CN202849212U - Rear earth metallurgy wastewater treatment device - Google Patents
Rear earth metallurgy wastewater treatment device Download PDFInfo
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- CN202849212U CN202849212U CN 201220536969 CN201220536969U CN202849212U CN 202849212 U CN202849212 U CN 202849212U CN 201220536969 CN201220536969 CN 201220536969 CN 201220536969 U CN201220536969 U CN 201220536969U CN 202849212 U CN202849212 U CN 202849212U
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Abstract
The utility model discloses a rear earth metallurgy wastewater treatment device. The rear earth metallurgy wastewater treatment device is combined with a flue gas desulfurization and denitrification device; the flue gas desulfurization and denitrification device comprises a main desulfurization and denitrification tower and an auxiliary desulfurization and denitrification tower; the rear earth metallurgy wastewater treatment device comprises an oil separator, an air flotation tank, a regulating tank, a neutralization reaction tank, an efficient thickener, a first-stage aerated sedimentation tank, a biological aerated filter, a break point chlorination reaction tower, a second-stage aerated sedimentation tank and a flocculation and sedimentation tank; the efficient thickener is connected with the auxiliary desulfurization and denitrification tower through a pipeline, and the first-stage aerated sedimentation tank is connected with the auxiliary desulfurization and denitrification tower through a pipeline; and the break point chlorination reaction tower is connected with the main desulfurization and denitrification tower through a pipeline, and the second-stage aerated sedimentation tank is connected with the main desulfurization and denitrification tower and connected with the flocculation and sedimentation tank through a pipeline. Heavy metal ions, COD (Chemical Oxygen Demand) and ammonia nitrogen in treated wastewater can reach the emission standard.
Description
Technical field
The utility model relates to technical field of waste water processing, relate in particular to a kind for the treatment of unit of rare earth metallurgy, the treatment unit of described rare earth metallurgy is applicable to process the soda soap method or calcium soap method rare-earth wet method is smelted the low factory effluent of ammonia quantity that produces in the production process, also is applicable to the processing of lower concentration ammonia-containing water in the ammonia saponification factory effluent.
Background technology
China's rare earth resources is abundant, approximately 8,800 ten thousand tons of rare earth resources reserves, and accounting for world's ratio is 30.7%, rare earth resources mainly is distributed in Sichuan, the Inner Mongol, Shandong, Guangdong, Jiangxi, Hunan, Fujian, Yunnan, zhejiang and other places.2005, China's rare-earth smelting product separation reached 10.39 ten thousand tons, accounts for more than 90% of world's aggregate demand.
Rare-earth smelting technique mainly contains two kinds of wet method and pyrogenic processes, and the hydrometallurgy extraction separation process adopts liquefied ammonia or ammoniacal liquor saponification in the past, does not enter product as saponifying agent, finally discharges with the ammonium chloride waste-water form.Because concentration is up to several ten thousand milligrams per liters, adopting ammonia distillation process, air stripping technique is that the resource recovery process of representative becomes the ammonia-containing water treatment process that numerous rare-earth smelting factory selects.The end of the year 2011, relevant ministries and commissions of country assign the rare-earth smelting industry and strictly limit and adopt liquefied ammonia or ammoniacal liquor as saponifying agent, adopt the less caustic soda of environmental pollution as saponifying agent, contain the ammonium ion decrease in the waste water of production discharging, basicly stable between 200-300PPM.Because ammonia quantity is lower, do not possess the value that resource reclaims.
The rare-earth wet method smelting wastewater adopts caustic soda as the technique of saponifying agent, saponification and other waste water mix by the factory effluent after oil removal by air bubbling, the chemical precipitation, its saltiness increases substantially than the ammonia saponification process, up to 2.5-3.5%, specific conductivity is up to 50000-70000 μ s/cm, COD150-300mg/L, ammonia nitrogen 200-300mg/L.Supersalinity, low organism, high-calcium ionic, high chloride ion characteristics are such wastewater treatment difficult points.Physicochemical techniques is mainly adopted at present such sewage disposal, mainly comprises: ion exchange method, evaporation concentration method, chemical precipitation method, break are thrown chlorine method, air stripping method, steam air lift method.
