CN204122439U - For the city garbage burning flying ash resource pretreatment system of cement producting material - Google Patents
For the city garbage burning flying ash resource pretreatment system of cement producting material Download PDFInfo
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- CN204122439U CN204122439U CN201420425244.XU CN201420425244U CN204122439U CN 204122439 U CN204122439 U CN 204122439U CN 201420425244 U CN201420425244 U CN 201420425244U CN 204122439 U CN204122439 U CN 204122439U
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- 239000000463 material Substances 0.000 title claims abstract description 17
- 239000004568 cement Substances 0.000 title claims abstract description 15
- 239000010813 municipal solid waste Substances 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 149
- 238000006243 chemical reaction Methods 0.000 claims abstract description 100
- 239000000428 dust Substances 0.000 claims abstract description 65
- 239000002912 waste gas Substances 0.000 claims abstract description 36
- 238000001914 filtration Methods 0.000 claims abstract description 35
- 238000002425 crystallisation Methods 0.000 claims abstract description 24
- 230000008025 crystallization Effects 0.000 claims abstract description 24
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 24
- 238000000746 purification Methods 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims description 33
- 238000011001 backwashing Methods 0.000 claims description 28
- 239000000706 filtrate Substances 0.000 claims description 26
- 239000012452 mother liquor Substances 0.000 claims description 26
- 239000010802 sludge Substances 0.000 claims description 25
- 239000006228 supernatant Substances 0.000 claims description 21
- 238000001704 evaporation Methods 0.000 claims description 19
- 230000008020 evaporation Effects 0.000 claims description 19
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 238000004062 sedimentation Methods 0.000 claims description 17
- 238000006386 neutralization reaction Methods 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 16
- 239000003814 drug Substances 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 11
- 238000001035 drying Methods 0.000 claims description 10
- 239000013078 crystal Substances 0.000 claims description 9
- 238000001556 precipitation Methods 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 7
- 239000011268 mixed slurry Substances 0.000 claims description 7
- 239000013049 sediment Substances 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- 239000000376 reactant Substances 0.000 claims description 6
- 239000008399 tap water Substances 0.000 claims description 6
- 235000020679 tap water Nutrition 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 5
- 150000003839 salts Chemical class 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000006004 Quartz sand Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 13
- 239000010881 fly ash Substances 0.000 description 10
- 230000018044 dehydration Effects 0.000 description 8
- 238000006297 dehydration reaction Methods 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
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- 239000002920 hazardous waste Substances 0.000 description 2
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 2
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- 229910052708 sodium Inorganic materials 0.000 description 2
- 230000002195 synergetic effect Effects 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
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Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a kind of city garbage burning flying ash resource pretreatment system for cement producting material, comprise flying dust feeder unit, flying dust hybrid reaction unit, exhaust purification unit connection, heavy metal removing reaction member, filter turbidity removal unit, evaporative crystallization unit and dehydrate unit; Described flying dust feeder unit is connected with described flying dust hybrid reaction unit by belt conveyor, described flying dust hybrid reaction unit is connected with described heavy metal removing reaction member by pipeline, described heavy metal removing reaction member is connected with described filtration turbidity removal unit by pipeline, described filtration turbidity removal unit is connected with described evaporative crystallization unit by pipeline, and described evaporative crystallization unit is connected with the described unit that dehydrates by pipeline.Discarded object is converted into resource by system provided by the utility model, realizes water circulation use in system, without waste water and gas discharge, reclaims Nacl simultaneously.
Description
Technical field
The utility model relates to a kind of city garbage burning flying ash resource pretreatment system for cement producting material.
Background technology
Along with the continuous propelling of urbanization process, population size is increasing, and Output of Domestic Waste increases severely, limited due to urban land, burns a kind of effective ways becoming Disposal of Domestic.Rubbish can produce a large amount of flying dusts in burning process, and its generation accounts for into stove quantity of refuse 2 ~ 5%.Containing silica, aluminium oxide, chloride, heavy metal, bioxin etc. in incineration of refuse flyash, it is the hazardous waste of national Specification, cannot in entered environment without specific method of disposal process, therefore, the timely safe disposal of incineration of refuse flyash becomes a very important task.
Existing incineration of refuse flyash disposal technology all cannot carry out recycling to flying dust as cement solidification method, pharmaceutical treatment etc., there is Environmental Risk, and needs larger floor space.
Our national policy fully utilizes hazardous waste under encouraging to meet relevant criterion prerequisite, incineration of refuse flyash can according to " cement kiln synergic processing solid waste pollution control criterion " (GB30485-2013) requirement, utilize cement kiln synergic processing mode to fully utilize, therefore incineration of refuse flyash can as a kind of raw material of manufacture of cement.But incineration of refuse flyash can not directly as producing the raw material of cement, the principal element that restriction incineration of refuse flyash directly enters cement kiln is chlorinty wherein.The systems approach developing a kind of chlorinty reduced in incineration of refuse flyash not only can make incineration of refuse flyash recycling, can reclaim wherein valuable component simultaneously.
