scraper normally operates, the current is less than or equal to 7.5A, if the current is higher, the discharging at the bottom of the cloth bag is not smooth, the scraper load is increased due to the accumulation of materials at the bottom of the cloth bag, and the scraper needs to be checked in time to remove faults.
4) The ash and slag discharged by the star-shaped discharge valve enters a main chain conveyor through a screw conveyor so as to enter a rotary kiln incineration system.
5) The -grade cloth bag ash slag is mainly dried fine mud, in order to prevent the ash slag at the bottom of the cloth bag from being accumulated, the bottom of the cloth bag is provided with a thermometer, and when the temperature indicated by the thermometer at the bottom of the cloth bag rises, the ash accumulation phenomenon at the bottom of the cloth bag is indicated, whether the scraper, the star-shaped discharge valve and the screw conveyor work normally needs to be checked in time, faults need to be eliminated in time, and the stability of the system is ensured.
(4) An active carbon adding system:
1) the active carbon is stored in the active carbon bin and is conveyed to a flue between the two bag-type dust collectors by the wind power of the wind blower through the active carbon feeding device so as to adsorb harmful substances such as dioxin, heavy metals and the like in the flue gas.
2) The activated carbon is delivered into the warehouse and stored by two modes of pneumatic delivery of an air-pressure delivery type tank car or delivery of a cargo lift and feeding (bagged activated carbon). The capacity of the activated carbon bin should meet the consumption of activated carbon for 1.5 days of normal operation of the incineration line.
3) The active carbon adding device comprises an active carbon storage tank, a feeding device, a material pneumatic conveying device and the like; adjusting the amount of activated carbon supplied to the flue gas according to the amount of the flue gas at the outlet of the chimney; the adding amount of the activated carbon is variable-frequency adjustable;
4) in the system, an activated carbon injection port is arranged on a flue gas pipeline between the two bag-type dust collectors, and the activated carbon injection device injects powdery activated carbon into a flue positioned between the two bag-type dust collectors. The air blower is used as power equipment for injecting active carbon into the flue of the bag-type dust collector.
5) The powder activated carbon passes through the disc feeder and is quantitatively fed into the Venturi injection pipe below the storage bin, the disc feeder is provided with a control panel of the variable-frequency speed regulator, the control panel receives signals of a central control system to automatically adjust the rotating speed of the disc feeder and timely adjust the injection amount of the activated carbon, the active carbon dosage is controlled to be 8-10 kg/h like , and the Venturi injection pipe blows the powder activated carbon into a flue by utilizing high-pressure air generated by an air blower.
9.2 technical design:
(1) the dust remover is mainly composed of a filter chamber, an air purifying chamber, a tangential air inlet, a bottom flat-bottom scraper forced ash discharging device, a low-pressure pulse online ash cleaning device, an electric control device, a valve and other parts;
(2) the dust remover is circular, and a scraper with a flat bottom at the bottom forcibly discharges dust out of the dust hopper in a free flow manner;
(3) the cloth bag is made of PPS + PTFE film. Fully considering the condition of meeting different temperatures of the flue gas under the desulfurization working condition or the fault working condition
(4) Two sets of bag-type dust collectors are designed to be connected in series, a phi 1800 electric cut-off valve (manual operation during power failure) is installed at an inlet, and the filtering wind speed is less than 0.8 m/min;
(5) the bag-type dust collector adopts a circular tangential air inlet mode so as to pre-collect dust by utilizing the cyclone effect, the air inlet is uniformly distributed, and the filtering load of the bag is reduced;
(6) the dust remover body is circular, two overhauls are designed to be , and the dust remover is fully covered by heat preservation.
(7) The pulse valve is made of Shanghai Shangtai brand. The surface coating of the pulse valve is smooth and beautiful, the defects of peeling, bruising, scratching, burrs and the like cannot be caused, and the fastening piece does not have the phenomena of loosening, damage and the like. The ash removal system is reasonable in arrangement, stable and reliable in working performance and capable of completing ash removal work according to requirements; the action of the pulse valve is sensitive and reliable; the ash removal system should have sufficient gas storage capacity;
(8) the escalator operation platform can reach the operation surface needing to be overhauled and operated on each layer;
(9) the ash discharging mode of the dust remover is that the bottom scraper forcibly discharges ash, so that the accumulation of the dust is effectively controlled;
(10) the upper side of a scraper at the bottom of the dust remover is provided with a temperature monitor, and if the temperature is higher than the temperature of flue gas, the ash discharge abnormity is alarmed; monitoring the current of the scraper speed reducing motor, and if the current is higher than a normal operation value, alarming the abnormal ash discharge;
(11) the filter bag automatically removes dust by adopting a pulse injection mode.
10. Wet desulfurization and denitrification system:
10.1 System:
10.1.1 wet denitration system mainly comprises spraying system, liquid caustic soda dosing system, ozone denitration system and cooling system.
(1) A spraying system:
1) the spray system is provided with three spray towers, each spray tower is provided with two layers of spray, each layer of spray is provided with 8 spray nozzles and two centrifugal pumps, each centrifugal pump is provided with spray nozzles, a pressure transmitter is arranged on each stage of spray water supply pipe and used for monitoring the spray condition in normal operation, the centrifugal pumps extract spray liquid on the lower part of the spray towers, the spray liquid enters the spray towers through a spray header pipe and is conveyed to the spray layers through 8 uniformly distributed spray nozzles, the spray nozzles adopt spiral spray heads, the spray liquid is refined in the spray towers after passing through the spiral spray heads, the spray nozzles are convenient to maintain and replace, the spray nozzles are designed into a drawing and inserting type, when the spray heads need to be replaced, the centrifugal pumps for spraying are firstly closed, and the spray heads are re-opened after being.
2) In order to improve the spraying effect and ensure that the flue gas is fully contacted with the spraying liquid, pall ring packing layers are arranged below two layers of spraying of the two-stage and three-stage spraying towers, the spraying liquid after the preliminary reaction with the flue gas is sprayed on the pall rings, and the flue gas and the spraying liquid continue to be in contact reaction under a larger comparison area, so that the spraying effect is improved.
3) The space at the lower part of the spray tower is used as a spray liquid buffer tank, and the spray liquid is recycled.
4) level spraying and secondary and tertiary spraying have different functions, alkaline liquor is added into a level spraying tower to treat acid gas, an ozone uniform distribution pipeline is arranged between two layers of spraying of a level spraying tower, ozone denitration and deodorization are added, the rear two level spraying tower washes the flue gas sprayed by level, acid gas and trace dust in the flue gas are removed in steps, the flue gas is ensured to be discharged up to the standard, in order to ensure the deacidification effect and facilitate the tail gas to be discharged up to the standard when maintenance is carried out under the operation state, an alkaline liquor adding port is prepared in the rear two level spraying, and when the level spraying deacidification effect is insufficient or maintenance is required, deacidification is carried out by the rear two level spraying.
(2) Liquid caustic soda feeding system:
1) the method comprises the following steps of conveying 30% liquid caustic soda into a workshop through a vehicle, connecting the liquid caustic soda with an alkali inlet pump through a connector, and conveying the liquid caustic soda into a liquid caustic soda tank through the alkali inlet pump, wherein the liquid caustic soda tank is provided with a liquid level meter, the liquid caustic soda amount in the liquid caustic soda tank is monitored through the liquid level meter, the liquid caustic soda is added in time, an inlet of the liquid caustic soda pump is independently arranged, pump outlets are combined into main pipes to be led to a spray tower, and the main pipes are provided with a pressure transmitter and a flowmeter for monitoring the liquid caustic soda adding.
2) The adding amount of the liquid caustic soda is controlled by a PH meter on an -grade spray tower, in order to ensure the desulfurization effect of the liquid caustic soda, the PH value of a -grade spray tower is controlled between 8 and 9, and the final grade is about 7.
(3) Ozone deNOx systems:
1) the denitration system can simultaneously remove pollutants such as NOx, sulfur dioxide, particulate matters and the like in flue gas at high efficiency under different concentrations and proportions of pollutants such as NOx and the like, is more efficient and better in controllability than the traditional denitration method, and is efficient alternative technologies of the traditional denitration technology.
2) The ozone denitration technology is added between a bag-type dust collector and a fan, the reaction time is not less than 1-1.5S, the flue gas temperature is about 100 ℃, and the operation cost of the ozone denitration is only the power consumption of the ozone equipment and the consumption of a small amount of liquid oxygen.
3) According to the principle of economic operation of system equipment, a 5kg/h ozone generator selects a rated ozone concentration of 148mg/L, and a liquid oxygen tank of an air source system supplies oxygen. The output adjusting range of the ozone generator can realize linear adjustment, the adjustment and the like can be realized by adopting a mode of simultaneously adjusting power and air quantity, and the cooling adopts a plate heat exchanger mode for cooling circulation and the like. The system adopts a PLC control mode and the like.
4) Oxygen enters the ozone generator. The air inlet pipeline of the ozone generator is provided with a pressure reducing valve for stabilizing the working pressure of the ozone generating chamber. Oxygen inside the ozone generating chamber is changed into ozone through medium-frequency high-voltage discharge, and product gas is output from an ozone gas outlet after temperature, pressure and flow monitoring and regulation. The ozone generating chamber is provided with an ozone gas taking port, and the ozone concentration detector arranged on the ozone generator is used for monitoring the gas outlet concentration of the ozone generator on line.
5) The ozone generating system is provided with closed-loop circulating cooling water systems, which exchange heat through a plate heat exchanger and provide cooling water for the ozone generator, the closed-loop circulating cooling water system comprises a plate heat exchanger, a circulating water pump, an expansion tank, a valve and the like, a flow switch and a temperature transmitter are arranged on a cooling water outlet pipeline of the ozone generator, and an alarm is given when the flow rate of cooling water is insufficient and the temperature exceeds a set value.
6) An ozone/oxygen leakage alarm instrument is installed in the ozone preparation room, and when the ozone/oxygen leakage in the environment in the preparation room exceeds the standard, the system determines to output an alarm, start an exhaust fan or stop the machine according to a detection signal.
7) In order to remove nitrogen oxides in the flue gas, ozone is added between the back of the bag-type dust collector and the main fan to remove organic odor in the flue gas and fully react with the NOx in the flue gas, so that the aim of denitration is fulfilled.
8) Along with the continuous supplement of the circulating spray liquid, the circulating spray liquid with higher temperature in the spray tower is continuously replaced, so that the temperature and the salinity of the circulating spray liquid in the spray tower reach dynamic balances.
9) The th spray tower is separately provided with a fresh water supplement port with DN50 pipe diameter, and fresh cooling water is used for supplement, thereby ensuring the quality of spray circulating liquid in the spray tower under special conditions.
10.2 principle:
(1) denitration:
before the cloth bag flue gas enters the absorption tower, strong oxidant (ozone) generated by an ozone generation system is adopted to forcibly oxidize NOx in the flue gas, so that the NOx is converted into high-valence nitrogen oxide (N2O5) which is easily dissolved in water, and the oxidized high-valence nitrogen oxide enters the absorption tower along with the flue gas. In the absorption tower, the nitric acid is dissolved in water to produce nitric acid, and the nitric acid and the sodium hydroxide water solution in the circulating slurry in the absorption tower are subjected to neutralization reaction to generate sodium nitrate.
(2) And (3) desulfurization:
the slurry circulating pump sends the circulating slurry at the bottom of the tower to the absorption section spraying layer, and the slurry is used for absorbing sulfur dioxide and nitrogen oxide in the flue gas.
(3) System raw material medium supply:
the method comprises the steps of supplying an absorbent, wherein a flue gas dedusting, desulfurization and denitrification system adopts 30% by weight of sodium hydroxide aqueous solution as a desulfurization absorbent, sending the 30% by weight of sodium hydroxide aqueous solution outside a boundary area to a flue gas dedusting, desulfurization and denitrification facility, and carrying out acid-base neutralization reactions in the process of absorbing sulfur dioxide and nitric oxide in flue gas by using the 30% by weight of sodium hydroxide aqueous solution, wherein the 30% by weight of sodium hydroxide aqueous solution is continuously supplemented into the slurry of an absorption tower in order to keep the pH value of circulating slurry in the absorption tower to meet the requirement of absorbing sulfur dioxide and nitric oxide in the flue gas.
10.3 technical requirements:
(1) the flue gas pipeline from the cloth bag to the spray tower is 2205, , and the connecting pipeline of the second spray tower and the third spray tower is FRP.
(2) The tower body is made of: the material of the cylindrical high-temperature-resistant resin glass fiber wound pipe fitting is FRP;
(3) the water pump adopts mechanical seal and steel lining plastic
(4) Valve is made of steel-lined PE;
10.4 SNCR denitration technique:
the project can adopt SNCR technology process to denitrate due to the limited use of ozone. Sludge materialThe original concentration value of the nitrogen oxides in the flue gas is 300mg/m by analyzing and referring to detection data of other items of my department3. The SNCR denitration adopts urea as a reducing agent. 36000Nm according to smoke amount3And calculating the consumption amount of the urea as 10kg/h, diluting and spraying according to 10% of urea solution, wherein the pumping amount of the urea solution is 100 kg/h.
The SNCR denitration adopts an optimized process, and multi-point injection is carried out in a high-temperature section (above 850 ℃) of a secondary combustion chamber. And respectively arranging corresponding nozzles according to the temperature in the furnace, and accurately spraying. And respectively spraying 10% urea solution into the two combustion chambers according to the quantity of the nozzles and the temperature proportion, reducing nitrogen oxides in the flue gas into harmless nitrogen and water, and calculating the denitration efficiency according to 80%.
The SNCR denitration principle is that reducing agents such as ammonia water and urea are sprayed into an area with the temperature of 850-1100 ℃, and the reducing agents are rapidly thermally decomposed into NH3And with NO in the flue gasXReaction is carried out to generate N2And H2And O. The SNCR process reactor is the high temperature zone of an incinerator.
The reaction formula is as follows: 2NO + CO (NH)3)2+1/2O2→2N2+CO2+2H2O
Based on the original NOx content of 95%, the NO discharge capacity is 10.3kg/h, the high-valence nitrogen oxides are 0.5kg/h, and the high-valence nitrogen oxides can be removed in the subsequent deacidification process. 80% NO can be removed in the SNCR process, the urea consumption is 10.3kg/h considering the urea loss rate of 20%, and the urea solution dosage is about 100kg/h when the urea solution is prepared into 10% urea solution. Adopts multi-point injection, uniform feeding and atomized injection to achieve the best contact effect to enable NO to be sprayedXThe outlet concentration reaches and is superior to the requirement of European Union standard.
The method comprises the following steps of preparing main equipment:
1. a urea preparation tank: 1 stage, material SUS304, volume 3m3
2. A urea dilution tank: 1 stage, material SUS304, capacity 5m3
3.2 jet pumps, model G10 diaphragm pump prepared from spare pumps and with rated flow rate of 1m3H, flow rate regulation by frequency conversion, rated pressure 7.0MPaAnd the power is 4 KW.
11. White removal system and chimney system:
11.1 System description:
11.1.1 the de-whitening system is mainly composed of stainless steel heat exchanger and environmental air blower.
11.1.2 the system is provided with a stainless steel heat exchanger which separates the flue gas from the ambient air by a specially made metal heat exchange plate.
11.1.3 the saturated flue gas desulfurized by the wet method passes through the metal plate heat exchanger from top to bottom, the ambient air fan extracts ambient air, the ambient air enters the heat exchanger from the side edge of the metal plate heat exchanger, the flue gas and ambient dry air carry out gas-gas indirect heat exchange through the metal heat exchange plate from bottom to top, the temperature is reduced, a large amount of moisture is condensed out to reduce the humidity of the flue gas, and the whitening effect in the stage is achieved.