Ion exchange method adopts clinoptilolite that ammonia is had stronger adsorption selectivity, because loading capacity is limited, regeneration is complicated, mainly is applicable to the lower concentration ammonia-containing water and processes, and ammonia nitrogen can be up to standard, but COD can't be up to standard.The evaporation concentration method ammonia nitrogen rate of recovery is higher, and water outlet is easily up to standard, but energy consumption is high, and working cost is high, and equipment corrosion is large, invests higher.Chemical precipitation method generates the method for magnesium ammonium phosphate (struvite) for adding phosphoric acid or hydrophosphate and magnesium salts, subject matter is that processing cost is higher, the raw material supplying difficulty, and relatively poor to lower concentration ammonia-containing water removal effect, ammonia nitrogen and COD index can't qualified discharges.Break is thrown the chlorine method waste water is adjusted in about PH=7, presses Cl
-: NN
4 +=8:1 mainly is applicable to the lower concentration ammonia-containing water and processes, and ammonia nitrogen can be up to standard, but COD can't be up to standard.Physical chemistry method can not drop to ammonia nitrogen concentration enough low (below 100 mg/L), and biological denitrificaion can be suppressed because of high density free ammonia or nitrite nitrogen, adds that organism is lower, and saltiness is higher, and biological treatment seldom is used.But biological treatment processes that to have a cost low, effluent quality can be up to standard etc. advantage.
Enterprise generally adopts the oil removal pre-treatment at present, then adds the liming neutralization precipitation, the supernatant liquor discharging.The supporting wastewater flow rate of most of medium and small sized enterprises is at 500-1200m
3/ d is 65-200mg/L with the COD index of discharge of wastewater in 130-500mg/L, ammonia nitrogen index, all can't reach the emission request of " rare-earth industry pollutant emission standard ".
Most domestic adopts the original supporting air stripping of medium and small sized enterprises of Rare Earths smelting technology lower owing to containing ammonia concentration in the former water except ammonia tower (ammonia still), the clearance of ammonia is lower, energy consumption is high, add basic employing liming and carry out neutralizing treatment, fouling is serious, and the facility great majority all are in dead status.
In sum, the present most of rare-earth smelting enterprise of China is restricting the development of industry because wastewater treatment treatment technology level and working cost restriction are faced with severe environmental protection pressure.Forbid ammonia saponification process and after adopting the soda saponification process from country, the saltiness in the waste water rises, and ammonia quantity descends, and adopts traditional waste water treatment process can not satisfy environmental requirement, and surrounding enviroment are caused great pollution.
Therefore, prior art has yet to be improved and developed.
The utility model content
In view of above-mentioned the deficiencies in the prior art, the purpose of this utility model is to provide a kind for the treatment of unit of rare earth metallurgy, the treatment unit of described rare earth metallurgy is applicable to process the low saponification waste-water of ammonia quantity that produces in the rare-earth wet method smelting process, be intended to solve at present because rare-earth wet method smelting enterprise production technique is adjusted into saltiness increase and ammonia quantity minimizing in the saponification waste-water that causes behind the soda saponification process by the ammonia saponification process, and the supporting air stripping process facility of original sewage disposal, ammonia distillation process facility energy consumption is high, and ammonia resource recovery value is not high, causes the too high problem of system operation cost.
The technical solution of the utility model is as follows:
A kind for the treatment of unit of rare earth metallurgy, the treatment unit of described rare earth metallurgy combines with Dume desulfurizing denitrogenation appts, described Dume desulfurizing denitrogenation appts comprises that king-tower is denitrogenated in desulfurization and secondary tower is denitrogenated in desulfurization, desulfurization is denitrogenated king-tower and is denitrogenated secondary tower with desulfurization and link to each other by pipeline, wherein, described rare earth metallurgy treatment unit comprises: oil trap, air flotation pool, be used for rare earth metallurgy is carried out the equalizing tank of homogeneous, be used for and rare earth metallurgy in heavy metal and the neutralization reaction pond of acidic substance, be used for carrying out the Hhigh-efficient thickener of waste residue precipitation, be used for the sulfite ion of rare earth oxide smelting wastewater and the organic one-level aerated precipitation tank in the absorption rare earth metallurgy, be used for the organism to rare earth metallurgy, ammonia nitrogen adsorbs and the biological degradation BAF, be used for carrying out the break throwing chlorine reaction tower that break is thrown the ammonia nitrogen of chlorine reaction removal rare earth metallurgy, be used for the sulfite ion of rare earth oxide smelting wastewater and the organic secondary aerated precipitation tank in the absorption rare earth metallurgy, the flocculation sedimentation tank that is used for the body refuse of precipitating rare earth smelting wastewater;
Described oil trap, air flotation pool, equalizing tank, neutralization reaction pond, Hhigh-efficient thickener connect successively by pipeline; Described Hhigh-efficient thickener is denitrogenated secondary tower by pipeline with described desulfurization and is linked to each other, and described one-level aerated precipitation tank is denitrogenated secondary tower by pipeline with described desulfurization and linked to each other; Described one-level aerated precipitation tank, BAF, break are thrown the chlorine reaction tower and are linked to each other successively by pipeline; Described break throwing chlorine reaction tower is denitrogenated king-tower by pipeline with described desulfurization and is linked to each other, and described secondary aerated precipitation tank is denitrogenated king-tower by pipeline with described desulfurization and linked to each other, and described secondary aerated precipitation tank is connected by pipeline with flocculation sedimentation tank.