Summary of the invention
In order to overcome exist in conventional garbage flying ash disposal technology cannot carry out larger etc. the shortcoming of the large and floor space of recycling, Environmental Risk to flying dust, the utility model provides a kind of city garbage burning flying ash resource pretreatment system for cement producting material.
The technical solution adopted in the utility model is:
For the city garbage burning flying ash resource pretreatment system of cement producting material, it is characterized in that: comprise incinerator ash and fly treatment system, exhaust purification unit, water treatment and reclaiming system, described incinerator ash flies treatment system and is connected with exhaust purification unit, water treatment and reclaiming system respectively;
Described incinerator ash flies treatment system and comprises flying dust feeder unit and flying dust hybrid reaction unit, and described flying dust feeder unit is connected with described exhaust purification unit respectively with flying dust hybrid reaction unit; Described water treatment and reclaiming system comprise heavy metal removing reaction member, filter turbidity removal unit, evaporative crystallization unit and dehydrate unit;
Described flying dust feeder unit is connected with described flying dust hybrid reaction unit by belt conveyor, described flying dust hybrid reaction unit is connected with described heavy metal removing reaction member by pipeline, described heavy metal removing reaction member is connected with described filtration turbidity removal unit by pipeline, described filtration turbidity removal unit is connected with described evaporative crystallization unit by pipeline, and described evaporative crystallization unit is connected with the described unit that dehydrates by pipeline.
Further, described flying dust feeder unit comprises flying dust storehouse, batcher and belt conveyor, the outlet in described flying dust storehouse is connected with the entrance of batcher by valve, described batcher is provided with the first outlet and the second outlet, the first described outlet is connected with the entrance of described belt conveyor, and the second described outlet is connected with described exhaust purification unit by pipeline; The outlet of described belt conveyor is connected with described flying dust hybrid reaction unit.
Further, described flying dust hybrid reaction unit comprises hybrid reaction tank, first sludge pump, first plate and frame filter press, mechanical agitator is provided with in described hybrid reaction tank, the top of described hybrid reaction tank is provided with the removable cover preventing mixed process waste gas from escaping, the top of described hybrid reaction tank is provided with tap water inlets, sediment entrance, condensing water inlet, first backwashing water entrance and waste gas outlet, described waste gas outlet is connected with described exhaust purification unit, described tap water inlets is connected with running water pipe, described sediment porch is provided with removable cover, described condensing water inlet is connected with the condensation-water drain on described evaporative crystallization unit by pipeline, the first described backwashing water entrance to be exported with the backwashing water on described filtration turbidity removal unit by pipeline and is connected, the bottom of described hybrid reaction tank is provided with mixed slurry outlet, described mixed slurry outlet is connected with the first described sludge pump by pipeline, the first described sludge pump is connected by the entrance of pipeline with the first described plate and frame filter press, and the filtrate (liquid of the first described plate and frame filter press is connected by the filtrate inlet of pipeline with described heavy metal removing reaction member.
Further, described heavy metal removing reaction member comprises reaction tank, sedimentation basin, neutralization pond, the second sludge pump, the second plate and frame filter press; Described reaction tank is provided with the outlet of filtrate inlet, 3 medicament entrances and reactant liquor, the medicament entrance described in 3 is connected with dosing pump, medicament storage tank respectively by pipeline, and described reactant liquor outlet is connected by the entrance of pipeline with described sedimentation basin; Described sedimentation basin is provided with supernatant outlet and precipitation outlet, described supernatant outlet is connected by the entrance of pipeline with described neutralization pond, described precipitation outlet is connected with the second described sludge pump by pipeline, the second described sludge pump is connected by the entrance of pipeline with the second plate and frame filter press, and the filtrate (liquid of the second described plate and frame filter press is connected by the filtrate inlet of pipeline with described reaction tank; Described neutralization pond is provided with supernatant entrance, medicament entrance and in and water out, described supernatant entrance to be exported with the supernatant of described sedimentation basin by pipeline and is connected, described medicament entrance is connected with dosing pump, salt acid storage tank by pipeline, is connected in described with water out by pipeline with described filtration turbidity removal unit.The muddy water containing body refuse that reaction tank produces precipitates in sedimentation basin, and the mud precipitated feeds the first plate and frame filter press dehydration by sludge pump, and the supernatant after precipitation enters neutralization pond, by hydrochloric acid, supernatant pH value is adjusted to 7 ~ 8.