11.1.4 technological principle: the saturated flue gas which is desulfurized by the wet method passes through the HINO-PILE plate heat exchanger from bottom to top, performing gas-gas indirect heat exchange with ambient dry air, condensing out a large amount of water, wherein the condensed water accounts for 15-30% of the total water in the flue gas, meanwhile, a large amount of heat energy is released when the moisture of the tail gas is condensed to heat the ambient dry air blown into the heat exchanger so as to increase the temperature of the ambient dry air, then the heated dry air is introduced into a chimney by an air pipe to be mixed with the flue gas after temperature reduction and dehydration, so that the humidity of the mixed flue gas is greatly reduced, therefore, the dew point temperature of the exhausted flue gas is reduced, the temperature difference between the temperature (T) of the flue gas at the main exhaust port and the saturation temperature (T') under the humidity condition is more than or equal to 10 ℃, the exhausted flue gas can not reach the dew point temperature in a short time after being exhausted, and the moisture in the flue gas can not be condensed into water mist, so that the aim of reducing the white smoke is achieved.
11.1.5 the environmental wind fan of device disposition adopts inverter motor to carry out the frequency conversion regulation and control, and the amount of wind of fan is the device full load amount of wind, and along with the change of weather, the temperature of ambient air and atmospheric humidity all can change, can take off white visual effect according to the change and the flue gas of these external factors during the use, through the height of artificial regulation frequency conversion power to reach the best visual effect of taking off white.
11.1.6 chimney is provided with interior outer tube, separates each other between the interior outer tube, installs online monitoring system above the interior section of thick bamboo, and the steel platform that sets up through the chimney outside makes things convenient for online monitoring's maintenance and maintenance.
11.1.7 the flue gas after heat exchange enters the inner cylinder of the chimney, and the environmental wind enters the outer cylinder of the chimney, so that the flue gas entering the inner cylinder can be monitored in real time by on-line monitoring, and the influence of the environmental wind is avoided.
11.1.8 the dry air after temperature rise is mixed with the flue gas after temperature reduction and dehydration at the outlet of the inner cylinder, thus greatly reducing the humidity of the mixed flue gas, reducing the dew point temperature of the exhausted flue gas, ensuring that the exhausted flue gas can not reach the dew point temperature in a short time after being exhausted, and the moisture in the flue gas can not be condensed into water mist, thereby achieving the purpose of reducing the white smoke.
11.1.9 the environmental wind fan of device disposition adopts inverter motor to carry out the frequency conversion regulation and control, and the amount of wind of fan is the device full load amount of wind, and along with the change of weather, the temperature of ambient air and atmospheric humidity all can change, can take off white visual effect according to the change and the flue gas of these external factors during the use, through the height of artificial regulation frequency conversion power to reach the best visual effect of taking off white.
Therefore, the operation method of the kinds of industrial solid waste and sludge rotary kiln cooperative treatment integrated device provided by the invention further protects the environment in steps and improves the comprehensive utilization rate of the solid waste.
Detailed Description
The technical solution of the present invention is further specifically described in by examples.
The embodiment discloses an operation method of an type industrial solid waste and sludge rotary kiln cooperative treatment integrated device, which comprises the following steps:
(), structural composition:
the system comprises a sludge receiving system, a sludge spray drying or disc drying system, a sludge incineration system, a flue gas treatment system, a wind power slag suction system and an incineration slag ash collecting system;
the sludge receiving system, the sludge spray drying or disc drying system, the sludge incineration system, the flue gas treatment system, the wind power slag suction system and the incineration slag ash collecting system are sequentially connected;
(II) a sludge feeding system:
sludge reception takes place through two pathways:
the method comprises pouring sludge with water content of 70-80% into underground receiving system, lifting with shaftless auger, feeding into large sludge storage tank with screw pump via filter, feeding into high-position mud tank with plunger pump, lifting with screw pump, feeding into spray drying tower, pumping into high-position mud tank with plunger pump via mud filter;
the method also comprises steps of loading engineering sludge into a field, pouring the engineering sludge into a sludge receiving tank, arranging two shaftless packing augers in the sludge receiving tank, lifting the sludge to a screw pump on the side of the sludge receiving tank by using the shaftless packing augers, lifting the sludge to two sludge receiving tanks by the two screw pumps respectively, arranging two plunger pumps with hydraulic stations on the periphery of the sludge receiving tanks, preparing plunger pumps , lifting the sludge in the sludge receiving tanks to a high-level sludge storage tank in a factory by using the plunger pumps, arranging sludge filters on pipelines, screening large particles in the sludge in a step, and providing the high-level sludge storage tank with feed sludge for a drying tower;
four DN400 pipelines are arranged below the high-level sludge storage tank and are controlled by a manual valve , the sludge falls into 4 screw pump receiving ports respectively, the lifted sludge is sent into the spray drying tower and atomized by a nozzle at the top of the tower, the compressed air is sent to the top of the tower by an air compressor room main pipe and is divided into 4 strands at the atomizing nozzle, and a pressure transmitter is arranged on an air pipe and is connected with a control room computer for adjusting the amount of compressed air entering the tower so as to achieve the optimal atomization effect;
(III) a sludge drying system:
the high-temperature flue gas entering the top of the spray drying tower is output from the high-temperature flue gas at the outlet of the waste heat boiler;
the sludge is dried by spray drying or super disc drying, and is obtained or the two are used in combination;
the spray drying is to disperse the dewatered sludge with the water content of about 80 percent into fine particles like fog by the action of an atomizer, contact the fine particles with the high-temperature flue gas for burning, remove most of water instantly and dry solid substances in the materials;
the atomized sludge is directly dried by burning high-temperature flue gas, so that the heat loss of a complex heat exchanger is avoided, the heat utilization efficiency can be improved to more than 80 percent, and the atomized sludge is effectively atomized and dried quickly;
through the effective atomization of the sludge, the problems of blockage and abrasion are avoided, and the dried sludge particles are uniform and reasonably distributed, so that the sludge is favorable for incineration;
the spray drying system adopts a novel special two-fluid atomized sludge system, and the atomized sludge system is left together with the high-temperature flue gas, and the tower diameter and the tower height are adjusted by optimizing the structure of the drying system according to the characteristics of the sludge and the contact condition of the atomized sludge and the high-temperature flue gas, so that the phenomenon of sludge wall adhesion is avoided;
the super-disc dryer adopts a steam indirect heat exchange mode, water is evaporated more quickly by stirring materials, and the dryer is suitable for semi-drying and full-drying of the materials;
(III) a sludge incineration system:
dried sludge with the water content of 20-30% is respectively sent into a rotary kiln for incineration through a stokehole feeding screw, industrial solid waste is combusted in a hot air furnace, and flue gas directly enters an incinerator through the hot air furnace to be incinerated together with the sludge;
the leftover materials with the thickness determined by in the hot blast stove are burnt in a hearth to generate high-temperature smoke and enter a sludge burning system, the temperature of the hot blast stove can be controlled according to process requirements, burned-out slag is discharged from the other end of the chain grate to a slag discharging machine and is sent out by an automatic slag discharging machine, the burning hearth is built by high-temperature resistant refractory materials, and the whole burning system is electrically controlled;
the sludge incineration system adopts a rotary incinerator-rotary kiln, a hot blast stove is integrated to the kiln head of the rotary kiln, high-temperature flue gas generated by combustion of the hot blast stove is mixed with flue gas generated by combustion of dried sludge in the rotary kiln, carbon particles/dust and high-temperature coal gas brought by flue gas enter a secondary combustion chamber for sufficient combustion and polymerization and sedimentation, high-temperature hot flue gas after secondary incineration enters a waste heat boiler, the temperature of the high-temperature hot flue gas is 750-1000 ℃, waste heat is recovered by the waste heat boiler, the high-temperature hot flue gas enters a drying tower to serve as a drying heat source of wet sludge, and finally the waste flue gas enters a tail gas treatment system;
(IV) a dried sludge ignition flame system:
the dried sludge ignition flame system adopts a natural gas burner, and the equipment is characterized by complete combustion and no black smoke; the hot blast stove generates 500-1000 ℃ flame, the dried sludge is heated to the ignition temperature of 300 ℃ and is made to spontaneously combust, and combustion-supporting air is fed by a high-pressure fan through a pipeline;
the heat of natural gas has a value of 8500kcal/m3The specification of the hot blast stove is 600 ten thousand kilocalories per hour;
(V) burning the rotary kiln:
the dried sludge after spray drying is sent into a sludge incinerator for incineration through a chain conveyor and an inclined feeding pipe; the dried sludge after the disc drying is sent into a rotary kiln for incineration through sludge conveying equipment;
adopting a horizontal rotary incinerator; the rotary incinerator is characterized in that high-temperature air from a hot blast stove is blown into the incinerator from a furnace end, so that the temperature of dried sludge is quickly raised and dried continuously, the dried sludge is completely combusted at the high temperature of 900 ℃, high-temperature flue gas generated by combustion is introduced into a secondary combustion chamber, then the high-temperature flue gas is distributed with air through cold air and enters a drying tower to serve as a drying heat source of wet sludge, and finally waste flue gas enters a tail gas treatment system;
the dried sludge is fed into an inclined pipe through a dried sludge chain conveyor and then slides into the rotary kiln, and the dried sludge rotates from a high end to a low end in the rotary kiln; after sliding into the rotary kiln, the sludge is ignited when walking for 3-4 m, is burnt out when walking for 21m, falls into a slag discharging hopper after being burnt out, and is conveyed to a slag suction system through a sludge adjusting cylinder;
the diameter of the rotary kiln is 3.7m, the length of the rotary drum is 21m, and the inclination is 1-1; 5 ℃, the rotating speed is 1-2 r/min, and the residence time of the sludge in the kiln is adjustable within 20-60 min;
the air inlet of the rotary kiln is divided into two paths, paths of hot blast stoves supply heat flame, the temperature is 500-1000 ℃, paths of ambient air for adjusting the oxygen content in the kiln, and the exhaust temperature of the rotary kiln is above 850 ℃;
(VI) a second combustion chamber:
in order to ensure that harmful gas is burnt out and reaches the emission standard, the gas burned in the rotary kiln enters a secondary combustion chamber; the secondary combustion chamber adopts a vertical structure, the thickness of a heat-insulating wall body is 0.58m, so that the temperature of the secondary combustion chamber is not lower than 850 ℃, and the gas flowing time is not less than 2.5 seconds so as to decompose and control the generation of dioxin;
(VII) a flue gas treatment system:
seventhly, 1, flue gas treatment and purification process:
the waste gas treatment process of a cyclone dust collector, a two-stage bag dust collector, activated carbon adsorption, ozone denitration and deodorization, three-stage spray tower washing, whitening and demisting is adopted;
seventhly, 2, white smoke reduction flow:
the method comprises the steps of selecting a Japanese HINO-TEC technical device, mainly utilizing gas-gas heat exchange, enabling smoke to enter a white smoke reduction device through a dehydration spray tower, cooling the smoke through a HINO-PILE plate heat exchanger, condensing a large amount of moisture, simultaneously utilizing a large amount of heat energy released during moisture condensation to heat ambient dry air, mixing the heated dry air with the smoke subjected to cooling and dehydration, greatly reducing the absolute humidity of the mixed smoke, reducing the dew point temperature of the evacuated smoke, enabling the evacuated smoke to not reach the dew point temperature in a short time after being exhausted, and further achieving the purpose of reducing the white smoke;
seventhly, 3, a heating and ventilating system:
the heat supply system comprises a hot blast stove, an air inducing device and a flue gas pipeline, wherein the air inducing device comprises two parts, the part introduces air to the hot blast stove to be used as combustion-supporting air, and the air is burnt and preheated by the hot blast stove and then sent into the rotary incinerator, the second part introduces flue gas discharged by the sludge incinerator into the sludge drying system, the heat source of the drying system mainly comes from 650 ℃ waste heat flue gas which is discharged by the sludge incinerator and has the temperature of over 850 ℃ and is formed by air distribution of cold air, and the heat source enters the top of the spray drying tower after being distributed by a corresponding hot air distribution system, namely, the downstream direct heating mode adopted by the drying process of the project;
seventhly, 4, a flue gas purification system:
designing the dry gas quantity of about 3.1 ten thousand square standard for subsequent flue gas treatment matched projects, wherein the flue gas temperature is 110 +/-10 ℃;
(eighth), cyclone system:
eight.1 system description:
the cyclone dust collector is used as a middle channel of the drying tower and the tail gas treatment system, and makes the dust-containing airflow rotate, separates dust particles from the airflow by means of centrifugal force and collects the dust particles on the wall of the drying tower and makes the dust particles fall into the dust hopper by means of gravity;
(nine), bag dust removal system:
the bag-type dust collector adopts a circular design, and tangentially enters air without dead angles;
(ten) a wet desulfurization and denitrification system:
the wet denitration system mainly comprises a spraying system, a liquid caustic soda feeding system, an ozone denitration system and a cooling system;
(ten ), a whitening system, and a chimney system:
the de-whitening system mainly comprises a stainless steel heat exchanger and an environmental air fan.