The treatment unit of described rare earth metallurgy, wherein, the described desulfurization multilayer denitrogenating and be provided with from the bottom to top the swirling inlet device that enters for flue gas in the king-tower, be used for discharging the gas barrier of flue gas and being used for the spray flue gas is without stopping up spiral type solid cone shaped tuyere arrangement; Described multilayer links to each other by pipeline and described break throwing chlorine reaction tower without stopping up spiral type solid cone shaped tuyere arrangement.
The treatment unit of described rare earth metallurgy, wherein, desulfurization is denitrogenated and is provided with 3-5 in the secondary tower for the treatment of the processing unit of flue gas, is provided with from the bottom to top in each processing unit for the single layer cloth device of air of air inlet and the individual layer that is used for the spray flue gas without stopping up spiral type hollow cone nozzles device; Described individual layer links to each other with described Hhigh-efficient thickener by pipeline without stopping up spiral type hollow cone nozzles device.
The treatment unit of described rare earth metallurgy, wherein, the treatment unit of described rare earth metallurgy also comprises the dechlorination apparatus for subsequent use for dechlorination, described dechlorination apparatus is thrown the chlorine reaction tower by pipeline and described break and is linked to each other with flocculation sedimentation tank; Be filled with gac or coking coal for dechlorination in the described dechlorination apparatus for subsequent use.
The treatment unit of described rare earth metallurgy, wherein, the treatment unit of described rare earth metallurgy also comprises first-level buffer pond, level 2 buffering pond and the three grades of Buffer Pools for homogenizing water quality and stabilizing water quantity, described first-level buffer pond is arranged on Hhigh-efficient thickener and desulfurization is denitrogenated between the secondary tower, described level 2 buffering pond is arranged between described one-level aerated precipitation tank and the BAF, and described three grades of Buffer Pools are arranged on BAF and break is thrown between the chlorine reaction tower.
The treatment unit of described rare earth metallurgy, wherein, described rare earth metallurgy treatment unit also comprises liming throwing device, a PAM throwing device, caustic soda throwing device, deamidization throwing device, the 2nd PAM throwing device, sulfuric acid throwing device, nutrition throwing device, clorox throwing device, Sodium Pyrosulfite throwing device; Described liming throwing device links to each other with described neutralization reaction pond with a PAM throwing device, described caustic soda throwing device and deamidization throwing device are arranged on described first-level buffer pond and described desulfurization is denitrogenated between the secondary tower, described the 2nd PAM throwing device and sulfuric acid throwing device are arranged on described desulfurization and denitrogenate between secondary tower and the described one-level aerated precipitation tank, described nutrition throwing device links to each other with described BAF, described clorox throwing device is thrown the chlorine reaction tower with described break and is linked to each other, and described Sodium Pyrosulfite throwing device links to each other with described dechlorination apparatus for subsequent use.
The treatment unit of described rare earth metallurgy wherein, also arranges a comprehensive wastewater collecting tank for mishmetal smelting wastewater and factory effluent between described air flotation pool and the neutralization reaction pond.
The treatment unit of described rare earth metallurgy, wherein, described rare earth metallurgy treatment unit also comprises the pressure filter of the waste residue that produces for the described Hhigh-efficient thickener of press filtration, described pressure filter is connected with Hhigh-efficient thickener.