Further, described filtration turbidity removal unit comprises elevator pump, fast filtering pond, accurate filter and collecting-tank, described elevator pump with described in and water out be connected by pipeline, during described fast filtering pond is provided with and water inlet, the second backwashing water entrance, filtering water outlet and backwashing water outlet; Be connected with described elevator pump by pipeline with water inlet in described, the second described backwashing water entrance is connected with backwashing water delivery side of pump by pipeline, and the entrance of backwash pump is connected with described collecting-tank by pipeline; Described filtering water outlet is connected by the entrance of pipeline with described accurate filter; Described backwashing water outlet is connected with the first described backwashing water entrance by pipeline, and the outlet of described accurate filter is connected with described collecting-tank by pipeline; Described collecting-tank is provided with backwash water outlet and evaporation water out, described backwash water outlet is connected with described backwash pump by pipeline, and described evaporation water out is connected with described elevator pump, described evaporative crystallization unit respectively by pipeline.
Further, described evaporative crystallization unit comprises preheater, evaporimeter and crystallizer, export and steam-condensation water out after described preheater being provided with the first entrance, the second entrance, evaporation water preheat, the first described entrance is connected with water out with the evaporation on described collecting-tank by pipeline, water pump successively, and the second described entrance is connected by the steam (vapor) outlet of pipeline with described evaporimeter; Described evaporation is connected with the entrance of evaporimeter by pipeline with exporting after water preheat, and described steam-condensation water out is connected by the condensing water inlet of pipeline with the hybrid reaction tank with described flying dust hybrid reaction unit; Described evaporimeter is provided with raw steam inlet, preheating water entrance, mother liquor entrance, magma entrance, steam (vapor) outlet and high-temperature water outlet; Described raw steam inlet is connected with central heating jet chimney by pipeline; Described preheating water entrance is connected with exporting after water preheat with described evaporation by pipeline; Described mother liquor entrance is connected with the described unit that dehydrates by pipeline; Described magma entrance is connected with described crystallizer by pipeline; Described steam (vapor) outlet is connected with the second entrance of described preheater by pipeline; Described high-temperature water outlet is connected by the entrance of pipeline with described crystallizer; Described crystallizer is provided with 2 outlets, is connected with the magma entrance of described evaporimeter, the described unit that dehydrates respectively.
Further, the described unit that dehydrates comprises dewatering centrifuge, mother liquor tank and drying machine, described dewatering centrifuge is provided with mother liquor outlet and crystal outlet; Described mother liquor outlet is connected with described mother liquor tank by pipeline; Described crystal outlet is connected by the entrance of belt conveyor with described drying machine; The outlet of described mother liquor tank is connected with pump entrance by pipeline, and exit of pump is connected with the mother liquor entrance of described evaporimeter.
Further, described exhaust purification unit comprises air-introduced machine, waste gas absorption tower and water circulating pump, and the entrance of described air-introduced machine is connected with the waste gas outlet of the batcher on the waste gas outlet of the hybrid reaction tank on flying dust hybrid reaction unit and flying dust feeder unit respectively by pipeline; The bottom of described waste gas absorption tower is provided with absorbing liquid storage tank; Described waste gas absorption tower is provided with exhaust gas entrance, absorbing liquid entrance, offgas outlet and absorbing liquid outlet, described exhaust gas entrance is positioned at the ullage of absorbing liquid storage tank and is connected by the outlet of pipeline with described air-introduced machine; Described absorbing liquid entrance is positioned at the bottom of absorbing liquid storage tank and is connected by the entrance of pipeline with described water circulating pump; Described offgas outlet is positioned at the top of waste gas absorption tower and is communicated with air; Described absorbing liquid outlet is positioned at the top of waste gas absorption tower and is connected with described recirculated water delivery side of pump by pipeline; Described recirculated water delivery side of pump is exported with described absorbing liquid respectively by pipeline, the filtrate inlet of reaction tank on heavy metal removing reaction member is connected.
Further, the filtrate in described fast filtering pond is the quartz sand of particle diameter 1 ~ 12mm, and the filter medium of described accurate filter is the filter core of 5 ~ 10 μm.
Further, described dewatering centrifuge is two-level piston material pushing centrifugal machine or Horizental centrifugal force material discharging centrifuge, and drying machine is vacuum drier or band drier.
Further, described hybrid reaction tank is circular tank, and volume is 20 ~ 80m
3, the power of mechanical agitator is 7.5 ~ 22kW, and tank body material is carbon steel or stainless steel.
The beneficial effects of the utility model are embodied in:
(1) in flying dust feeder unit and flying dust hybrid reaction unit, be provided with dust, gas sampling pipeline by exhaust purification unit process, avoid exhaust emission.
(2) flying dust mixed cell have employed hybrid reaction tank and the first plate and frame filter press, and the chlorinity in the flying dust after washing can be reduced to less than 0.4%, has effectively ensured the material quality entering cement kiln.
By heavy metal removing reaction member, filter turbidity removal unit, evaporative crystallization unit, dehydrate the efficient combination process of unit, achieve recycling of water, not only ensure each unit and normally run, and can Nacl be reclaimed.
(4) the equipment adopted in system is common apparatus on market, and assembling builds convenient.
(5) whole system closed operation, without waste water and gas discharge, non-environmental-pollution problem.