Preferably, the sludge feeding system in the step (II):
two sludge receiving ways are provided with two control modes, namely a manual control mode and an electric control mode:
sludge receiving tankThe effective depth of the sludge receiving pool is 4.5m, a sealed room adopting a brick-concrete structure is built above the sludge receiving pool, and the floor area is 70m2(ii) a A filter screen is arranged above the receiving tank to screen out large impurities in the sludge;
air pumping ports are respectively arranged above the sludge receiving pool and at the top of the sludge low-level storage tank, and odor in the bin is pumped as combustion-supporting air of the sludge incinerator, so that a storage pit area forms negative pressure to prevent odor from overflowing; the extracted air is sent into a hearth for incineration, and the malodorous substances in the air are decomposed and oxidized in the combustion process;
the sludge receiving tank is provided with two sludge receiving tanks, the height of each sludge receiving tank is 18m, the radius of each sludge receiving tank is 10.5m, and the storage capacity of each sludge receiving tank is 1500m3The capacity of the high-level sludge storage tank is about 100m3
The pipelines before sludge atomization are respectively provided with a tower top flowmeter; each tower is provided with 4 atomizing nozzles, and the consumption of compressed air at each nozzle is 7m3Min, pressure 0.45 mPa;
wherein the sludge drying system in the step (II):
the drying tower of the engineering has the diameter phi of 10m to 15m, the effective height of the drying process is 25m, each tower is provided with 4 to 10 atomizing nozzles, and the spraying angle of the nozzles is adjustable between 50 and 80 ℃; the amount of compressed air at each nozzle is 7m3Min, pressure 0.45Mpa, sludge treatment capacity of each nozzle 4m3/h;
Auxiliary equipment, an atomization system and an air distribution system are arranged in the drying tower, the atomization system is used for forming the sludge into granular droplets with the particle size of 30-500 mu m, and the sludge is naturally granulated after drying; the air distribution system has the function of enabling air distribution in the drying system to be uniform, so that the sludge is more effectively dried, and the heat utilization efficiency is improved; the air quantity source of the air distribution system is high-temperature flue gas generated by the incineration system; the compressed air is conveyed to the top of the tower through a header pipe and is divided into 4 strands at an atomizing nozzle, and a pressure transmitter is arranged on an air pipe and is connected with a control room computer for adjusting the air consumption;
the temperature of the high-temperature flue gas entering the top of the spray drying tower is 550 ℃, the pressure is-500 Pa, and the high-temperature flue gas is output from the outlet of the waste heat boiler; an air supplementing system and a main air valve are arranged on the tower inlet flue gas pipeline and used for adjusting the air quantity: a thermocouple is arranged on the high-temperature flue gas pipeline to measure the temperature, a thermocouple and a pressure transmitter are arranged on the mixed flue gas pipeline, all temperature and pressure monitoring is connected with a computer in a control room, the temperature and pressure changes are monitored in time, the opening degree of a cold air valve and a main air valve is adjusted, cold air comes from the treated gas of an inner chimney, and the gas taking has the advantages of energy conservation and low oxygen content; the sludge outlet temperature of the drying tower is 50-60 ℃, and the water content of the sludge is about 20%;
the drying tower is made of heat-resistant stainless steel SUS310S and 2205, the heat-insulating material is an aluminum silicate fiberboard, the heat-insulating material is determined according to different temperature zones, the maximum thickness of the heat-insulating thickness is 250mm, the minimum thickness is 100mm, and the heat-insulating material is externally provided with a 304 stainless steel outer skin; because the volatile gas quantity generated in the drying process and the dust concentration in the tower are both very low and are far lower than the explosion limit of the combustible gas and dust concentration, the control of the drying tower on the oxygen content is not considered in the design, and the water content of the sludge with the water content of 80 percent is reduced to 20 percent after drying;
the spray drying is to disperse the dewatered sludge with the water content of about 80 percent into fine particles like fog through the action of an atomizer, increase the heat transfer surface area, accelerate the drying, contact with the incineration high-temperature flue gas, instantly remove most of water, and dry the solid matters in the materials, wherein the drying process is rapid, the heat utilization rate is high, the incineration high-temperature flue gas is used for directly drying the atomized sludge, the heat loss of a complex heat exchanger is avoided, the heat utilization efficiency can be improved to more than 80 percent, the effective atomization and the drying are rapid, the problems of blockage and abrasion are avoided through the effective atomization of the sludge, the dried sludge particles are uniform and reasonably distributed, the particle mesh degree is 60-120 meshes, the incineration is facilitated, the spray drying tower is safe and stable, the drying degree of the sludge particles is regulated and controlled, the safety and the dust explosion are ensured, the flue gas temperature is rapidly reduced from 550 ℃ to below 200 ℃, the cooling time is less than 1.5s, the regeneration of dioxin and the precursors of the dioxin can be prevented, the drying process is extremely less volatile organic gas can be absorbed in the atomized in the sludge, the subsequent spray drying tower, and the subsequent flue gas drying treatment load and the subsequent flue gas purification facility;
the main body of the dryer consists of cylindrical shells, hollow shafts and groups of hollow disks welded on the shafts, a heat medium flows through the hollow disks and indirectly transmits heat to sludge through the disks, the sludge passes between the super disks and the shells and receives the heat transmitted by the super disks to evaporate water, and the generated water vapor is gathered in a dome above the super disks and is taken out of the dryer by a small amount of ventilation;
wherein in the step (III), the sludge incineration system:
the rotary kiln comprises a kiln head, a kiln body, a kiln tail and related mechanisms of a transmission mechanism, wherein the kiln head is mainly used for smoothly feeding materials, arranging sets of multifunctional burners and conveying combustion air, sealing the rotary kiln and the kiln head, the kiln head sealing device of the incinerator is sealed by a traction rope sealing system by adopting a composite graphite block, and has good sealing effect, a kiln face cover of the rotary kiln is protected by refractory materials, waste collectors are arranged at the lower part of the kiln face cover for collecting waste leakage, the rotary kiln body is cylinders rolled by a steel plate, the inclination of the cylinder is 2.5% for ensuring that the materials are conveyed downwards, supporting and transmission parts are reinforced by a 50mm steel plate, the outer surface of the rotary kiln body is coated with high-temperature resistant paint and resists the temperature of 500 ℃, two belt wheels and gear rings are arranged on the rotary kiln body, the transmission mechanism drives a large gear ring on the rotary kiln body through a pinion, then drives the rotary kiln body to rotate through the large gear ring, the rotary kiln tail is a transition body connected with the rotary kiln body and the rotary kiln body, the rotary kiln body and the rotary kiln tail is a transition body, and a kiln which is a flue gas-fired air regulating valve which is used for ensuring that the rotary kiln is used for controlling the combustion of a secondary air-fired kiln, and a secondary air-fired furnace-fired-air-fired-operated automatic air-fired-operated secondary-operated auxiliary-operated air-operated auxiliary-;
1, the incineration system comprises:
the sludge incineration system consists of the following main devices:
a rotary incinerator: the incinerator body, the gear transmission mechanism, the refractory lining and the air distribution device;
hot blast stove: the hot blast stove comprises a hot blast stove body, a feeding system, a slag discharging system and an air distribution system;
ignition and auxiliary combustion equipment: the ignition combustor, the ignition combustor fan and the spiral slag conveyor;
a second combustion chamber: a second combustion chamber body and a refractory lining;
a combustion air system: comprises a blower;
① rotary incinerator, which is the most important part of incinerator, where all the incineration reactions determining the discharge result occur, the incinerator is composed of sludge distributor and hearth, the sludge distributor is used to make air contact with sludge to the maximum in the incinerator load range, the sludge distributor adopts bar grid structure to divide the sludge into small flows to generate good sludge flow distribution, making the sludge flow contact with high temperature air to the maximum, burning fast and making the solid in the incinerator flow to the slag outlet, the sludge distributor should have the characteristics of heat resistance, high temperature gas corrosion resistance, simple structure, easy maintenance and small abrasion;
② incinerator furnace hearth is heat insulation furnace hearth, inner wall is wear resistant and high temperature resistant material, fire resistant layer is outside heat insulation material, the most outside layer is steel welding cylinder to ensure furnace hearth sealing, start burner, secondary air nozzle, necessary measuring instrument are installed at incinerator head, and explosion proof is reserved on incinerator smoke outlet pipeline, fire resistant and heat insulation material ensures room temperature state, outer wall temperature of incinerator is not higher than 50 deg.C;
③ ignition and auxiliary combustion equipment, wherein the incinerator is equipped with ignition burner, diesel oil is used for combustion supporting, when the incinerator is started, the ignition burner is needed to raise the incinerator temperature to 850 ℃, sludge is started to be thrown in, and when the incinerator is normally operated, the oil supply amount is adjusted or the incinerator is quitted from operating according to the change of the heat value and the solid content of the sludge;
④ air burning system, wherein the air quantity required by sludge burning is times air and secondary air, times air is supplied by auxiliary burner, the high temperature air from burner is distributed uniformly on the cross section of the whole hearth, and contacts with small mud flow fully to the utmost extent, quickly dries the residual water in sludge and raises the temperature of sludge, and the secondary air enters air through air pipe mounted on the furnace end to supplement the air required by sludge complete burning, and forms strong turbulence in the suspension burning space, to maintain the best burning condition and control the formation of CO and NO X;
⑤ slag storage and conveying equipment, wherein the slag of the incinerator flows from a furnace end to a furnace tail end along with the rotation of the incinerator, is cooled by water spraying, and is conveyed to a slag tank through a pneumatic conveying system, and if the slag generated in the incineration process is identified as -shaped solid waste, the slag is temporarily stored in the slag tank and then is conveyed to a brick factory for making bricks or a nearby cement factory for producing cement or bricks;
thirdly, 2, technical parameters of the rotary incinerator are as follows:
analyzing according to material sources, mixing and matching the sludge entering the rotary kiln with municipal and industrial sludge, calculating according to the water content of the sludge entering the kiln as 20%, and taking the converted heat value of the sludge as 8.9MJ/kg as a design basis;
the incinerator can ensure that the sludge is completely incinerated, the temperature of the flue gas in the hearth is above 650 ℃, the temperature is above 850 ℃ after the flue gas enters the second combustion chamber, and the retention time is not less than 2.5 seconds;
size: outer diameter/inner diameter phi 3700/phi 3000, and length L of 21.5 m;
designing the amount of dry sludge in a single furnace: 5208 kg/h;
rotating speed: 0.2-2 rp/min;
inclination: 2.5 percent;
designing the solid content of the sludge in the furnace: 80 percent;
ash scorching and reducing rate: < 5%;
incinerator load variation range: 70% -110%;
wherein the dried sludge ignition flame system in the step (IV):
fan parameters: the air quantity is 8306m3/h, the full pressure is 11377pa, and the power is 45 kw;
when the natural gas is used as a standby auxiliary fuel and is used for unstable leftover material supply, the natural gas adopts a low-nitrogen combustion technology, and the adopted combustor is a combustor based on the low-nitrogen combustion technology;
fourthly, 1 composition of the incineration system:
the sludge incineration system consists of the following main devices:
a rotary incinerator: the incinerator comprises an incinerator body, a gear transmission mechanism, a refractory lining and a sludge distributing device;
ignition and auxiliary combustion equipment: an ignition burner, an ignition burner fan;
a combustion air system: comprises a blower;
wherein, in the step (six), the second combustion chamber:
when the sludge heat value is low and the burning calorific value is insufficient, so that the temperature of a secondary combustion chamber cannot reach 850 ℃, a 300 ten thousand kilocalories per hour natural gas combustion system is arranged at the bottom side of the secondary combustion chamber, a combustion-supporting fan is used for supplying heat at 4328m3/h, the full pressure 10770pa and the power 22kw, so as to supplement heat at the time of insufficient temperature, a 3T technology is adopted to inhibit the generation of dioxin-like substances, gas generated by volatilization and pyrolysis in the burning process forms high-temperature rotary backflow-shaped flame at the temperature of more than 850 ℃ in the burning furnace, the retention time of flue gas in a high-temperature area is more than or equal to 2s, the thorough burning of organic matters and pyrolysis gas is realized, the generation of dioxin is avoided from the source, the dioxin and heavy metals in the flue gas are removed, the emission index of dioxin and heavy metal related substances in the flue gas is ensured to reach the requirement, an auxiliary purification measure for activated carbon injection is added in the flue gas purification system, the activated carbon is pan applied adsorbent, the adsorbed large specific surface area of the activated carbon is mainly depended on the large specific surface area of the activated carbon, the same mass of the activated carbon, and the mixed turbulent flow of the flue gas can reach 10000, and the purification efficiency is enough to be purified by the;
sixth, 1 waste heat recovery system:
after the flue gas is fully combusted in the front-end rotary kiln and the secondary combustion chamber, the temperature of the flue gas is higher than 850 ℃, a waste heat boiler is arranged at the top of the secondary combustion chamber, the flue gas enters the waste heat boiler for waste heat recovery, and the exhaust temperature of the waste heat boiler is 550 ℃; the design and the construction of the waste heat boiler consider high utilization rate and long-term continuous operation, and fully consider high-temperature corrosion of the flue gas; the high-temperature area of the waste heat boiler adopts a membrane wall radiation heating mode, the temperature of the high-temperature area of the waste heat boiler is 850-500 ℃, and a flue inlet of the waste heat boiler is not allowed to be provided with a heat exchange pipe for directly blowing flue gas, so that high-temperature corrosion is avoided;
in order to fully recover the combustion waste heat, a boiler matched with the incinerator is arranged and used as a heat source for drying the disc, and the waste heat is recovered to the maximum extent on the premise of realizing sludge reduction; the steam of most steam is connected into a disc dryer as a heating medium, a steam collecting box is arranged in an indirect sludge heating and steam heating system and used for distributing steam used in each process, and safety valves are respectively arranged on the steam collecting box and a boiler drum; an emergency waterproof pipe is arranged on a steam drum of the waste heat boiler; the control of the boiler adopts automatic control and has related control means of drum water level three-impulse regulation and recording, steam pressure regulation and recording, water level alarm and steam pressure alarm;
the waste heat boiler is composed of a boiler body part, flues, flue interfaces, valves and instruments in system ranges, in order to prevent solid fly ash from fouling convection heating surfaces and influencing the heat transfer effect of the heating surfaces, fixed soot blowers are arranged on a calandria and the boiler body part, and soot blowing is carried out periodically through an automatic control system to ensure the cleanness and the heat transfer effect of the convection heating surfaces;
because the rotary kiln is stirred and rolled, a large amount of dust is clamped in the generated flue gas, and soot blowing and cleaning are needed in the operation process of the waste heat boiler so as to ensure efficient heat transfer and stable steam generation;
technical parameters of the waste heat boiler are as follows:
rated evaporation capacity is 2 t/h;
nominal operating pressure (gauge pressure);
the temperature of saturated steam;
the feed water temperature is 114 ℃;
the temperature of a flue gas inlet is 850 ℃;
the temperature of a flue gas outlet is 550 ℃;
the boiler resistance is 1500 Pa;
inlet dust concentration 5000mg/Nm3
The outlet dust concentration is 500 mg/Nm;
wherein the flue gas treatment system in the step (seven):
seventhly, 1, flue gas treatment and purification process:
the method is designed aiming at the problem that the particle size of smoke dust contained in the generated waste gas is large in the sludge drying and incineration process, and is characterized by large operation elasticity, high removal rate of harmful substances and dust, less consumption of a reactant, good deacidification effect, low emission concentration of heavy metal and dioxin, and low comprehensive cost, and the discharged waste water enters a sewage treatment system for treatment;
the waste gas discharged from the bottom of the spray drying tower contains dust, a small amount of volatile organic compounds, CO, HCl, SO2, NOx and heavy metal compound related toxic and harmful substances; the waste gas discharged from the drying tower firstly enters a cyclone dust collector, then enters two bag-type dust collectors arranged in series, is discharged into three spraying towers for washing after passing through a main induced draft fan of the system, an ozone feeding pipeline is arranged on a connecting air pipe between the bag-type dust collectors and a purification tower, and finally is washed, desulfurized and denitrated through the spraying towers, and then the demisted and purified flue gas is discharged to the high altitude through a chimney after being monitored on line;
the bag-type dust remover adopts a Danish Jinerkang dust removal technology, and has the advantages of automatic timing back blowing, good dust removal effect, ash discharge of a flat-bottom scraper, circular tangential air inlet of a shell and external filtration type design, wherein the dust removal efficiency is 99.9%; dust in tail gas discharged by the spray tower can be effectively removed by using a bag-type dust collector for dust removal; an active carbon injection port is arranged on a flue gas pipeline between the two bag-type dust collectors, and the active carbon injection device injects powdery active carbon into the flue; so as to adsorb dioxin and heavy metal related harmful substances in the flue gas; passing through a rear bag-type dust collector; collecting and managing part of dioxin substances and heavy metal compounds adsorbed on the dust as hazardous wastes; tail gas discharged by the bag-type dust collector enters the spraying tower through a system induced draft fan; an ozone feeding point is arranged on an air pipe behind the bag-type dust collector; decomposing organic odor in the tail gas by ozone, purifying the tail gas, oxidizing NO into high-valence NOX, and purifying the tail gas; tail gas after the advanced oxidation deodorization process enters from the lower side of the spray tower, and the gas is firstly subjected to alkaline washing by three spray towers, SO that dust and dissolved substances in the gas can be removed, and HCl, H2S, SO2 and NOx related acidic substances in the waste gas are absorbed; conveying the alkali liquor to a high-level alkali storage tank by using an alkali liquor pump, automatically controlling the liquid level, then adding the alkali liquor to a spray tower from the high-level alkali storage tank, and conveying the spray tower spray by using a plastic lined pump to a purification tower nozzle, and spraying the spray tower from top to bottom in sections; the waste liquid generated by spraying is returned to a sewage treatment plant for centralized treatment through a sewage pipeline;
seventhly, 2, white smoke reduction flow:
the tail gas which is finally demisted and dehydrated by the tail gas treatment system enters an inner chimney, and a flue gas online monitoring system is arranged on the inner chimney to monitor the index of the exhaust component in real time;