The treatment unit of described rare earth metallurgy, wherein, be provided with packing layer in the described BAF, described packing layer is comprised of the active carbon layer and the clinoptilolite layer that arrange from top to bottom, described active carbon layer accounts for the 50-75% of total filler layer volume, and described clinoptilolite layer accounts for the 25-50% of total filler layer volume.
Beneficial effect: the utility model is according to the practical situation of Rare Earths smelting enterprise, boiler smoke improvement and factory effluent improvement are combined, take full advantage of boiler smoke and be rich in the characteristics such as coal ash, carbonic acid gas, sulfurous gas and higher flue-gas temperature, also utilized that waste water treatment technique neutral and alkali is higher, the stripping deamination need to be heated simultaneously, break throw after the chlorine technique chlorine residue higher, need to cut down the characteristics such as organism, ammonia nitrogen.After processing through method for waste water provided by the utility model, soda soap (calcium soap) but method Rare Earth Production heavy metal ions in wastewater, COD, ammonia nitrogen qualified discharge, the indexs such as the blackness of exhaustion of coal firing boiler, sulfurous gas, oxynitride all can qualified discharge simultaneously.The Processes and apparatus of wastewater comprehensive treatment provided by the utility model is all being obtained preferably effect aspect energy-saving and emission-reduction, the treatment of wastes with processes of wastes against one another, the qualified discharge.
Description of drawings
Fig. 1 is the structure function block diagram of soda soap method Rare Earth Production wastewater treatment equipment of the present utility model.
Fig. 2 is desulfurization removing nitric king-tower, the desulfurization removing nitric secondary tower equipment drawing of soda soap method Rare Earth Production wastewater treatment equipment of the present utility model.
Embodiment
The utility model provides a kind for the treatment of unit of rare earth metallurgy, and is clearer, clear and definite for making the purpose of this utility model, technical scheme and effect, below the utility model further described.Should be appreciated that specific embodiment described herein only in order to explaining the utility model, and be not used in restriction the utility model.
Most domestic adopts the medium and small sized enterprises of Rare Earths smelting technology, basically all needs supporting coal-fired steam boiler, and the coal firing boiler capacity is commonly 4-10T/H, and sulphur content is 2-3%(even higher in the coal combustion), exhaust gas volumn is at 12000-30000m
3/ H, 160-210 ℃ of discharging flue-gas temperature, discharging sulfur dioxide in flue gas content is at 3200-4800mg/m
3, amount of nitrogen oxides is at 450-600mg/m
3, carbon dioxide content is at 7-9%.Coal-fired steam boiler is supporting numb stone water mill dust collector generally adopts Wet Lime Desulfurization, but desulfuration efficiency is below 65%, and nitric efficiency can't reach the emission request of " emission standard of air pollutants for boilers " below 20%.
Therefore, in the utility model rare earth metallurgy improvement and fire coal boiler fume improvement are combined, take full advantage of boiler smoke and be rich in the characteristics such as coal ash, carbonic acid gas, sulfurous gas and higher flue-gas temperature, also utilized that waste water treatment technique neutral and alkali is higher, the stripping deamination need to be heated simultaneously, break throw after the chlorine technique chlorine residue higher, need to cut down the characteristics such as organism, ammonia nitrogen.After processing through method for waste water provided by the utility model, but heavy metal ion, COD, ammonia nitrogen qualified discharge in the saponification waste-water, and the indexs such as the blackness of exhaustion of coal firing boiler, sulfurous gas, oxynitride all can qualified discharge simultaneously.