Accompanying drawing explanation
Fig. 1 is city garbage burning flying ash resource pretreatment system block diagram.
Fig. 2 is the device connection diagram of flying dust feeder unit, flying dust hybrid reaction unit.
Fig. 3 is heavy metal removing reaction member, filter turbidity removal unit, evaporative crystallization unit, dehydrate the device connection diagram of unit.
Fig. 4 is the device connection diagram of exhaust purification unit.
Detailed description of the invention
Referring to figs. 1 through Fig. 4, for the city garbage burning flying ash resource pretreatment system of cement producting material, comprise incinerator ash and fly treatment system, exhaust purification unit G, water treatment and reclaiming system, described incinerator ash flies treatment system and is connected with exhaust purification unit, water treatment and reclaiming system respectively;
Described incinerator ash flies treatment system and comprises flying dust feeder unit A and flying dust hybrid reaction unit B, and described flying dust feeder unit A is connected with described exhaust purification unit G respectively with flying dust hybrid reaction unit B; Described water treatment and reclaiming system comprise heavy metal removing reaction member C, filter turbidity removal cells D, evaporative crystallization unit E and dehydrate unit F;
Described flying dust feeder unit A is connected with described flying dust hybrid reaction unit B by belt conveyor 3, described flying dust hybrid reaction unit B is connected with described heavy metal removing reaction member C by pipeline, described heavy metal removing reaction member C is connected with described filtration turbidity removal cells D by pipeline, described filtration turbidity removal cells D is connected with described evaporative crystallization unit E by pipeline, and described evaporative crystallization unit E is connected with the described unit F that dehydrates by pipeline.
Further, described flying dust feeder unit A comprises flying dust storehouse 1, batcher 2 and belt conveyor 3, the outlet in described flying dust storehouse 1 is connected by the entrance of valve with batcher 2, described batcher 2 is provided with the first outlet and the second outlet, the first described outlet is connected with the entrance of described belt conveyor 3, and the second described outlet is connected with described exhaust purification unit G by pipeline; The outlet of described belt conveyor 3 is connected with described flying dust hybrid reaction unit B.
Further, described flying dust hybrid reaction unit B comprises hybrid reaction tank 4, first sludge pump 5, first plate and frame filter press 6, mechanical agitator is provided with in described hybrid reaction tank, the top of described hybrid reaction tank is provided with the removable cover preventing mixed process waste gas from escaping, the top of described hybrid reaction tank is provided with tap water inlets, sediment entrance, condensing water inlet, first backwashing water entrance and waste gas outlet, described waste gas outlet is connected with described exhaust purification unit, described tap water inlets is connected with running water pipe, described sediment porch is provided with removable cover, described condensing water inlet is connected with the condensation-water drain on described evaporative crystallization unit by pipeline, the first described backwashing water entrance to be exported with the backwashing water on described filtration turbidity removal unit by pipeline and is connected, the bottom of described hybrid reaction tank is provided with mixed slurry outlet, described mixed slurry outlet is connected with the first described sludge pump by pipeline, the first described sludge pump is connected by the entrance of pipeline with the first described plate and frame filter press, and the filtrate (liquid of the first described plate and frame filter press is connected by the filtrate inlet of pipeline with described heavy metal removing reaction member.
Further, described heavy metal removing reaction C unit comprises reaction tank 7, sedimentation basin 8, neutralization pond 9, second sludge pump 10, second plate and frame filter press 11; Described reaction tank is provided with the outlet of filtrate inlet, 3 medicament entrances and reactant liquor, the medicament entrance described in 3 is connected with dosing pump, medicament storage tank respectively by pipeline, and described reactant liquor outlet is connected by the entrance of pipeline with described sedimentation basin; Described sedimentation basin is provided with supernatant outlet and precipitation outlet, described supernatant outlet is connected by the entrance of pipeline with described neutralization pond, described precipitation outlet is connected with the second described sludge pump by pipeline, the second described sludge pump is connected by the entrance of pipeline with the second plate and frame filter press, and the filtrate (liquid of the second described plate and frame filter press is connected by the filtrate inlet of pipeline with described reaction tank; Described neutralization pond is provided with supernatant entrance, medicament entrance and in and water out, described supernatant entrance to be exported with the supernatant of described sedimentation basin by pipeline and is connected, described medicament entrance is connected with dosing pump, salt acid storage tank by pipeline, is connected in described with water out by pipeline with described filtration turbidity removal unit.The muddy water containing body refuse that reaction tank produces precipitates in sedimentation basin, and the mud precipitated feeds the first plate and frame filter press dehydration by sludge pump, and the supernatant after precipitation enters neutralization pond, by hydrochloric acid, supernatant pH value is adjusted to 7 ~ 8.