the height of the flue gas discharge port is 45m, and a gas online monitoring system instrument is arranged before discharge according to the standard requirement;
the aspect of storage tank odor treatment considers that: the engineering is provided with a sludge receiving bin and a storage system, and in order to prevent odor from diffusing, after the sludge receiving bin and the storage system are subjected to air extraction, odorous gas is used as combustion air of the hot blast stove;
in the operation of the system, sewage is generated, and the system mainly comprises tail gas treatment desulfurization spray sewage, demister condensation and whitening sewage, ground washing sewage and worker domestic sewage, wherein the total amount is about 120 plus materials and 150t/d, and the waste water enters a pipe network of a sewage treatment plant through a sewage pump for centralized treatment;
seventhly, 4, a flue gas purification system:
the flue gas purification system refers to all equipment and facilities which are arranged for meeting the requirement of flue gas purification from a flue gas outlet of the drying tower to an outlet of a flue pipe chimney; the tail gas treatment process adopts a combined process of a cyclone dust collector, a two-stage bag dust collector, activated carbon injection, ozone denitration and deodorization, washing of a purification tower and whitening and demisting;
the flue gas temperature of the flue gas outlet of the drying tower is 110 ℃, the flue gas firstly enters a cyclone dust collector, an electric star-shaped valve is arranged at the bottom of the cyclone dust collector and is used for discharging settled dry sludge, a pressure transmitter and a thermometer are arranged at the outlet of the cyclone dust collector and are used for monitoring the circulation condition of the flue gas, the flue gas passing through the cyclone dust collector enters a bag-type dust collector, the flue gas treatment system is provided with two bag-type dust collectors, the two bag-type dust collectors are connected in series during normal operation, a cut-off valve is arranged in front of the bag-type dust collector and can be controlled electrically and manually, powdered activated carbon is sprayed into a flue pipe between the two bag-type dust collectors through an activated carbon spraying device and is fully mixed with the flue gas in a flue, heavy metal and dioxin-related pollutants in the flue gas are adsorbed by the activated carbon bag-type dust collector and enter a rear-stage bag-type dust collector along with the flue gas, and;
the bag-type dust collector is provided with a back-blowing device, a filter bag in the bag-type dust collector is back-blown regularly by utilizing compressed air, and dust attached to the surface of the filter bag is blown off by instantly back-blowing excessive air, so that the bag-type dust collection efficiency is improved;
in order to remove nitrogen oxides in the flue gas, ozone is introduced into a flue gas pipe at the rear part of the second-stage bag-type dust collector to remove organic odor in the flue gas and fully react with the NOx in the flue gas, so that the aim of denitration is fulfilled;
stage spray tower adds alkali liquor to treat acid gas, , second, third stage spray tower underpart communicate each other, the circulating alkali liquor of underpart carries on the make-up of alkali and water supplement according to the actual situation, wash the flue gas sprayed through stage, second, third stage sprays and prepares the alkali liquor and adds the mouth as well, when stage sprays and deacidifies effects insufficiently, second, third stage sprays and steps deacidify, remove dust and cool, in order to guarantee the overall treatment effect;
the method comprises the steps of removing harmful components and trace dust in flue gas by a spraying system to ensure that the flue gas is discharged after reaching standards, wherein -stage spraying towers are provided with two spraying ports, each spraying port is provided with 8 nozzles, stages of multi-stage pumps arranged after passing through a high-level alkali tank are conveyed to an alkali liquor nozzle in the middle of -stage spraying towers to atomize NaOH solution into fine liquid drops, the spraying towers are uniformly distributed and fully contact with the flue gas by a large surface area, high-price NOx and SO2 related acid gas after being oxidized are fully reacted and removed, an alkali liquor feeding system is used for keeping the pH value of a circulating solution to 8-9 to ensure the concentration of the alkali liquor, SO that the related removal rates of NOX and SOX can reach more than 80 percent, -stage spraying towers are provided with two centrifugal pumps, is provided with , alkaline spraying liquid at the bottoms of the spraying towers are conveyed to spraying ports at the tops of the spraying towers by adopting spiral nozzles to wash the residual NaOH solution at the bottom of the three-stage flue gas, the three-stage spraying towers are provided with two spraying nozzles, spraying nozzles, each spraying ports are provided with , a special spray mist eliminating devices which are provided with a spray mist eliminating devices for removing and discharging the flue gas after reaching the effect of a large amount of a white dust removing, and reducing the emission reduction of SO2, the flue gas after reaching the effect of eliminating, the emission reduction of a white smoke dust removal by adopting a flue gas treatment, the flue gas after the flue gas treatment, the flue gas treatment of a flue gas after reaching the tail gas treatment step of a flue gas purification treatment, the tail gas treatment step of a flue gas purification;
wherein, the cyclone dust collector system in the step (eight): eight.1 system description:
an electric star-shaped valve is arranged at the bottom of the cyclone dust collector, and when the cyclone dust collector normally operates, the manual gate valve keeps an open state; the smoke from the drying tower passes through a cyclone dust collector, separates dust particles from airflow by means of centrifugal force and collects the dust particles on the wall of the cyclone dust collector, then the dust particles fall into an ash bucket by means of gravity action and enter the bottom of the dust collector, and the dry mud and dust particles are input into a bottom dry mud conveying system through a star-shaped discharge valve continuously running at the bottom of the dust collector;
wherein nine.1 in the step (nine) describes the system:
the bag-type dust collector adopts a circular design, and tangentially enters air without dead angles; the key point of the system is that an electrical control system with reasonable design is adopted, 84 pulse jet pipes are subjected to pulse back blowing in sequence, and high-quality PPS + pure PTFE membrane filter bags are selected as the filter bags, so that the dust removal effect reaches that the dust is less than or equal to 10mg/Nm 3; meanwhile, in the operation process of the filtering system, under normal load, the maximum pressure difference in the back flushing process is kept below 800Pa, the operation is reliable, the back flushing and dust removing performance of the filter bag is excellent, the bottom of the dust remover is flat, and dust at the bottom is cleaned in real time by adopting a rotary scraper system, so that dust accumulation is avoided; the dust remover has good sealing performance in the whole structure, is insulated and fully covered, and avoids the occurrence of local corrosion phenomenon;
the system comprises a pulse back-blowing device, a filtering and dust removing system and an active carbon adding system, wherein the upper part and the lower part of each cloth bag are respectively provided with an overhaul , so that the cloth bags can be maintained and overhauled conveniently;
pulse blowback device:
air bags are arranged on two sides above each cloth bag and used for storing compressed air, and each air bag is provided with a pressure transmitter and used for monitoring the pressure of the compressed air in the air bag; under normal conditions, the pressure of the compressed air in the bag air bag is kept at about 0.4 Mpa; each air bag is provided with a pulse injection pipe, and the opening and closing of each injection pipe are controlled by an electromagnetic valve; each path of injection pipe is responsible for back flushing of a filter bag below the injection pipe; the injection pipe is provided with an injection port above each filter bag and is aligned to the center of each filter bag;
the injection pipe is kept normally closed by an electromagnetic valve on the injection pipe, the pulse valve is opened by the electromagnetic valve during dust cleaning, compressed air is subjected to pulse blowing by the dust cleaning control device according to a set time interval, the compressed air passes through each pulse valve in sequence at a very short time, and air which is several times of the injection air quantity is induced by a nozzle on an injection pipe to enter the filter bag to form air waves, so that the filter bag generates sharp expansion and impact vibration from the bag opening to the bottom, a strong dust cleaning effect is caused, dust is blown off from the back of the filter bag, the effective filtering area is increased, and the smoke passing resistance is effectively reduced;
the upper cabin and the lower cabin of the cloth bag are provided with pressure transmitters, and the pressure difference condition of the cloth bag can be displayed through the pressure difference between the two pressure transmitters; during operation of the filter system, the maximum pressure difference is kept below 800pa under normal load; if the pressure difference of the cloth bag is increased, the time interval of back flushing of the cloth bag can be properly shortened, the back flushing frequency is increased, when the pressure difference is within a reasonable range, the back flushing frequency is reduced as much as possible, the quantity of external cold air entering the cloth bag is reduced, the phenomenon that the cloth bag is invalid due to water vapor condensation caused by local low temperature of smoke in the cloth bag is reduced, and meanwhile, the online monitoring data of a smoke discharge port is influenced;
a filtering and dust removing system:
the filtering and dust removing system mainly comprises a filter bag and a mesh cage, and the mesh cage is divided into three sections for convenient installation, and the middle parts are connected in a buckling way; the inside of the filter bag is provided with a mesh cage framework which is used for supporting the filter bag and ensuring the effective filtering area of the filter bag;
for convenience of installation and maintenance, the cloth bag net cage is designed to be installed in sections; the filter bag is fixed on the cloth bag card by a buckle, and the mesh cage is arranged at the inner side of the filter bag and is placed on the cloth bag card;
each filter bag net cage is independent, and when an individual filter bag or net cage in the cloth bag is damaged and needs to be replaced, the filter bag net cage can be replaced independently without dismantling the rest filter bag net cages;
a residue collection system:
the ash residue collecting system consists of a cloth bag scraper and a star-shaped discharge valve;
the bottom of the cloth bag is flat, ash residues intercepted by the filter bag fall into the bottom of the cloth bag and are forcibly conveyed to the ash outlet by the scraper, the ash outlet is provided with a star-shaped discharge valve, and the scraper and the star-shaped discharge valve are normally opened during normal operation, so that the ash residues in the cloth bag are ensured to be discharged in time;
when the scraper normally operates, the current is less than or equal to 7.5A, if the current is higher, the discharging at the bottom of the cloth bag is not smooth, the scraper load is increased due to the accumulation of materials at the bottom of the cloth bag, and the scraper needs to be checked in time to remove faults;
ash and slag discharged by the star-shaped discharge valve enters a main chain conveyor through a screw conveyor so as to enter a rotary kiln incineration system;
-grade cloth bag ash slag is mainly dried fine mud, in order to prevent the accumulation of the ash slag at the bottom of the cloth bag, a thermometer is arranged at the bottom of the cloth bag, when the temperature indicated by the thermometer at the bottom of the cloth bag rises, the phenomenon of ash accumulation at the bottom of the cloth bag is indicated, whether a scraper, a star-shaped discharge valve and a screw conveyor work normally or not needs to be checked in time, faults need to be eliminated in time, and the stability of the system is ensured;
an active carbon adding system:
the activated carbon is stored in the activated carbon bin and is conveyed into a flue between the two bag-type dust collectors by the wind power of a wind blower through an activated carbon feeding device so as to adsorb dioxin and heavy metal related harmful substances in the flue gas;
the active carbon is delivered into a bin and stored by two modes of pneumatic delivery of an air pressure delivery type tank car or delivery and feeding of a cargo lift; the capacity of the activated carbon bin is required to meet the consumption of activated carbon for 1.5 days of normal operation of the incineration line;
the active carbon adding device is composed of an active carbon storage tank, a feeding device and a material pneumatic conveying device; adjusting the amount of activated carbon supplied to the flue gas according to the amount of the flue gas at the outlet of the chimney; the adding amount of the activated carbon is variable-frequency adjustable;
in the system, a flue gas pipeline between two bag-type dust collectors is provided with an active carbon injection port, and an active carbon injection device injects powdery active carbon into a flue between the two bag-type dust collectors; the air blower is used as power equipment for injecting active carbon into the flue of the bag-type dust collector;
the powder activated carbon is quantitatively fed into a Venturi injection pipe below the storage bin through a disc feeder, the disc feeder is provided with a control panel of a variable-frequency speed regulator, the control panel receives a signal of a central control system to automatically adjust the rotating speed of the disc feeder and timely adjust the injection amount of the activated carbon, and the adding amount of the activated carbon is controlled to be 8-10 kg/h like ;
the technical design requirements are as follows:
the dust remover is mainly composed of a filter chamber, an air purifying chamber, a tangential air inlet, a bottom flat-bottom scraper forced ash discharging device, a low-pressure pulse online ash cleaning device, an electric control device, a valve and other parts;
the dust remover is circular, and a scraper with a flat bottom at the bottom forcibly discharges dust out of the dust hopper in a free flow manner;
the cloth bag is made of PPS + PTFE film; fully considering the condition of meeting different temperatures of the flue gas under the desulfurization working condition or the fault working condition
Two sets of bag-type dust collectors are designed to be connected in series, a phi 1800 electric cut-off valve (manual operation during power failure) is installed at an inlet, and the filtering wind speed is less than 0.8 m/min;
the bag-type dust collector adopts a circular tangential air inlet mode so as to pre-collect dust by utilizing the cyclone effect, the air inlet is uniformly distributed, and the filtering load of the bag is reduced;
the dust remover body is round, two overhauls are designed in a double mode, and the dust remover body is insulated and fully covered;
the pulse valve is made of Shanghai Shangtai brand; the surface coating of the pulse valve is smooth and attractive, the defects of peeling, bruising, scratching and burrs are avoided, and the phenomena of looseness and damage of the fastening piece are avoided; the ash removal system is reasonable in arrangement, stable and reliable in working performance and capable of completing ash removal work according to requirements; the action of the pulse valve is sensitive and reliable; the ash removal system should have sufficient gas storage capacity;
the escalator operation platform can reach the operation surface needing to be overhauled and operated on each layer;
the ash discharging mode of the dust remover is that the bottom scraper forcibly discharges ash, so that the accumulation of the dust is effectively controlled;
the upper side of a scraper at the bottom of the dust remover is provided with a temperature monitor, and if the temperature is higher than the temperature of flue gas, the ash discharge abnormity is alarmed; monitoring the current of the scraper speed reducing motor, and if the current is higher than a normal operation value, alarming the abnormal ash discharge;
the filter bag automatically removes dust by adopting a pulse injection mode;
wherein, the wet desulfurization and denitrification system in the step (ten):
the wet denitration system mainly comprises a spraying system, a liquid caustic soda feeding system, an ozone denitration system and a cooling system;
a spraying system:
the flue gas enters a spraying system after being dedusted by a cloth bag, the spraying system is provided with three spraying towers, each spraying tower is provided with two layers of spraying, each layer of spraying is provided with 8 spray nozzles and two centrifugal pumps, a centrifugal pump is provided with , a pressure transmitter is arranged on a spraying upper water pipe of each stage and is used for monitoring the spraying condition in normal operation, the centrifugal pumps pump extracts the spraying liquid at the lower part of the spraying towers and conveys the spraying liquid to a spraying layer through a spraying main pipe, and the spraying liquid enters the spraying towers from 8 uniformly distributed spray nozzles;
in order to improve the spraying effect and ensure that the flue gas is fully contacted with the spraying liquid, pall ring packing layers are arranged below two layers of spraying of the second-level and third-level spraying towers, the spraying liquid after preliminary reaction with the flue gas is sprayed on pall rings, and the flue gas and the spraying liquid continue to be contacted and reacted under a larger comparative area, so that the spraying effect is improved;
the space at the lower part of the spray tower is used as a spray liquid buffer tank, and the spray liquid is recycled;
the method comprises the steps of , 8932, adding alkali liquor into a -grade spray tower to treat acid gas, installing an ozone uniform distribution pipeline between two layers of spray of a -grade spray tower, adding ozone to denitrate and deodorize, washing the -grade sprayed flue gas by a second-grade spray tower, steps of removing the acid gas and trace dust in the flue gas to ensure that the flue gas is discharged after reaching the standard, preparing an alkali liquor adding port for ensuring the deacidification effect and being beneficial to the tail gas discharge after reaching the standard in maintenance under the operation state, and deacidifying by the second-grade spray tower when the -grade spray deacidification effect is insufficient or needs to be maintained;
liquid caustic soda feeding system:
after being transported to a workshop on a vehicle, liquid caustic soda with the concentration of 30% is connected with an alkali inlet pump through a connector, and the liquid caustic soda is conveyed into a liquid caustic soda tank through the alkali inlet pump;
the adding amount of the liquid caustic soda is controlled by a PH meter on an -grade spray tower, in order to ensure the desulfurization effect of the liquid caustic soda, the PH of a -grade spray tower is controlled between 8 and 9, and the final grade is about 7;
ozone deNOx systems:
the denitration system can simultaneously remove NOx, sulfur dioxide and particulate matter related pollutants in flue gas at high efficiency under different concentrations and proportions of NOx related pollutants, is more efficient and better in controllability than the traditional denitration method, and is efficient alternative technologies of the traditional denitration technology;
the ozone denitration technology is added between a bag-type dust collector and a fan, the reaction time is not less than 1-1.5S, the flue gas temperature is about 100 ℃, and the operation cost of the ozone denitration is only the power consumption of the ozone equipment and the consumption of a small amount of liquid oxygen;
selecting a rated ozone concentration of 148mg/L by a 5kg/h ozone generator according to the economic operation principle of system equipment, and supplying oxygen to a liquid oxygen tank of an air source system; the output adjusting range of the ozone generator can realize linear adjustment, the adjustment correlation is realized by adopting a mode of adjusting power and air quantity simultaneously, and the cooling is related by adopting a plate heat exchanger cooling circulation; the system is related in a PLC control mode;
oxygen enters an ozone generator; the air inlet pipeline of the ozone generator is provided with a pressure reducing valve for stabilizing the working pressure of the ozone generating chamber; oxygen inside the ozone generating chamber is changed into ozone through medium-frequency high-voltage discharge, and product gas is generated through an ozone gas outlet after temperature, pressure and flow monitoring and regulation; the ozone generating chamber is provided with an ozone gas taking port, and the outlet concentration of the ozone generator is monitored on line through an ozone concentration detector equipped on the ozone generator;
the ozone generation system is provided with closed-loop circulating cooling water systems which exchange heat through a plate heat exchanger and provide cooling water for the ozone generator, wherein the closed-loop circulating cooling water systems comprise plate heat exchangers, circulating water pumps, expansion tanks and valves which are related, a flow switch and a temperature transmitter are arranged on a cooling water outlet pipeline of the ozone generator, and an alarm is given when the flow rate of cooling water is insufficient and the temperature exceeds a set value;