Further, described filtration turbidity removal cells D comprises elevator pump 12, fast filtering pond 13, accurate filter 14 and collecting-tank 15, described elevator pump with described in and water out be connected by pipeline, during described fast filtering pond is provided with and water inlet, the second backwashing water entrance, filtering water outlet and backwashing water outlet; Be connected with described elevator pump by pipeline with water inlet in described, the second described backwashing water entrance is connected with backwashing water delivery side of pump by pipeline, and the entrance of backwash pump is connected with described collecting-tank by pipeline; Described filtering water outlet is connected by the entrance of pipeline with described accurate filter; Described backwashing water outlet is connected with the first described backwashing water entrance by pipeline, and the outlet of described accurate filter is connected with described collecting-tank by pipeline; Described collecting-tank is provided with backwash water outlet and evaporation water out, described backwash water outlet is connected with described backwash pump by pipeline, and described evaporation water out is connected with described elevator pump, described evaporative crystallization unit respectively by pipeline.
Further, described evaporative crystallization unit E comprises preheater 16, evaporimeter 17 and crystallizer 18, export and steam-condensation water out after described preheater being provided with the first entrance, the second entrance, evaporation water preheat, the first described entrance is connected with water out with the evaporation on described collecting-tank by pipeline, water pump successively, and the second described entrance is connected by the steam (vapor) outlet of pipeline with described evaporimeter; Described evaporation is connected with the entrance of evaporimeter by pipeline with exporting after water preheat, and described steam-condensation water out is connected by the condensing water inlet of pipeline with the hybrid reaction tank with described flying dust hybrid reaction unit; Described evaporimeter is provided with raw steam inlet, preheating water entrance, mother liquor entrance, magma entrance, steam (vapor) outlet and high-temperature water outlet; Described raw steam inlet is connected with central heating jet chimney by pipeline; Described preheating water entrance is connected with exporting after water preheat with described evaporation by pipeline; Described mother liquor entrance is connected with the described unit that dehydrates by pipeline; Described magma entrance is connected with described crystallizer by pipeline; Described steam (vapor) outlet is connected with the second entrance of described preheater by pipeline; Described high-temperature water outlet is connected by the entrance of pipeline with described crystallizer; Described crystallizer is provided with 2 outlets, is connected with the magma entrance of described evaporimeter, the described unit that dehydrates respectively.
Further, the described unit F that dehydrates comprises dewatering centrifuge 19, mother liquor tank 20 and drying machine 21, described dewatering centrifuge is provided with mother liquor outlet and crystal outlet; Described mother liquor outlet is connected with described mother liquor tank by pipeline; Described crystal outlet is connected by the entrance of belt conveyor with described drying machine; The outlet of described mother liquor tank is connected with pump entrance by pipeline, and exit of pump is connected with the mother liquor entrance of described evaporimeter.
Further, described exhaust purification unit G comprises air-introduced machine 22, waste gas absorption tower 23 and water circulating pump 24, and the entrance of described air-introduced machine is connected with the waste gas outlet of the batcher on the waste gas outlet of the hybrid reaction tank on flying dust hybrid reaction unit and flying dust feeder unit respectively by pipeline; The bottom of described waste gas absorption tower is provided with absorbing liquid storage tank; Described waste gas absorption tower is provided with exhaust gas entrance, absorbing liquid entrance, offgas outlet and absorbing liquid outlet, described exhaust gas entrance is positioned at the ullage of absorbing liquid storage tank and is connected by the outlet of pipeline with described air-introduced machine; Described absorbing liquid entrance is positioned at the bottom of absorbing liquid storage tank and is connected by the entrance of pipeline with described water circulating pump; Described offgas outlet is positioned at the top of waste gas absorption tower and is communicated with air; Described absorbing liquid outlet is positioned at the top of waste gas absorption tower and is connected with described recirculated water delivery side of pump by pipeline; Described recirculated water delivery side of pump is exported with described absorbing liquid respectively by pipeline, the filtrate inlet of reaction tank on heavy metal removing reaction member is connected.
Further, the filtrate in described fast filtering pond is the quartz sand of particle diameter 1 ~ 12mm, and the filter medium of described accurate filter is the filter core of 5 ~ 10 μm.
Hybrid reaction tank used in such scheme, reaction tank, neutralization pond, sedimentation basin, collecting-tank all adopt carbon steel or stainless steel, and salt acid storage tank, waste gas absorption tower all adopt PVC or glass steel material; Preheater, evaporimeter, crystallizer all adopt stainless steel; Hybrid reaction tank volume is 20 ~ 80m
3, agitator power is 7.5 ~ 22kW; Sludge pump adopts screw pump, and elevator pump and circulating pump adopt centrifugal pump, and compound pump adopts corrosion-resistant measuring pump; Dewatering centrifuge is two-level piston material pushing centrifugal machine or Horizental centrifugal force material discharging centrifuge, and drying machine is vacuum drier or band drier.
Except the requirement of above-mentioned embodiment, the various equipment adopted in the utility model system all do not limit by above-mentioned specification and quantity.
Operation principle of the present utility model is as follows:
Incineration of refuse flyash autofeed enters hybrid reaction tank 4, then water (comprising condensed water, backwashing water, running water) is added according to water and flying dust weight ratio 1.5:1 ~ 5:1, after stirring 30 ~ 60min by mechanical agitator, form mixed slurry, slurry is connected with the first sludge pump 5 through the outlet conduit of hybrid reaction pot bottom, then be connected with the first plate and frame filter press 6, the mud after dehydration is qualified flying dust, and the filtrate of the first plate and frame filter press is then from flowing into reaction tank 7; Filtrate reacts with chemical agent under agitator effect, reaction time is 30 ~ 60min, the chemical agent added is vulcanized sodium, ferrous sulfate, aluminium polychloride, and filtrate needs per ton adds 20 ~ 120g vulcanized sodium, 60 ~ 300g ferrous sulfate, 100 ~ 500g aluminium polychloride; After reaction, mixed liquor is from flowing into sedimentation basin 8, sedimentation time is 120min, after precipitation, mixed liquor is divided into precipitating sludge and supernatant, wherein supernatant is from flowing into neutralization pond 9, precipitating sludge is transported to the second plate and frame filter press 11 by outlet at bottom by the second sludge pump 10 and dewaters, sediment after dehydration turns back to hybrid reaction tank 4, and the filtrate after dehydration is from flowing into neutralization pond 9; Filtrate under agitator effect with hydrochloric acid generation neutralization reaction, reaction pH control 7 ~ 8, the reaction time is 30 ~ 60min; Water after neutralization feeds fast filtering pond 13 by elevator pump 12, filters and removes particle residual in water, and after filtration is saturated, the particle that filter medium retains by unlatching backwash pump is gone out, and recovers the filter capacity in fast filtering pond 13; Again further by thinner particle residual in accurate filter 14 filtered water, water outlet is from flowing into collecting-tank 15 stored for future use; Water in collecting-tank 15 enters preheater 16 by elevator pump, and simultaneously evaporimeter 17 evaporates the steam produced and also enters preheater 16, and steam and water carry out indirect heat exchange in preheater again, and water can be warmed up to 60 ~ 80 DEG C, and steam then cools and becomes condensed water; Water after intensification heats and is converted to steam in evaporimeter 17, and wherein in water the concentration of salt progressively improve, and crystallization in crystallizer 18; The crystal of separating out is by the further centrifugal dehydration of dewatering centrifuge, and the mother liquor that dehydration produces turns back to evaporimeter by mother liquor tank elevator pump and evaporates further, and the crystal of dehydration then passes through the residual moisture of drying machine heating evaporation; Dried crystal is qualified Nacl, packing and storing; Batcher 2 and hybrid reaction tank 4 produce dust waste gas, after air-introduced machine 22 vacuumizes, dust waste gas enters waste gas absorption tower 23 and processes, after dust contacts with absorbing liquid is reverse, dust absorbed liquid can catch and dissolve in water, and absorbing liquid regularly can be drained in reaction tank 7 and process further.
Content described in this description embodiment is only enumerating the way of realization of inventive concept; protection domain of the present utility model should not be regarded as being only limitted to the concrete form that embodiment is stated, protection domain of the present utility model also and conceive the equivalent technologies means that can expect according to the utility model in those skilled in the art.
Claims (10)
1. for the city garbage burning flying ash resource pretreatment system of cement producting material, it is characterized in that: comprise incinerator ash and fly treatment system, exhaust purification unit, water treatment and reclaiming system, described incinerator ash flies treatment system and is connected with exhaust purification unit, water treatment and reclaiming system respectively;
Described incinerator ash flies treatment system and comprises flying dust feeder unit and flying dust hybrid reaction unit, and described flying dust feeder unit is connected with described exhaust purification unit respectively with flying dust hybrid reaction unit; Described water treatment and reclaiming system comprise heavy metal removing reaction member, filter turbidity removal unit, evaporative crystallization unit and dehydrate unit;
Described flying dust feeder unit is connected with described flying dust hybrid reaction unit by belt conveyor, described flying dust hybrid reaction unit is connected with described heavy metal removing reaction member by pipeline, described heavy metal removing reaction member is connected with described filtration turbidity removal unit by pipeline, described filtration turbidity removal unit is connected with described evaporative crystallization unit by pipeline, and described evaporative crystallization unit is connected with the described unit that dehydrates by pipeline.
2. pretreatment system as claimed in claim 1, it is characterized in that: described flying dust feeder unit comprises flying dust storehouse, batcher and belt conveyor, the outlet in described flying dust storehouse is connected with the entrance of batcher by valve, described batcher is provided with the first outlet and the second outlet, the first described outlet is connected with the entrance of described belt conveyor, and the second described outlet is connected with described exhaust purification unit by pipeline; The outlet of described belt conveyor is connected with described flying dust hybrid reaction unit.