an ozone/oxygen leakage alarm instrument is installed in the ozone preparation room, and when the ozone/oxygen leakage in the environment in the preparation room exceeds the standard, the system determines to output an alarm, start an exhaust fan or stop the machine according to a detection signal;
in order to remove nitrogen oxides in the flue gas, ozone is added between the back of the bag-type dust collector and the main fan to remove organic odor in the flue gas and fully react with the NOx in the flue gas, so that the aim of denitration is fulfilled;
along with the continuous supplement of the circulating spray liquid, the circulating spray liquid with higher temperature in the spray tower is continuously replaced, so that the temperature and the salinity of the circulating spray liquid in the spray tower reach dynamic balances;
an th spray tower is separately provided with a fresh water supplement port with DN50 pipe diameter, and fresh cooling water is used for supplement, thereby ensuring the quality of spray circulating liquid in the spray tower under special conditions;
denitration treatment:
before the cloth bag flue gas enters the absorption tower, strong oxidant (ozone) generated by an ozone generation system is adopted to forcibly oxidize NOx in the flue gas, so that the NOx is converted into high-valence nitrogen oxide (N2O5) which is easily dissolved in water, and the oxidized high-valence nitrogen oxide enters the absorption tower along with the flue gas; dissolving in water in an absorption tower to produce nitric acid, and performing neutralization reaction with a sodium hydroxide aqueous solution in circulating slurry in the absorption tower to generate sodium nitrate;
and (3) desulfurization treatment:
the slurry circulating pump sends the circulating slurry at the bottom of the tower to the absorption section spraying layer, and the slurry is used for absorbing sulfur dioxide and nitrogen oxide in the flue gas;
system raw material medium supply:
supplying an absorbent, namely a flue gas dedusting, desulfurization and denitrification system adopts 30 percent by weight of sodium hydroxide aqueous solution as a desulfurization absorbent, sending the 30 percent by weight of sodium hydroxide aqueous solution outside a boundary area to a flue gas dedusting, desulfurization and denitrification facility, wherein the process of absorbing sulfur dioxide and nitric oxide in flue gas by using the 30 percent by weight of sodium hydroxide aqueous solution is acid-base neutralization reactions, and the 30 percent by weight of sodium hydroxide aqueous solution is continuously supplemented into the slurry of an absorption tower in order to keep the pH value of circulating slurry in the absorption tower to meet the requirement of absorbing sulfur dioxide and nitric oxide in the flue gas;
the technical requirements are as follows:
the flue gas pipeline from the cloth bag to the spray tower is 2205, , and the connecting pipeline of the second spray tower and the third spray tower is FRP;
the tower body is made of: the material of the cylindrical high-temperature-resistant resin glass fiber wound pipe fitting is FRP;
the water pump adopts mechanical seal and steel lining plastic;
valve is made of steel-lined PE;
SNCR denitration technology:
the original concentration value of the nitrogen oxides in the flue gas is 300mg/m by analyzing the sludge materials and referring to detection data of other items of my department3(ii) a The SNCR denitration adopts urea as a reducing agent; 36000Nm according to smoke amount3Calculating the consumption amount of the urea to be 10kg/h, diluting and spraying according to 10% of urea solution, wherein the pumping amount of the urea solution is 100 kg/h;
the SNCR denitration adopts an optimization process, multi-point injection is carried out at a high-temperature section of a secondary combustion chamber, and the temperature of the high-temperature section of the secondary combustion chamber is above 850 ℃; according to the temperature in the furnace, corresponding nozzles are respectively arranged for accurate injection; respectively spraying 10% urea solution into the two combustion chambers according to the number of nozzles and the temperature proportion, reducing nitrogen oxides in the flue gas into harmless nitrogen and water, and calculating the denitration efficiency according to 80%;
the SNCR denitration principle is that reducing agents such as ammonia water and urea are sprayed into an area with the temperature of 850-1100 ℃, and the reducing agents are rapidly thermally decomposed into NH3And with NO in the flue gasXReaction is carried out to generate N2And H2O; the SNCR process reactor is a high-temperature area of an incinerator;
the reaction formula is as follows: 2NO + CO (NH)3)2+1/2O2→2N2+CO2+2H2O;
Based on the original NOx content of 95%, the NO discharge capacity is 10.3kg/h, the high-valence nitrogen oxide is 0.5kg/h, and the high-valence nitrogen oxide can be removed in the subsequent deacidification process; 80% NO can be removed in the SNCR process, the urea consumption is 10.3kg/h considering that the urea loss rate is 20%, and the urea solution dosage is about 100kg/h when 10% urea solution is prepared; adopts multi-point injection, uniform feeding and atomized injection to achieve the best contact effect to enable NO to be sprayedXThe outlet concentration reaches and is superior to the European Union standard requirement;
wherein the de-whitening system and the chimney system in the step (tenth ):
the system is provided with a stainless steel heat exchanger, and the heat exchanger separates flue gas from ambient air through a specially-made metal heat exchange plate;
the saturated flue gas desulfurized by the wet method passes through the metal plate heat exchanger from top to bottom, the ambient air is extracted by the ambient air fan and enters the heat exchanger from the side edge of the metal plate heat exchanger, and the flue gas and ambient dry air perform gas-gas indirect heat exchange through the metal heat exchange plate from bottom to top, so that the temperature is reduced, a large amount of moisture is condensed to reduce the humidity of the flue gas, and the whitening effect of the stage is achieved;
the process principle is as follows: the saturated flue gas which is desulfurized by the wet method passes through the HINO-PILE plate heat exchanger from bottom to top, performing gas-gas indirect heat exchange with ambient dry air, condensing out a large amount of water, wherein the condensed water accounts for 15-30% of the total water in the flue gas, meanwhile, a large amount of heat energy is released when the moisture of the tail gas is condensed to heat the ambient dry air blown into the heat exchanger so as to increase the temperature of the ambient dry air, then the heated dry air is introduced into a chimney by an air pipe to be mixed with the flue gas after temperature reduction and dehydration, so that the humidity of the mixed flue gas is greatly reduced, the dew point temperature of the exhausted smoke is reduced, the temperature difference between the temperature (T) of the smoke at the main exhaust port and the saturation temperature (T') under the humidity condition is more than or equal to 10 ℃, so that the exhausted smoke does not reach the dew point temperature in a short time after being exhausted, and the moisture in the smoke is not condensed into water mist, thereby achieving the purpose of reducing the white smoke;
the device is provided with an environmental air fan, a variable frequency motor is adopted for frequency conversion regulation, the air quantity of the fan is full load air quantity of the device, the temperature of environmental air and the humidity of atmosphere can change along with the change of climate, and the optimal whitening visual effect can be achieved by artificially regulating the level of frequency conversion power according to the change of external factors and the whitening visual effect of smoke when in use;
the chimney is provided with an inner barrel and an outer barrel which are mutually separated, an online monitoring system is arranged above the inner barrel, and the online monitoring maintenance and repair are facilitated through a steel platform arranged outside the chimney;
the flue gas after heat exchange enters an inner cylinder of the chimney, and the environmental wind enters an outer cylinder of the chimney, so that the flue gas entering the inner cylinder can be monitored in real time by on-line monitoring, and the influence of the environmental wind is avoided;
the heated dry air is mixed with the cooled and dehydrated smoke at the outlet of the inner barrel, so that the humidity of the mixed smoke is greatly reduced, the dew point temperature of the evacuated smoke is reduced, the evacuated smoke cannot reach the dew point temperature in a short time after being discharged, and the moisture in the smoke cannot be condensed into water mist, so that the aim of reducing white smoke is fulfilled;
the environment air fan that the device was equipped with adopts inverter motor to carry out the frequency conversion regulation and control, and the amount of wind of fan is the device full load amount of wind, and along with the change of weather, the temperature of ambient air and atmospheric humidity all can change, can take off white visual effect according to the change and the flue gas of these external factors during the use, through the height of artificial regulation frequency conversion power to reach the best visual effect that takes off white.

Claims (2)

  1. The operation method of the industrial solid waste and sludge rotary kiln cooperative treatment integrated device is characterized by comprising the following steps of:
    (), structural composition:
    the system comprises a sludge receiving system, a sludge spray drying or disc drying system, a sludge incineration system, a flue gas treatment system, a wind power slag suction system and an incineration slag ash collecting system;
    the sludge receiving system, the sludge spray drying or disc drying system, the sludge incineration system, the flue gas treatment system, the wind power slag suction system and the incineration slag ash collecting system are sequentially connected;
    (II) a sludge feeding system:
    sludge reception takes place through two pathways:
    the method comprises pouring sludge with water content of 70-80% into underground receiving system, lifting with shaftless auger, feeding into large sludge storage tank with screw pump via filter, feeding into high-position mud tank with plunger pump, lifting with screw pump, feeding into spray drying tower, pumping into high-position mud tank with plunger pump via mud filter;
    the method also comprises steps of loading engineering sludge into a field, pouring the engineering sludge into a sludge receiving tank, arranging two shaftless packing augers in the sludge receiving tank, lifting the sludge to a screw pump on the side of the sludge receiving tank by using the shaftless packing augers, lifting the sludge to two sludge receiving tanks by the two screw pumps respectively, arranging two plunger pumps with hydraulic stations on the periphery of the sludge receiving tanks, preparing plunger pumps , lifting the sludge in the sludge receiving tanks to a high-level sludge storage tank in a factory by using the plunger pumps, arranging sludge filters on pipelines, screening large particles in the sludge in a step, and providing the high-level sludge storage tank with feed sludge for a drying tower;
    four DN400 pipelines are arranged below the high-level sludge storage tank and are controlled by a manual valve , the sludge falls into 4 screw pump receiving ports respectively, the lifted sludge is sent into the spray drying tower and atomized by a nozzle at the top of the tower, the compressed air is sent to the top of the tower by an air compressor room main pipe and is divided into 4 strands at the atomizing nozzle, and a pressure transmitter is arranged on an air pipe and is connected with a control room computer for adjusting the amount of compressed air entering the tower so as to achieve the optimal atomization effect;
    (III) a sludge drying system:
    the high-temperature flue gas entering the top of the spray drying tower is output from the high-temperature flue gas at the outlet of the waste heat boiler;
    the sludge is dried by spray drying or super disc drying, and is obtained or the two are used in combination;
    the spray drying is to disperse the dewatered sludge with the water content of about 80 percent into fine particles like fog by the action of an atomizer, contact the fine particles with the high-temperature flue gas for burning, remove most of water instantly and dry solid substances in the materials;
    the atomized sludge is directly dried by burning high-temperature flue gas, so that the heat loss of a complex heat exchanger is avoided, the heat utilization efficiency can be improved to more than 80 percent, and the atomized sludge is effectively atomized and dried quickly;
    through the effective atomization of the sludge, the problems of blockage and abrasion are avoided, and the dried sludge particles are uniform and reasonably distributed, so that the sludge is favorable for incineration;
    the spray drying system adopts a novel special two-fluid atomized sludge system, and the atomized sludge system is left together with the high-temperature flue gas, and the tower diameter and the tower height are adjusted by optimizing the structure of the drying system according to the characteristics of the sludge and the contact condition of the atomized sludge and the high-temperature flue gas, so that the phenomenon of sludge wall adhesion is avoided;
    the super-disc dryer adopts a steam indirect heat exchange mode, water is evaporated more quickly by stirring materials, and the dryer is suitable for semi-drying and full-drying of the materials;
    (III) a sludge incineration system:
    dried sludge with the water content of 20-30% is respectively sent into a rotary kiln for incineration through a stokehole feeding screw, industrial solid waste is combusted in a hot air furnace, and flue gas directly enters an incinerator through the hot air furnace to be incinerated together with the sludge;
    the leftover materials with the thickness determined by in the hot blast stove are burnt in a hearth to generate high-temperature smoke and enter a sludge burning system, the temperature of the hot blast stove can be controlled according to process requirements, burned-out slag is discharged from the other end of the chain grate to a slag discharging machine and is sent out by an automatic slag discharging machine, the burning hearth is built by high-temperature resistant refractory materials, and the whole burning system is electrically controlled;
    the sludge incineration system adopts a rotary incinerator-rotary kiln, a hot blast stove is integrated to the kiln head of the rotary kiln, high-temperature flue gas generated by combustion of the hot blast stove is mixed with flue gas generated by combustion of dried sludge in the rotary kiln, carbon particles/dust and high-temperature coal gas brought by flue gas enter a secondary combustion chamber for sufficient combustion and polymerization and sedimentation, high-temperature hot flue gas after secondary incineration enters a waste heat boiler, the temperature of the high-temperature hot flue gas is 750-1000 ℃, waste heat is recovered by the waste heat boiler, the high-temperature hot flue gas enters a drying tower to serve as a drying heat source of wet sludge, and finally the waste flue gas enters a tail gas treatment system;
    (IV) a dried sludge ignition flame system:
    the dried sludge ignition flame system adopts a natural gas burner, and the equipment is characterized by complete combustion and no black smoke; the hot blast stove generates 500-1000 ℃ flame, the dried sludge is heated to the ignition temperature of 300 ℃ and is made to spontaneously combust, and combustion-supporting air is fed by a high-pressure fan through a pipeline;
    the heat of natural gas has a value of 8500kcal/m3The specification of the hot blast stove is 600 ten thousand kilocalories per hour;
    (V) burning the rotary kiln:
    the dried sludge after spray drying is sent into a sludge incinerator for incineration through a chain conveyor and an inclined feeding pipe; the dried sludge after the disc drying is sent into a rotary kiln for incineration through sludge conveying equipment;
    adopting a horizontal rotary incinerator; the rotary incinerator is characterized in that high-temperature air from a hot blast stove is blown into the incinerator from a furnace end, so that the temperature of dried sludge is quickly raised and dried continuously, the dried sludge is completely combusted at the high temperature of 900 ℃, high-temperature flue gas generated by combustion is introduced into a secondary combustion chamber, then the high-temperature flue gas is distributed with air through cold air and enters a drying tower to serve as a drying heat source of wet sludge, and finally waste flue gas enters a tail gas treatment system;
    the dried sludge is fed into an inclined pipe through a dried sludge chain conveyor and then slides into the rotary kiln, and the dried sludge rotates from a high end to a low end in the rotary kiln; after sliding into the rotary kiln, the sludge is ignited when walking for 3-4 m, is burnt out when walking for 21m, falls into a slag discharging hopper after being burnt out, and is conveyed to a slag suction system through a sludge adjusting cylinder;
    the diameter of the rotary kiln is 3.7m, the length of the rotary drum is 21m, and the inclination is 1-1; 5 ℃, the rotating speed is 1-2 r/min, and the residence time of the sludge in the kiln is adjustable within 20-60 min;
    the air inlet of the rotary kiln is divided into two paths, paths of hot blast stoves supply heat flame, the temperature is 500-1000 ℃, paths of ambient air for adjusting the oxygen content in the kiln, and the exhaust temperature of the rotary kiln is above 850 ℃;
    (VI) a second combustion chamber:
    in order to ensure that harmful gas is burnt out and reaches the emission standard, the gas burned in the rotary kiln enters a secondary combustion chamber; the secondary combustion chamber adopts a vertical structure, the thickness of a heat-insulating wall body is 0.58m, so that the temperature of the secondary combustion chamber is not lower than 850 ℃, and the gas flowing time is not less than 2.5 seconds so as to decompose and control the generation of dioxin;
    (VII) a flue gas treatment system:
    seventhly, 1, flue gas treatment and purification process:
    the waste gas treatment process of a cyclone dust collector, a two-stage bag dust collector, activated carbon adsorption, ozone denitration and deodorization, three-stage spray tower washing, whitening and demisting is adopted;
    seventhly, 2, white smoke reduction flow:
    the method comprises the steps of selecting a Japanese HINO-TEC technical device, mainly utilizing gas-gas heat exchange, enabling smoke to enter a white smoke reduction device through a dehydration spray tower, cooling the smoke through a HINO-PILE plate heat exchanger, condensing a large amount of moisture, simultaneously utilizing a large amount of heat energy released during moisture condensation to heat ambient dry air, mixing the heated dry air with the smoke subjected to cooling and dehydration, greatly reducing the absolute humidity of the mixed smoke, reducing the dew point temperature of the evacuated smoke, enabling the evacuated smoke to not reach the dew point temperature in a short time after being exhausted, and further achieving the purpose of reducing the white smoke;
    seventhly, 3, a heating and ventilating system:
    the heat supply system comprises a hot blast stove, an air inducing device and a flue gas pipeline, wherein the air inducing device comprises two parts, the part introduces air to the hot blast stove to be used as combustion-supporting air, and the air is burnt and preheated by the hot blast stove and then sent into the rotary incinerator, the second part introduces flue gas discharged by the sludge incinerator into the sludge drying system, the heat source of the drying system mainly comes from 650 ℃ waste heat flue gas which is discharged by the sludge incinerator and has the temperature of over 850 ℃ and is formed by air distribution of cold air, and the heat source enters the top of the spray drying tower after being distributed by a corresponding hot air distribution system, namely, the downstream direct heating mode adopted by the drying process of the project;
    seventhly, 4, a flue gas purification system:
    designing the dry gas quantity of about 3.1 ten thousand square standard for subsequent flue gas treatment matched projects, wherein the flue gas temperature is 110 +/-10 ℃;
    (eighth), cyclone system:
    eight.1 system description:
    the cyclone dust collector is used as a middle channel of the drying tower and the tail gas treatment system, and makes the dust-containing airflow rotate, separates dust particles from the airflow by means of centrifugal force and collects the dust particles on the wall of the drying tower and makes the dust particles fall into the dust hopper by means of gravity;
    (nine), bag dust removal system:
    the bag-type dust collector adopts a circular design, and tangentially enters air without dead angles;
    (ten) a wet desulfurization and denitrification system:
    the wet denitration system mainly comprises a spraying system, a liquid caustic soda feeding system, an ozone denitration system and a cooling system;
    (ten ), a whitening system, and a chimney system:
    the de-whitening system mainly comprises a stainless steel heat exchanger and an environmental air fan.
  2. 2. The operation method of the kinds of industrial solid wastes and sludge rotary kiln co-processing integrated device as claimed in claim 1, wherein:
    wherein the sludge feeding system in the step (II):
    two sludge receiving ways are provided with two control modes, namely a manual control mode and an electric control mode:
    the effective depth of the sludge receiving tank is 4.5m, a sealed room adopting a brick-concrete structure is built above the sludge receiving tank, and the occupied area is 70m2(ii) a A filter screen is arranged above the receiving tank to screen out large impurities in the sludge;
    air pumping ports are respectively arranged above the sludge receiving pool and at the top of the sludge low-level storage tank, and odor in the bin is pumped as combustion-supporting air of the sludge incinerator, so that a storage pit area forms negative pressure to prevent odor from overflowing; the extracted air is sent into a hearth for incineration, and the malodorous substances in the air are decomposed and oxidized in the combustion process;
    the sludge receiving tank is provided with two sludge receiving tanks, the height of each sludge receiving tank is 18m, the radius of each sludge receiving tank is 10.5m, and the storage capacity of each sludge receiving tank is 1500m3The capacity of the high-level sludge storage tank is about 100m3
    The pipelines before sludge atomization are respectively provided with a tower top flowmeter; each tower is provided with 4 atomizing nozzles, and the consumption of compressed air at each nozzle is 7m3Min, pressure 0.45 mPa;
    wherein the sludge drying system in the step (II):
    the drying tower of the engineering has the diameter phi of 10m to 15m, the effective height of the drying process is 25m, each tower is provided with 4 to 10 atomizing nozzles, and the spraying angle of the nozzles is adjustable between 50 and 80 ℃; the amount of compressed air at each nozzle is 7m3Min, pressure 0.45Mpa, sludge treatment capacity of each nozzle 4m3/h;
    Auxiliary equipment, an atomization system and an air distribution system are arranged in the drying tower, the atomization system is used for forming the sludge into granular droplets with the particle size of 30-500 mu m, and the sludge is naturally granulated after drying; the air distribution system has the function of enabling air distribution in the drying system to be uniform, so that the sludge is more effectively dried, and the heat utilization efficiency is improved; the air quantity source of the air distribution system is high-temperature flue gas generated by the incineration system; the compressed air is conveyed to the top of the tower through a header pipe and is divided into 4 strands at an atomizing nozzle, and a pressure transmitter is arranged on an air pipe and is connected with a control room computer for adjusting the air consumption;
    the temperature of the high-temperature flue gas entering the top of the spray drying tower is 550 ℃, the pressure is-500 Pa, and the high-temperature flue gas is output from the outlet of the waste heat boiler; an air supplementing system and a main air valve are arranged on the tower inlet flue gas pipeline and used for adjusting the air quantity: a thermocouple is arranged on the high-temperature flue gas pipeline to measure the temperature, a thermocouple and a pressure transmitter are arranged on the mixed flue gas pipeline, all temperature and pressure monitoring is connected with a computer in a control room, the temperature and pressure changes are monitored in time, the opening degree of a cold air valve and a main air valve is adjusted, cold air comes from the treated gas of an inner chimney, and the gas taking has the advantages of energy conservation and low oxygen content; the sludge outlet temperature of the drying tower is 50-60 ℃, and the water content of the sludge is about 20%;
    the drying tower is made of heat-resistant stainless steel SUS310S and 2205, the heat-insulating material is an aluminum silicate fiberboard, the heat-insulating material is determined according to different temperature zones, the maximum thickness of the heat-insulating thickness is 250mm, the minimum thickness is 100mm, and the heat-insulating material is externally provided with a 304 stainless steel outer skin; because the volatile gas quantity generated in the drying process and the dust concentration in the tower are both very low and are far lower than the explosion limit of the combustible gas and dust concentration, the control of the drying tower on the oxygen content is not considered in the design, and the water content of the sludge with the water content of 80 percent is reduced to 20 percent after drying;
    the spray drying is to disperse the dewatered sludge with the water content of about 80 percent into fine particles like fog through the action of an atomizer, increase the heat transfer surface area, accelerate the drying, contact with the incineration high-temperature flue gas, instantly remove most of water, and dry the solid matters in the materials, wherein the drying process is rapid, the heat utilization rate is high, the incineration high-temperature flue gas is used for directly drying the atomized sludge, the heat loss of a complex heat exchanger is avoided, the heat utilization efficiency can be improved to more than 80 percent, the effective atomization and the drying are rapid, the problems of blockage and abrasion are avoided through the effective atomization of the sludge, the dried sludge particles are uniform and reasonably distributed, the particle mesh degree is 60-120 meshes, the incineration is facilitated, the spray drying tower is safe and stable, the drying degree of the sludge particles is regulated and controlled, the safety and the dust explosion are ensured, the flue gas temperature is rapidly reduced from 550 ℃ to below 200 ℃, the cooling time is less than 1.5s, the regeneration of dioxin and the precursors of the dioxin can be prevented, the drying process is extremely less volatile organic gas can be absorbed in the atomized in the sludge, the subsequent spray drying tower, and the subsequent flue gas drying treatment load and the subsequent flue gas purification facility;
    the main body of the dryer consists of cylindrical shells, hollow shafts and groups of hollow disks welded on the shafts, a heat medium flows through the hollow disks and indirectly transmits heat to sludge through the disks, the sludge passes between the super disks and the shells and receives the heat transmitted by the super disks to evaporate water, and the generated water vapor is gathered in a dome above the super disks and is taken out of the dryer by a small amount of ventilation;
    wherein in the step (III), the sludge incineration system:
    the rotary kiln comprises a kiln head, a kiln body, a kiln tail and related mechanisms of a transmission mechanism, wherein the kiln head is mainly used for smoothly feeding materials, arranging sets of multifunctional burners and conveying combustion air, sealing the rotary kiln and the kiln head, the kiln head sealing device of the incinerator is sealed by a traction rope sealing system by adopting a composite graphite block, and has good sealing effect, a kiln face cover of the rotary kiln is protected by refractory materials, waste collectors are arranged at the lower part of the kiln face cover for collecting waste leakage, the rotary kiln body is cylinders rolled by a steel plate, the inclination of the cylinder is 2.5% for ensuring that the materials are conveyed downwards, supporting and transmission parts are reinforced by a 50mm steel plate, the outer surface of the rotary kiln body is coated with high-temperature resistant paint and resists the temperature of 500 ℃, two belt wheels and gear rings are arranged on the rotary kiln body, the transmission mechanism drives a large gear ring on the rotary kiln body through a pinion, then drives the rotary kiln body to rotate through the large gear ring, the rotary kiln tail is a transition body connected with the rotary kiln body and the rotary kiln body, the rotary kiln body and the rotary kiln tail is a transition body, and a kiln which is a flue gas-fired air regulating valve which is used for ensuring that the rotary kiln is used for controlling the combustion of a secondary air-fired kiln, and a secondary air-fired furnace-fired-air-fired-operated automatic air-fired-operated secondary-operated auxiliary-operated air-operated auxiliary-;
    1, the incineration system comprises:
    the sludge incineration system consists of the following main devices:
    a rotary incinerator: the incinerator body, the gear transmission mechanism, the refractory lining and the air distribution device;
    hot blast stove: the hot blast stove comprises a hot blast stove body, a feeding system, a slag discharging system and an air distribution system;
    ignition and auxiliary combustion equipment: the ignition combustor, the ignition combustor fan and the spiral slag conveyor;
    a second combustion chamber: a second combustion chamber body and a refractory lining;
    a combustion air system: comprises a blower;
    ① rotary incinerator, which is the most important part of incinerator, where all the incineration reactions determining the discharge result occur, the incinerator is composed of sludge distributor and hearth, the sludge distributor is used to make air contact with sludge to the maximum in the incinerator load range, the sludge distributor adopts bar grid structure to divide the sludge into small flows to generate good sludge flow distribution, making the sludge flow contact with high temperature air to the maximum, burning fast and making the solid in the incinerator flow to the slag outlet, the sludge distributor should have the characteristics of heat resistance, high temperature gas corrosion resistance, simple structure, easy maintenance and small abrasion;
    ② incinerator furnace hearth is heat insulation furnace hearth, inner wall is wear resistant and high temperature resistant material, fire resistant layer is outside heat insulation material, the most outside layer is steel welding cylinder to ensure furnace hearth sealing, start burner, secondary air nozzle, necessary measuring instrument are installed at incinerator head, and explosion proof is reserved on incinerator smoke outlet pipeline, fire resistant and heat insulation material ensures room temperature state, outer wall temperature of incinerator is not higher than 50 deg.C;
    ③ ignition and auxiliary combustion equipment, wherein the incinerator is equipped with ignition burner, diesel oil is used for combustion supporting, when the incinerator is started, the ignition burner is needed to raise the incinerator temperature to 850 ℃, sludge is started to be thrown in, and when the incinerator is normally operated, the oil supply amount is adjusted or the incinerator is quitted from operating according to the change of the heat value and the solid content of the sludge;
    ④ air burning system, wherein the air quantity required by sludge burning is times air and secondary air, times air is supplied by auxiliary burner, the high temperature air from burner is distributed uniformly on the cross section of the whole hearth, and contacts with small mud flow fully to the utmost extent, quickly dries the residual water in sludge and raises the temperature of sludge, and the secondary air enters air through air pipe mounted on the furnace end to supplement the air required by sludge complete burning, and forms strong turbulence in the suspension burning space, to maintain the best burning condition and control the formation of CO and NO X;
    ⑤ slag storage and conveying equipment, wherein the slag of the incinerator flows from a furnace end to a furnace tail end along with the rotation of the incinerator, is cooled by water spraying, and is conveyed to a slag tank through a pneumatic conveying system, and if the slag generated in the incineration process is identified as -shaped solid waste, the slag is temporarily stored in the slag tank and then is conveyed to a brick factory for making bricks or a nearby cement factory for producing cement or bricks;
    thirdly, 2, technical parameters of the rotary incinerator are as follows:
    analyzing according to material sources, mixing and matching the sludge entering the rotary kiln with municipal and industrial sludge, calculating according to the water content of the sludge entering the kiln as 20%, and taking the converted heat value of the sludge as 8.9MJ/kg as a design basis;
    the incinerator can ensure that the sludge is completely incinerated, the temperature of the flue gas in the hearth is above 650 ℃, the temperature is above 850 ℃ after the flue gas enters the second combustion chamber, and the retention time is not less than 2.5 seconds;
    size: outer diameter/inner diameter phi 3700/phi 3000, and length L of 21.5 m;
    designing the amount of dry sludge in a single furnace: 5208 kg/h;
    rotating speed: 0.2-2 rp/min;
    inclination: 2.5 percent;
    designing the solid content of the sludge in the furnace: 80 percent;
    ash scorching and reducing rate: < 5%;
    incinerator load variation range: 70% -110%;
    wherein the dried sludge ignition flame system in the step (IV):
    fan parameters: the air quantity is 8306m3/h, the full pressure is 11377pa, and the power is 45 kw;
    when the natural gas is used as a standby auxiliary fuel and is used for unstable leftover material supply, the natural gas adopts a low-nitrogen combustion technology, and the adopted combustor is a combustor based on the low-nitrogen combustion technology;
    fourthly, 1 composition of the incineration system:
    the sludge incineration system consists of the following main devices:
    a rotary incinerator: the incinerator comprises an incinerator body, a gear transmission mechanism, a refractory lining and a sludge distributing device;
    ignition and auxiliary combustion equipment: an ignition burner, an ignition burner fan;
    a combustion air system: comprises a blower;
    wherein, in the step (six), the second combustion chamber:
    when the sludge heat value is low and the burning calorific value is insufficient, so that the temperature of a secondary combustion chamber cannot reach 850 ℃, a 300 ten thousand kilocalories per hour natural gas combustion system is arranged at the bottom side of the secondary combustion chamber, a combustion-supporting fan is used for supplying heat at 4328m3/h, the full pressure 10770pa and the power 22kw, so as to supplement heat at the time of insufficient temperature, a 3T technology is adopted to inhibit the generation of dioxin-like substances, gas generated by volatilization and pyrolysis in the burning process forms high-temperature rotary backflow-shaped flame at the temperature of more than 850 ℃ in the burning furnace, the retention time of flue gas in a high-temperature area is more than or equal to 2s, the thorough burning of organic matters and pyrolysis gas is realized, the generation of dioxin is avoided from the source, the dioxin and heavy metals in the flue gas are removed, the emission index of dioxin and heavy metal related substances in the flue gas is ensured to reach the requirement, an auxiliary purification measure for activated carbon injection is added in the flue gas purification system, the activated carbon is pan applied adsorbent, the adsorbed large specific surface area of the activated carbon is mainly depended on the large specific surface area of the activated carbon, the same mass of the activated carbon, and the mixed turbulent flow of the flue gas can reach 10000, and the purification efficiency is enough to be purified by the;
    sixth, 1 waste heat recovery system:
    after the flue gas is fully combusted in the front-end rotary kiln and the secondary combustion chamber, the temperature of the flue gas is higher than 850 ℃, a waste heat boiler is arranged at the top of the secondary combustion chamber, the flue gas enters the waste heat boiler for waste heat recovery, and the exhaust temperature of the waste heat boiler is 550 ℃; the design and the construction of the waste heat boiler consider high utilization rate and long-term continuous operation, and fully consider high-temperature corrosion of the flue gas; the high-temperature area of the waste heat boiler adopts a membrane wall radiation heating mode, the temperature of the high-temperature area of the waste heat boiler is 850-500 ℃, and a flue inlet of the waste heat boiler is not allowed to be provided with a heat exchange pipe for directly blowing flue gas, so that high-temperature corrosion is avoided;
    in order to fully recover the combustion waste heat, a boiler matched with the incinerator is arranged and used as a heat source for drying the disc, and the waste heat is recovered to the maximum extent on the premise of realizing sludge reduction; the steam of most steam is connected into a disc dryer as a heating medium, a steam collecting box is arranged in an indirect sludge heating and steam heating system and used for distributing steam used in each process, and safety valves are respectively arranged on the steam collecting box and a boiler drum; an emergency waterproof pipe is arranged on a steam drum of the waste heat boiler; the control of the boiler adopts automatic control and has related control means of drum water level three-impulse regulation and recording, steam pressure regulation and recording, water level alarm and steam pressure alarm;
    the waste heat boiler is composed of a boiler body part, flues, flue interfaces, valves and instruments in system ranges, in order to prevent solid fly ash from fouling convection heating surfaces and influencing the heat transfer effect of the heating surfaces, fixed soot blowers are arranged on a calandria and the boiler body part, and soot blowing is carried out periodically through an automatic control system to ensure the cleanness and the heat transfer effect of the convection heating surfaces;
    because the rotary kiln is stirred and rolled, a large amount of dust is clamped in the generated flue gas, and soot blowing and cleaning are needed in the operation process of the waste heat boiler so as to ensure efficient heat transfer and stable steam generation;
    technical parameters of the waste heat boiler are as follows:
    rated evaporation capacity is 2 t/h;
    nominal operating pressure (gauge pressure);
    the temperature of saturated steam;
    the feed water temperature is 114 ℃;
    the temperature of a flue gas inlet is 850 ℃;