3. pretreatment system as claimed in claim 2, it is characterized in that: described flying dust hybrid reaction unit comprises hybrid reaction tank, first sludge pump, first plate and frame filter press, mechanical agitator is provided with in described hybrid reaction tank, the top of described hybrid reaction tank is provided with the removable cover preventing mixed process waste gas from escaping, the top of described hybrid reaction tank is provided with tap water inlets, sediment entrance, condensing water inlet, first backwashing water entrance and waste gas outlet, described waste gas outlet is connected with described exhaust purification unit, described tap water inlets is connected with running water pipe, described sediment porch is provided with removable cover, described condensing water inlet is connected with the condensation-water drain on described evaporative crystallization unit by pipeline, the first described backwashing water entrance to be exported with the backwashing water on described filtration turbidity removal unit by pipeline and is connected, the bottom of described hybrid reaction tank is provided with mixed slurry outlet, described mixed slurry outlet is connected with the first described sludge pump by pipeline, the first described sludge pump is connected by the entrance of pipeline with the first described plate and frame filter press, and the filtrate (liquid of the first described plate and frame filter press is connected by the filtrate inlet of pipeline with described heavy metal removing reaction member.
4. pretreatment system as claimed in claim 3, is characterized in that: described heavy metal removing reaction member comprises reaction tank, sedimentation basin, neutralization pond, the second sludge pump, the second plate and frame filter press; Described reaction tank is provided with the outlet of filtrate inlet, 3 medicament entrances and reactant liquor, the medicament entrance described in 3 is connected with dosing pump, medicament storage tank respectively by pipeline, and described reactant liquor outlet is connected by the entrance of pipeline with described sedimentation basin; Described sedimentation basin is provided with supernatant outlet and precipitation outlet, described supernatant outlet is connected by the entrance of pipeline with described neutralization pond, described precipitation outlet is connected with the second described sludge pump by pipeline, the second described sludge pump is connected by the entrance of pipeline with the second plate and frame filter press, and the filtrate (liquid of the second described plate and frame filter press is connected by the filtrate inlet of pipeline with described reaction tank; Described neutralization pond is provided with supernatant entrance, medicament entrance and in and water out, described supernatant entrance to be exported with the supernatant of described sedimentation basin by pipeline and is connected, described medicament entrance is connected with dosing pump, salt acid storage tank by pipeline, is connected in described with water out by pipeline with described filtration turbidity removal unit.
5. pretreatment system as claimed in claim 4, it is characterized in that: described filtration turbidity removal unit comprises elevator pump, fast filtering pond, accurate filter and collecting-tank, described elevator pump with described in and water out be connected by pipeline, during described fast filtering pond is provided with and water inlet, the second backwashing water entrance, filtering water outlet and backwashing water outlet; Be connected with described elevator pump by pipeline with water inlet in described, the second described backwashing water entrance is connected with backwashing water delivery side of pump by pipeline, and the entrance of backwash pump is connected with described collecting-tank by pipeline; Described filtering water outlet is connected by the entrance of pipeline with described accurate filter; Described backwashing water outlet is connected with the first described backwashing water entrance by pipeline, and the outlet of described accurate filter is connected with described collecting-tank by pipeline; Described collecting-tank is provided with backwash water outlet and evaporation water out, described backwash water outlet is connected with described backwash pump by pipeline, and described evaporation water out is connected with described evaporative crystallization unit by pipeline.
6. pretreatment system as claimed in claim 5, it is characterized in that: described evaporative crystallization unit comprises preheater, evaporimeter and crystallizer, export and steam-condensation water out after described preheater being provided with the first entrance, the second entrance, evaporation water preheat, the first described entrance is connected with water out with the evaporation on described collecting-tank by pipeline, water pump successively, and the second described entrance is connected by the steam (vapor) outlet of pipeline with described evaporimeter; Described evaporation is connected with the entrance of evaporimeter by pipeline with exporting after water preheat, and described steam-condensation water out is connected by the condensing water inlet of pipeline with the hybrid reaction tank with described flying dust hybrid reaction unit; Described evaporimeter is provided with raw steam inlet, preheating water entrance, mother liquor entrance, magma entrance, steam (vapor) outlet and high-temperature water outlet; Described raw steam inlet is connected with central heating jet chimney by pipeline; Described preheating water entrance is connected with exporting after water preheat with described evaporation by pipeline; Described mother liquor entrance is connected with the described unit that dehydrates by pipeline; Described magma entrance is connected with described crystallizer by pipeline; Described steam (vapor) outlet is connected with the second entrance of described preheater by pipeline; Described high-temperature water outlet is connected by the entrance of pipeline with described crystallizer; Described crystallizer is provided with 2 outlets, is connected with the magma entrance of described evaporimeter, the described unit that dehydrates respectively.
7. pretreatment system as claimed in claim 6, is characterized in that: the described unit that dehydrates comprises dewatering centrifuge, mother liquor tank and drying machine, described dewatering centrifuge is provided with mother liquor outlet and crystal outlet; Described mother liquor outlet is connected with described mother liquor tank by pipeline; Described crystal outlet is connected by the entrance of belt conveyor with described drying machine; The outlet of described mother liquor tank is connected with pump entrance by pipeline, and exit of pump is connected with the mother liquor entrance of described evaporimeter.
8. pretreatment system as claimed in claim 7, it is characterized in that: described exhaust purification unit comprises air-introduced machine, waste gas absorption tower and water circulating pump, the entrance of described air-introduced machine is connected with the waste gas outlet of the batcher on the waste gas outlet of the hybrid reaction tank on flying dust hybrid reaction unit and flying dust feeder unit respectively by pipeline; The bottom of described waste gas absorption tower is provided with absorbing liquid storage tank; Described waste gas absorption tower is provided with exhaust gas entrance, absorbing liquid entrance, offgas outlet and absorbing liquid outlet, described exhaust gas entrance is positioned at the ullage of absorbing liquid storage tank and is connected by the outlet of pipeline with described air-introduced machine; Described absorbing liquid entrance is positioned at the bottom of absorbing liquid storage tank and is connected by the entrance of pipeline with described water circulating pump; Described offgas outlet is positioned at the top of waste gas absorption tower and is communicated with air; Described absorbing liquid outlet is positioned at the top of waste gas absorption tower and is connected with described recirculated water delivery side of pump by pipeline; Described recirculated water delivery side of pump is exported with described absorbing liquid respectively by pipeline, the filtrate inlet of reaction tank on heavy metal removing reaction member is connected.
9. pretreatment system as claimed in claim 8, is characterized in that: the filtrate in described fast filtering pond is the quartz sand of particle diameter 1 ~ 12mm, and the filter medium of described accurate filter is the filter core of 5 ~ 10 μm.
10. pretreatment system as claimed in claim 9, it is characterized in that: described dewatering centrifuge is two-level piston material pushing centrifugal machine or Horizental centrifugal force material discharging centrifuge, drying machine is vacuum drier or band drier.
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| CN201420425244.XU CN204122439U (en) | 2014-07-30 | 2014-07-30 | For the city garbage burning flying ash resource pretreatment system of cement producting material |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105478438A (en) * | 2015-01-29 | 2016-04-13 | 湖州森诺膜技术工程有限公司 | Method for synergistic treatment and harmless cyclic utilization of refuse fly ash by using cement kiln |
| CN105478449A (en) * | 2016-01-07 | 2016-04-13 | 浙江泰来环保科技有限公司 | Garbage incineration fly ash curing system |
| CN104803537B (en) * | 2015-05-11 | 2016-08-24 | 北京中科国润环保科技有限公司 | Incineration of refuse flyash washing softening process |
| CN108787700A (en) * | 2018-05-24 | 2018-11-13 | 湖南城市学院 | The method and apparatus of residue stabilization, sealing, stabilisation and removing toxic substances containing metal |
| CN111018376A (en) * | 2019-11-20 | 2020-04-17 | 浙江工业大学 | Household garbage incineration fly ash washing dechlorinating device and tail water discharging method |
| CN112775145A (en) * | 2020-12-22 | 2021-05-11 | 江山市虎鼎环保科技有限公司 | Efficient secondary washing process for household garbage incineration fly ash |
| CN115254923A (en) * | 2022-08-04 | 2022-11-01 | 江山市虎鼎环保科技有限公司 | Method for preparing high-purity calcium sulfate from waste incineration fly ash |
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2014
- 2014-07-30 CN CN201420425244.XU patent/CN204122439U/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105478438A (en) * | 2015-01-29 | 2016-04-13 | 湖州森诺膜技术工程有限公司 | Method for synergistic treatment and harmless cyclic utilization of refuse fly ash by using cement kiln |
| CN104803537B (en) * | 2015-05-11 | 2016-08-24 | 北京中科国润环保科技有限公司 | Incineration of refuse flyash washing softening process |
| CN105478449A (en) * | 2016-01-07 | 2016-04-13 | 浙江泰来环保科技有限公司 | Garbage incineration fly ash curing system |
| CN108787700A (en) * | 2018-05-24 | 2018-11-13 | 湖南城市学院 | The method and apparatus of residue stabilization, sealing, stabilisation and removing toxic substances containing metal |
| CN111018376A (en) * | 2019-11-20 | 2020-04-17 | 浙江工业大学 | Household garbage incineration fly ash washing dechlorinating device and tail water discharging method |
| CN112775145A (en) * | 2020-12-22 | 2021-05-11 | 江山市虎鼎环保科技有限公司 | Efficient secondary washing process for household garbage incineration fly ash |
| CN115254923A (en) * | 2022-08-04 | 2022-11-01 | 江山市虎鼎环保科技有限公司 | Method for preparing high-purity calcium sulfate from waste incineration fly ash |
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