    the temperature of a flue gas outlet is 550 ℃;
    the boiler resistance is 1500 Pa;
    inlet dust concentration 5000mg/Nm3
    The outlet dust concentration is 500 mg/Nm;
    wherein the flue gas treatment system in the step (seven):
    seventhly, 1, flue gas treatment and purification process:
    the method is designed aiming at the problem that the particle size of smoke dust contained in the generated waste gas is large in the sludge drying and incineration process, and is characterized by large operation elasticity, high removal rate of harmful substances and dust, less consumption of a reactant, good deacidification effect, low emission concentration of heavy metal and dioxin, and low comprehensive cost, and the discharged waste water enters a sewage treatment system for treatment;
    the waste gas discharged from the bottom of the spray drying tower contains dust, a small amount of volatile organic compounds, CO, HCl, SO2, NOx and heavy metal compound related toxic and harmful substances; the waste gas discharged from the drying tower firstly enters a cyclone dust collector, then enters two bag-type dust collectors arranged in series, is discharged into three spraying towers for washing after passing through a main induced draft fan of the system, an ozone feeding pipeline is arranged on a connecting air pipe between the bag-type dust collectors and a purification tower, and finally is washed, desulfurized and denitrated through the spraying towers, and then the demisted and purified flue gas is discharged to the high altitude through a chimney after being monitored on line;
    the bag-type dust remover adopts a Danish Jinerkang dust removal technology, and has the advantages of automatic timing back blowing, good dust removal effect, ash discharge of a flat-bottom scraper, circular tangential air inlet of a shell and external filtration type design, wherein the dust removal efficiency is 99.9%; dust in tail gas discharged by the spray tower can be effectively removed by using a bag-type dust collector for dust removal; an active carbon injection port is arranged on a flue gas pipeline between the two bag-type dust collectors, and the active carbon injection device injects powdery active carbon into the flue; so as to adsorb dioxin and heavy metal related harmful substances in the flue gas; passing through a rear bag-type dust collector; collecting and managing part of dioxin substances and heavy metal compounds adsorbed on the dust as hazardous wastes; tail gas discharged by the bag-type dust collector enters the spraying tower through a system induced draft fan; an ozone feeding point is arranged on an air pipe behind the bag-type dust collector; decomposing organic odor in the tail gas by ozone, purifying the tail gas, oxidizing NO into high-valence NOX, and purifying the tail gas; tail gas after the advanced oxidation deodorization process enters from the lower side of the spray tower, and the gas is firstly subjected to alkaline washing by three spray towers, SO that dust and dissolved substances in the gas can be removed, and HCl, H2S, SO2 and NOx related acidic substances in the waste gas are absorbed; conveying the alkali liquor to a high-level alkali storage tank by using an alkali liquor pump, automatically controlling the liquid level, then adding the alkali liquor to a spray tower from the high-level alkali storage tank, and conveying the spray tower spray by using a plastic lined pump to a purification tower nozzle, and spraying the spray tower from top to bottom in sections; the waste liquid generated by spraying is returned to a sewage treatment plant for centralized treatment through a sewage pipeline;
    seventhly, 2, white smoke reduction flow:
    the tail gas which is finally demisted and dehydrated by the tail gas treatment system enters an inner chimney, and a flue gas online monitoring system is arranged on the inner chimney to monitor the index of the exhaust component in real time;
    the height of the flue gas discharge port is 45m, and a gas online monitoring system instrument is arranged before discharge according to the standard requirement;
    the aspect of storage tank odor treatment considers that: the engineering is provided with a sludge receiving bin and a storage system, and in order to prevent odor from diffusing, after the sludge receiving bin and the storage system are subjected to air extraction, odorous gas is used as combustion air of the hot blast stove;
    in the operation of the system, sewage is generated, and the system mainly comprises tail gas treatment desulfurization spray sewage, demister condensation and whitening sewage, ground washing sewage and worker domestic sewage, wherein the total amount is about 120 plus materials and 150t/d, and the waste water enters a pipe network of a sewage treatment plant through a sewage pump for centralized treatment;
    seventhly, 4, a flue gas purification system:
    the flue gas purification system refers to all equipment and facilities which are arranged for meeting the requirement of flue gas purification from a flue gas outlet of the drying tower to an outlet of a flue pipe chimney; the tail gas treatment process adopts a combined process of a cyclone dust collector, a two-stage bag dust collector, activated carbon injection, ozone denitration and deodorization, washing of a purification tower and whitening and demisting;
    the flue gas temperature of the flue gas outlet of the drying tower is 110 ℃, the flue gas firstly enters a cyclone dust collector, an electric star-shaped valve is arranged at the bottom of the cyclone dust collector and is used for discharging settled dry sludge, a pressure transmitter and a thermometer are arranged at the outlet of the cyclone dust collector and are used for monitoring the circulation condition of the flue gas, the flue gas passing through the cyclone dust collector enters a bag-type dust collector, the flue gas treatment system is provided with two bag-type dust collectors, the two bag-type dust collectors are connected in series during normal operation, a cut-off valve is arranged in front of the bag-type dust collector and can be controlled electrically and manually, powdered activated carbon is sprayed into a flue pipe between the two bag-type dust collectors through an activated carbon spraying device and is fully mixed with the flue gas in a flue, heavy metal and dioxin-related pollutants in the flue gas are adsorbed by the activated carbon bag-type dust collector and enter a rear-stage bag-type dust collector along with the flue gas, and;
    the bag-type dust collector is provided with a back-blowing device, a filter bag in the bag-type dust collector is back-blown regularly by utilizing compressed air, and dust attached to the surface of the filter bag is blown off by instantly back-blowing excessive air, so that the bag-type dust collection efficiency is improved;
    in order to remove nitrogen oxides in the flue gas, ozone is introduced into a flue gas pipe at the rear part of the second-stage bag-type dust collector to remove organic odor in the flue gas and fully react with the NOx in the flue gas, so that the aim of denitration is fulfilled;
    stage spray tower adds alkali liquor to treat acid gas, , second, third stage spray tower underpart communicate each other, the circulating alkali liquor of underpart carries on the make-up of alkali and water supplement according to the actual situation, wash the flue gas sprayed through stage, second, third stage sprays and prepares the alkali liquor and adds the mouth as well, when stage sprays and deacidifies effects insufficiently, second, third stage sprays and steps deacidify, remove dust and cool, in order to guarantee the overall treatment effect;
    the method comprises the steps of removing harmful components and trace dust in flue gas by a spraying system to ensure that the flue gas is discharged after reaching standards, wherein -stage spraying towers are provided with two spraying ports, each spraying port is provided with 8 nozzles, stages of multi-stage pumps arranged after passing through a high-level alkali tank are conveyed to an alkali liquor nozzle in the middle of -stage spraying towers to atomize NaOH solution into fine liquid drops, the spraying towers are uniformly distributed and fully contact with the flue gas by a large surface area, high-price NOx and SO2 related acid gas after being oxidized are fully reacted and removed, an alkali liquor feeding system is used for keeping the pH value of a circulating solution to 8-9 to ensure the concentration of the alkali liquor, SO that the related removal rates of NOX and SOX can reach more than 80 percent, -stage spraying towers are provided with two centrifugal pumps, is provided with , alkaline spraying liquid at the bottoms of the spraying towers are conveyed to spraying ports at the tops of the spraying towers by adopting spiral nozzles to wash the residual NaOH solution at the bottom of the three-stage flue gas, the three-stage spraying towers are provided with two spraying nozzles, spraying nozzles, each spraying ports are provided with , a special spray mist eliminating devices which are provided with a spray mist eliminating devices for removing and discharging the flue gas after reaching the effect of a large amount of a white dust removing, and reducing the emission reduction of SO2, the flue gas after reaching the effect of eliminating, the emission reduction of a white smoke dust removal by adopting a flue gas treatment, the flue gas after the flue gas treatment, the flue gas treatment of a flue gas after reaching the tail gas treatment step of a flue gas purification treatment, the tail gas treatment step of a flue gas purification;
    wherein, the cyclone dust collector system in the step (eight): eight.1 system description:
    an electric star-shaped valve is arranged at the bottom of the cyclone dust collector, and when the cyclone dust collector normally operates, the manual gate valve keeps an open state; the smoke from the drying tower passes through a cyclone dust collector, separates dust particles from airflow by means of centrifugal force and collects the dust particles on the wall of the cyclone dust collector, then the dust particles fall into an ash bucket by means of gravity action and enter the bottom of the dust collector, and the dry mud and dust particles are input into a bottom dry mud conveying system through a star-shaped discharge valve continuously running at the bottom of the dust collector;
    wherein nine.1 in the step (nine) describes the system:
    the bag-type dust collector adopts a circular design, and tangentially enters air without dead angles; the key point of the system is that an electrical control system with reasonable design is adopted, 84 pulse jet pipes are subjected to pulse back blowing in sequence, and high-quality PPS + pure PTFE membrane filter bags are selected as the filter bags, so that the dust removal effect reaches that the dust is less than or equal to 10mg/Nm 3; meanwhile, in the operation process of the filtering system, under normal load, the maximum pressure difference in the back flushing process is kept below 800Pa, the operation is reliable, the back flushing and dust removing performance of the filter bag is excellent, the bottom of the dust remover is flat, and dust at the bottom is cleaned in real time by adopting a rotary scraper system, so that dust accumulation is avoided; the dust remover has good sealing performance in the whole structure, is insulated and fully covered, and avoids the occurrence of local corrosion phenomenon;
    the system comprises a pulse back-blowing device, a filtering and dust removing system and an active carbon adding system, wherein the upper part and the lower part of each cloth bag are respectively provided with an overhaul , so that the cloth bags can be maintained and overhauled conveniently;
    pulse blowback device:
    air bags are arranged on two sides above each cloth bag and used for storing compressed air, and each air bag is provided with a pressure transmitter and used for monitoring the pressure of the compressed air in the air bag; under normal conditions, the pressure of the compressed air in the bag air bag is kept at about 0.4 Mpa; each air bag is provided with a pulse injection pipe, and the opening and closing of each injection pipe are controlled by an electromagnetic valve; each path of injection pipe is responsible for back flushing of a filter bag below the injection pipe; the injection pipe is provided with an injection port above each filter bag and is aligned to the center of each filter bag;
    the injection pipe is kept normally closed by an electromagnetic valve on the injection pipe, the pulse valve is opened by the electromagnetic valve during dust cleaning, compressed air is subjected to pulse blowing by the dust cleaning control device according to a set time interval, the compressed air passes through each pulse valve in sequence at a very short time, and air which is several times of the injection air quantity is induced by a nozzle on an injection pipe to enter the filter bag to form air waves, so that the filter bag generates sharp expansion and impact vibration from the bag opening to the bottom, a strong dust cleaning effect is caused, dust is blown off from the back of the filter bag, the effective filtering area is increased, and the smoke passing resistance is effectively reduced;
    the upper cabin and the lower cabin of the cloth bag are provided with pressure transmitters, and the pressure difference condition of the cloth bag can be displayed through the pressure difference between the two pressure transmitters; during operation of the filter system, the maximum pressure difference is kept below 800pa under normal load; if the pressure difference of the cloth bag is increased, the time interval of back flushing of the cloth bag can be properly shortened, the back flushing frequency is increased, when the pressure difference is within a reasonable range, the back flushing frequency is reduced as much as possible, the quantity of external cold air entering the cloth bag is reduced, the phenomenon that the cloth bag is invalid due to water vapor condensation caused by local low temperature of smoke in the cloth bag is reduced, and meanwhile, the online monitoring data of a smoke discharge port is influenced;
    a filtering and dust removing system:
    the filtering and dust removing system mainly comprises a filter bag and a mesh cage, and the mesh cage is divided into three sections for convenient installation, and the middle parts are connected in a buckling way; the inside of the filter bag is provided with a mesh cage framework which is used for supporting the filter bag and ensuring the effective filtering area of the filter bag;
    for convenience of installation and maintenance, the cloth bag net cage is designed to be installed in sections; the filter bag is fixed on the cloth bag card by a buckle, and the mesh cage is arranged at the inner side of the filter bag and is placed on the cloth bag card;
    each filter bag net cage is independent, and when an individual filter bag or net cage in the cloth bag is damaged and needs to be replaced, the filter bag net cage can be replaced independently without dismantling the rest filter bag net cages;
    a residue collection system:
    the ash residue collecting system consists of a cloth bag scraper and a star-shaped discharge valve;
    the bottom of the cloth bag is flat, ash residues intercepted by the filter bag fall into the bottom of the cloth bag and are forcibly conveyed to the ash outlet by the scraper, the ash outlet is provided with a star-shaped discharge valve, and the scraper and the star-shaped discharge valve are normally opened during normal operation, so that the ash residues in the cloth bag are ensured to be discharged in time;
    when the scraper normally operates, the current is less than or equal to 7.5A, if the current is higher, the discharging at the bottom of the cloth bag is not smooth, the scraper load is increased due to the accumulation of materials at the bottom of the cloth bag, and the scraper needs to be checked in time to remove faults;
    ash and slag discharged by the star-shaped discharge valve enters a main chain conveyor through a screw conveyor so as to enter a rotary kiln incineration system;
    -grade cloth bag ash slag is mainly dried fine mud, in order to prevent the accumulation of the ash slag at the bottom of the cloth bag, a thermometer is arranged at the bottom of the cloth bag, when the temperature indicated by the thermometer at the bottom of the cloth bag rises, the phenomenon of ash accumulation at the bottom of the cloth bag is indicated, whether a scraper, a star-shaped discharge valve and a screw conveyor work normally or not needs to be checked in time, faults need to be eliminated in time, and the stability of the system is ensured;
    an active carbon adding system:
    the activated carbon is stored in the activated carbon bin and is conveyed into a flue between the two bag-type dust collectors by the wind power of a wind blower through an activated carbon feeding device so as to adsorb dioxin and heavy metal related harmful substances in the flue gas;
    the active carbon is delivered into a bin and stored by two modes of pneumatic delivery of an air pressure delivery type tank car or delivery and feeding of a cargo lift; the capacity of the activated carbon bin is required to meet the consumption of activated carbon for 1.5 days of normal operation of the incineration line;
    the active carbon adding device is composed of an active carbon storage tank, a feeding device and a material pneumatic conveying device; adjusting the amount of activated carbon supplied to the flue gas according to the amount of the flue gas at the outlet of the chimney; the adding amount of the activated carbon is variable-frequency adjustable;
    in the system, a flue gas pipeline between two bag-type dust collectors is provided with an active carbon injection port, and an active carbon injection device injects powdery active carbon into a flue between the two bag-type dust collectors; the air blower is used as power equipment for injecting active carbon into the flue of the bag-type dust collector;
    the powder activated carbon is quantitatively fed into a Venturi injection pipe below the storage bin through a disc feeder, the disc feeder is provided with a control panel of a variable-frequency speed regulator, the control panel receives a signal of a central control system to automatically adjust the rotating speed of the disc feeder and timely adjust the injection amount of the activated carbon, and the adding amount of the activated carbon is controlled to be 8-10 kg/h like ;
    the technical design requirements are as follows:
    the dust remover is mainly composed of a filter chamber, an air purifying chamber, a tangential air inlet, a bottom flat-bottom scraper forced ash discharging device, a low-pressure pulse online ash cleaning device, an electric control device, a valve and other parts;
    the dust remover is circular, and a scraper with a flat bottom at the bottom forcibly discharges dust out of the dust hopper in a free flow manner;
    the cloth bag is made of PPS + PTFE film; fully considering the condition of meeting different temperatures of the flue gas under the desulfurization working condition or the fault working condition
    Two sets of bag-type dust collectors are designed to be connected in series, a phi 1800 electric cut-off valve (manual operation during power failure) is installed at an inlet, and the filtering wind speed is less than 0.8 m/min;
    the bag-type dust collector adopts a circular tangential air inlet mode so as to pre-collect dust by utilizing the cyclone effect, the air inlet is uniformly distributed, and the filtering load of the bag is reduced;
    the dust remover body is round, two overhauls are designed in a double mode, and the dust remover body is insulated and fully covered;
    the pulse valve is made of Shanghai Shangtai brand; the surface coating of the pulse valve is smooth and attractive, the defects of peeling, bruising, scratching and burrs are avoided, and the phenomena of looseness and damage of the fastening piece are avoided; the ash removal system is reasonable in arrangement, stable and reliable in working performance and capable of completing ash removal work according to requirements; the action of the pulse valve is sensitive and reliable; the ash removal system should have sufficient gas storage capacity;
    the escalator operation platform can reach the operation surface needing to be overhauled and operated on each layer;
    the ash discharging mode of the dust remover is that the bottom scraper forcibly discharges ash, so that the accumulation of the dust is effectively controlled;
    the upper side of a scraper at the bottom of the dust remover is provided with a temperature monitor, and if the temperature is higher than the temperature of flue gas, the ash discharge abnormity is alarmed; monitoring the current of the scraper speed reducing motor, and if the current is higher than a normal operation value, alarming the abnormal ash discharge;
    the filter bag automatically removes dust by adopting a pulse injection mode;
    wherein, the wet desulfurization and denitrification system in the step (ten):
    the wet denitration system mainly comprises a spraying system, a liquid caustic soda feeding system, an ozone denitration system and a cooling system;
    a spraying system:
    the flue gas enters a spraying system after being dedusted by a cloth bag, the spraying system is provided with three spraying towers, each spraying tower is provided with two layers of spraying, each layer of spraying is provided with 8 spray nozzles and two centrifugal pumps, a centrifugal pump is provided with , a pressure transmitter is arranged on a spraying upper water pipe of each stage and is used for monitoring the spraying condition in normal operation, the centrifugal pumps pump extracts the spraying liquid at the lower part of the spraying towers and conveys the spraying liquid to a spraying layer through a spraying main pipe, and the spraying liquid enters the spraying towers from 8 uniformly distributed spray nozzles;
    in order to improve the spraying effect and ensure that the flue gas is fully contacted with the spraying liquid, pall ring packing layers are arranged below two layers of spraying of the second-level and third-level spraying towers, the spraying liquid after preliminary reaction with the flue gas is sprayed on pall rings, and the flue gas and the spraying liquid continue to be contacted and reacted under a larger comparative area, so that the spraying effect is improved;
    the space at the lower part of the spray tower is used as a spray liquid buffer tank, and the spray liquid is recycled;
    the method comprises the steps of , 8932, adding alkali liquor into a -grade spray tower to treat acid gas, installing an ozone uniform distribution pipeline between two layers of spray of a -grade spray tower, adding ozone to denitrate and deodorize, washing the -grade sprayed flue gas by a second-grade spray tower, steps of removing the acid gas and trace dust in the flue gas to ensure that the flue gas is discharged after reaching the standard, preparing an alkali liquor adding port for ensuring the deacidification effect and being beneficial to the tail gas discharge after reaching the standard in maintenance under the operation state, and deacidifying by the second-grade spray tower when the -grade spray deacidification effect is insufficient or needs to be maintained;
    liquid caustic soda feeding system:
    after being transported to a workshop on a vehicle, liquid caustic soda with the concentration of 30% is connected with an alkali inlet pump through a connector, and the liquid caustic soda is conveyed into a liquid caustic soda tank through the alkali inlet pump;
    the adding amount of the liquid caustic soda is controlled by a PH meter on an -grade spray tower, in order to ensure the desulfurization effect of the liquid caustic soda, the PH of a -grade spray tower is controlled between 8 and 9, and the final grade is about 7;
    ozone deNOx systems:
    the denitration system can simultaneously remove NOx, sulfur dioxide and particulate matter related pollutants in flue gas at high efficiency under different concentrations and proportions of NOx related pollutants, is more efficient and better in controllability than the traditional denitration method, and is efficient alternative technologies of the traditional denitration technology;
    the ozone denitration technology is added between a bag-type dust collector and a fan, the reaction time is not less than 1-1.5S, the flue gas temperature is about 100 ℃, and the operation cost of the ozone denitration is only the power consumption of the ozone equipment and the consumption of a small amount of liquid oxygen;
    selecting a rated ozone concentration of 148mg/L by a 5kg/h ozone generator according to the economic operation principle of system equipment, and supplying oxygen to a liquid oxygen tank of an air source system; the output adjusting range of the ozone generator can realize linear adjustment, the adjustment correlation is realized by adopting a mode of adjusting power and air quantity simultaneously, and the cooling is related by adopting a plate heat exchanger cooling circulation; the system is related in a PLC control mode;
    oxygen enters an ozone generator; the air inlet pipeline of the ozone generator is provided with a pressure reducing valve for stabilizing the working pressure of the ozone generating chamber; oxygen inside the ozone generating chamber is changed into ozone through medium-frequency high-voltage discharge, and product gas is generated through an ozone gas outlet after temperature, pressure and flow monitoring and regulation; the ozone generating chamber is provided with an ozone gas taking port, and the outlet concentration of the ozone generator is monitored on line through an ozone concentration detector equipped on the ozone generator;
    the ozone generation system is provided with closed-loop circulating cooling water systems which exchange heat through a plate heat exchanger and provide cooling water for the ozone generator, wherein the closed-loop circulating cooling water systems comprise plate heat exchangers, circulating water pumps, expansion tanks and valves which are related, a flow switch and a temperature transmitter are arranged on a cooling water outlet pipeline of the ozone generator, and an alarm is given when the flow rate of cooling water is insufficient and the temperature exceeds a set value;
    an ozone/oxygen leakage alarm instrument is installed in the ozone preparation room, and when the ozone/oxygen leakage in the environment in the preparation room exceeds the standard, the system determines to output an alarm, start an exhaust fan or stop the machine according to a detection signal;
    in order to remove nitrogen oxides in the flue gas, ozone is added between the back of the bag-type dust collector and the main fan to remove organic odor in the flue gas and fully react with the NOx in the flue gas, so that the aim of denitration is fulfilled;
    along with the continuous supplement of the circulating spray liquid, the circulating spray liquid with higher temperature in the spray tower is continuously replaced, so that the temperature and the salinity of the circulating spray liquid in the spray tower reach dynamic balances;
    an th spray tower is separately provided with a fresh water supplement port with DN50 pipe diameter, and fresh cooling water is used for supplement, thereby ensuring the quality of spray circulating liquid in the spray tower under special conditions;
    denitration treatment:
    before the cloth bag flue gas enters the absorption tower, strong oxidant (ozone) generated by an ozone generation system is adopted to forcibly oxidize NOx in the flue gas, so that the NOx is converted into high-valence nitrogen oxide (N2O5) which is easily dissolved in water, and the oxidized high-valence nitrogen oxide enters the absorption tower along with the flue gas; dissolving in water in an absorption tower to produce nitric acid, and performing neutralization reaction with a sodium hydroxide aqueous solution in circulating slurry in the absorption tower to generate sodium nitrate;
    and (3) desulfurization treatment:
    the slurry circulating pump sends the circulating slurry at the bottom of the tower to the absorption section spraying layer, and the slurry is used for absorbing sulfur dioxide and nitrogen oxide in the flue gas;
    system raw material medium supply:
    supplying an absorbent, namely a flue gas dedusting, desulfurization and denitrification system adopts 30 percent by weight of sodium hydroxide aqueous solution as a desulfurization absorbent, sending the 30 percent by weight of sodium hydroxide aqueous solution outside a boundary area to a flue gas dedusting, desulfurization and denitrification facility, wherein the process of absorbing sulfur dioxide and nitric oxide in flue gas by using the 30 percent by weight of sodium hydroxide aqueous solution is acid-base neutralization reactions, and the 30 percent by weight of sodium hydroxide aqueous solution is continuously supplemented into the slurry of an absorption tower in order to keep the pH value of circulating slurry in the absorption tower to meet the requirement of absorbing sulfur dioxide and nitric oxide in the flue gas;
    the technical requirements are as follows:
    the flue gas pipeline from the cloth bag to the spray tower is 2205, , and the connecting pipeline of the second spray tower and the third spray tower is FRP;
    the tower body is made of: the material of the cylindrical high-temperature-resistant resin glass fiber wound pipe fitting is FRP;
    the water pump adopts mechanical seal and steel lining plastic;
    valve is made of steel-lined PE;
    SNCR denitration technology:
    the original concentration value of the nitrogen oxides in the flue gas is 300mg/m by analyzing the sludge materials and referring to detection data of other items of my department3(ii) a The SNCR denitration adopts urea as a reducing agent; 36000Nm according to smoke amount3Calculating the consumption amount of the urea to be 10kg/h, diluting and spraying according to 10% of urea solution, wherein the pumping amount of the urea solution is 100 kg/h;
    the SNCR denitration adopts an optimization process, multi-point injection is carried out at a high-temperature section of a secondary combustion chamber, and the temperature of the high-temperature section of the secondary combustion chamber is above 850 ℃; according to the temperature in the furnace, corresponding nozzles are respectively arranged for accurate injection; respectively spraying 10% urea solution into the two combustion chambers according to the number of nozzles and the temperature proportion, reducing nitrogen oxides in the flue gas into harmless nitrogen and water, and calculating the denitration efficiency according to 80%;
    the SNCR denitration principle is that reducing agents such as ammonia water and urea are sprayed into an area with the temperature of 850-1100 ℃, and the reducing agents are rapidly thermally decomposed into NH3And with flue gasesNO in (1)XReaction is carried out to generate N2And H2O; the SNCR process reactor is a high-temperature area of an incinerator;
    the reaction formula is as follows: 2NO + CO (NH)3)2+1/2O2→2N2+CO2+2H2O;
    Based on the original NOx content of 95%, the NO discharge capacity is 10.3kg/h, the high-valence nitrogen oxide is 0.5kg/h, and the high-valence nitrogen oxide can be removed in the subsequent deacidification process; 80% NO can be removed in the SNCR process, the urea consumption is 10.3kg/h considering that the urea loss rate is 20%, and the urea solution dosage is about 100kg/h when 10% urea solution is prepared; adopts multi-point injection, uniform feeding and atomized injection to achieve the best contact effect to enable NO to be sprayedXThe outlet concentration reaches and is superior to the European Union standard requirement;
    wherein the de-whitening system and the chimney system in the step (tenth ):
    the system is provided with a stainless steel heat exchanger, and the heat exchanger separates flue gas from ambient air through a specially-made metal heat exchange plate;
    the saturated flue gas desulfurized by the wet method passes through the metal plate heat exchanger from top to bottom, the ambient air is extracted by the ambient air fan and enters the heat exchanger from the side edge of the metal plate heat exchanger, and the flue gas and ambient dry air perform gas-gas indirect heat exchange through the metal heat exchange plate from bottom to top, so that the temperature is reduced, a large amount of moisture is condensed to reduce the humidity of the flue gas, and the whitening effect of the stage is achieved;
    the process principle is as follows: the saturated flue gas which is desulfurized by the wet method passes through the HINO-PILE plate heat exchanger from bottom to top, performing gas-gas indirect heat exchange with ambient dry air, condensing out a large amount of water, wherein the condensed water accounts for 15-30% of the total water in the flue gas, meanwhile, a large amount of heat energy is released when the moisture of the tail gas is condensed to heat the ambient dry air blown into the heat exchanger so as to increase the temperature of the ambient dry air, then the heated dry air is introduced into a chimney by an air pipe to be mixed with the flue gas after temperature reduction and dehydration, so that the humidity of the mixed flue gas is greatly reduced, the dew point temperature of the exhausted smoke is reduced, the temperature difference between the temperature (T) of the smoke at the main exhaust port and the saturation temperature (T') under the humidity condition is more than or equal to 10 ℃, so that the exhausted smoke does not reach the dew point temperature in a short time after being exhausted, and the moisture in the smoke is not condensed into water mist, thereby achieving the purpose of reducing the white smoke;
    the device is provided with an environmental air fan, a variable frequency motor is adopted for frequency conversion regulation, the air quantity of the fan is full load air quantity of the device, the temperature of environmental air and the humidity of atmosphere can change along with the change of climate, and the optimal whitening visual effect can be achieved by artificially regulating the level of frequency conversion power according to the change of external factors and the whitening visual effect of smoke when in use;
    the chimney is provided with an inner barrel and an outer barrel which are mutually separated, an online monitoring system is arranged above the inner barrel, and the online monitoring maintenance and repair are facilitated through a steel platform arranged outside the chimney;
    the flue gas after heat exchange enters an inner cylinder of the chimney, and the environmental wind enters an outer cylinder of the chimney, so that the flue gas entering the inner cylinder can be monitored in real time by on-line monitoring, and the influence of the environmental wind is avoided;
    the heated dry air is mixed with the cooled and dehydrated smoke at the outlet of the inner barrel, so that the humidity of the mixed smoke is greatly reduced, the dew point temperature of the evacuated smoke is reduced, the evacuated smoke cannot reach the dew point temperature in a short time after being discharged, and the moisture in the smoke cannot be condensed into water mist, so that the aim of reducing white smoke is fulfilled;
    the environment air fan that the device was equipped with adopts inverter motor to carry out the frequency conversion regulation and control, and the amount of wind of fan is the device full load amount of wind, and along with the change of weather, the temperature of ambient air and atmospheric humidity all can change, can take off white visual effect according to the change and the flue gas of these external factors during the use, through the height of artificial regulation frequency conversion power to reach the best visual effect that takes off white.
CN201911006919.0A 2019-10-22 2019-10-22 Operation method of industrial solid waste and sludge rotary kiln co-processing integrated device Pending CN110734209A (en)

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CN111514694A (en) * 2020-04-29 2020-08-11 中国建材国际工程集团有限公司 Glass flue gas recovery method
CN111573885A (en) * 2020-05-07 2020-08-25 四川省工业环境监测研究院 Method and device for treating ammonia nitrogen in coking wastewater by resin adsorption method
CN111536533A (en) * 2020-05-20 2020-08-14 浙江裕峰环境服务股份有限公司 Incineration sludge treatment process and equipment thereof
CN113024056A (en) * 2021-03-16 2021-06-25 山东驰盛新能源设备有限公司 Rotational flow heat vibration drying machine and rotational flow heat vibration drying system
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