The treatment process of rare earth metallurgy provided by the utility model, for the treatment of the low saponification waste-water of the ammonia quantity that produces in the rare-earth wet method smelting process, the treatment process of described rare earth metallurgy is applicable to process the soda soap method or calcium soap method rare-earth wet method is smelted the low saponification waste-water of ammonia quantity that produces in the production process, also is applicable to the processing of lower concentration ammonia-containing water in the ammonia saponification factory effluent.Wherein, the treatment process of described rare earth metallurgy is processed wastewater treatment and is combined with fire coal boiler fume, specifically may further comprise the steps:
A, saponification waste-water are removed oil slick and the basic ester of P507(2-ethylhexyl phosphonic acids single 2-ethyl first by oil trap, air flotation pool); Described saponification waste-water can also mix with factory effluents such as the precipitation waste water, washes that produce in the subsequent step, enters step B again;
B, in saponification waste-water, add liming and carry out neutralization reaction, with in and heavy metal, oxalic acid and other acidic substance in the saponification waste-water, add again the PAM that is used for the deposit seeds material;
C, employing Hhigh-efficient thickener carry out the waste residue precipitation, to reclaim after the press filtration of gained waste residue process pressure filter, to add deamidization after with the little adjust pH of caustic soda from the saponification waste-water of Hhigh-efficient thickener water outlet, pump is proposed the desulfurization that enters for the fire coal boiler fume processing and is denitrogenated secondary tower, participate in desulfurization and denitrogenate the interior desulfurization of secondary tower except ammonia react, reduce the ammonia in the saponification waste-water;
D, water outlet enter the one-level aerated precipitation tank, the organism in the sulfite ion in the oxidation saponification waste-water and the absorption saponification waste-water, and little adjust pH adds flocculation agent and precipitates;
E, go out water pump and carry and enter BAF, the organism in the saponification waste-water, ammonia nitrogen are adsorbed and biological degradation;
F, water outlet enter break and throw the chlorine reaction tower, adopt break to throw chlorine and react the ammonia nitrogen of removing in the saponification waste-water;
G, water outlet enter the desulfurization of processing for fire coal boiler fume and denitrogenate king-tower, and reaction is denitrogenated in the desulfurization that the participation desulfurization is denitrogenated in the king-tower, reduces the contents of residual chlorine in the saponification waste-water;
H, water outlet enter the secondary aerated precipitation tank, the organism in the sulfite ion in the oxidation saponification waste-water and the absorption saponification waste-water;
I, water outlet qualified discharge behind flocculation sediment.
Particularly, in the described steps A, saponification waste-water at first enters oil trap, and the residence time is 20-30H, and most of kerosene, P507 are removed.Then pump into air flotation pool, the oil slick of saponification waste-water is scraped the collection tank into air flotation pool.Described air flotation pool can be the cavitation air flotation pond.Preferably, described saponification waste-water is through behind the air flotation pool, and water outlet is introduced into the comprehensive wastewater equalizing tank with factory effluents such as precipitation waste water and Cleaning Wastewater and mixes, and composite waste is 10-15H in effective residence time of comprehensive wastewater collecting tank.
Among the described step B, described saponification waste-water can be introduced into equalizing tank and carry out homogeneous before entering the neutralization reaction pond, to improve reaction effect.Saponification waste-water pump behind the equalizing tank homogeneous is carried and is entered the neutralization reaction pond, adds liming and carries out neutralization reaction, and adjusting PH is 9-10, adds the PAM(polyacrylamide of 5mg/l), for the particulate matter of precipitation saponification waste-water.
Among the described step C, described saponification waste-water carries out the waste residue precipitation through entering after the neutralization reaction in the Hhigh-efficient thickener, be specially, and by described Hhigh-efficient thickener described saponification waste-water is carried out solid-liquid separation, the gained solid is waste residue, and described waste residue pumps into pressure filter to carry out reclaiming after press filtration is processed.Before denitrogenating secondary tower, desulfurization can be introduced into the first Buffer Pool through the saponification waste-water after after the waste residue precipitation entering, further homogenizing water quality and stabilizing water quantity.Then adding caustic soda in described saponification waste-water carries out PH and finely tunes to PH10-11, and add deamidization, then pump is proposed the desulfurization that enters for the fire coal boiler fume processing and is denitrogenated secondary tower, participate in desulfurization and denitrogenate secondary tower interior deliming, desulfurization, deamination reaction, by the ammonia in the stripping effect reduction waste water of flue gas.Without stopping up desulfurization nozzle spray flue gas, vapour-liquid ratio can reach more than the 600:1 described saponification waste-water through multilayer, and the calcium hydroxide in sulfur dioxide in flue gas, carbonic acid gas and the saponification waste-water reacts.Ammonia in the saponification waste-water is under the effect of efficient deamidization simultaneously, and through the stripping of high-temperature flue gas, the ammonia in the saponification waste-water becomes ammonia and overflows from saponification waste-water, reaches the purpose except ammonia, has also purified the coal ash in the flue gas simultaneously.Because lower by stripping ammonia out concentration in flue gas, most of ammonia is discharged from high-order chimney with flue gas.Wherein, described saponification waste-water enter desulfurization denitrogenate secondary tower pressure and must guarantee 〉=35 meters.
Among the described step D, the saponification waste-water of discharging from the desulfurization nitrogen-rejection column enters the one-level aerated precipitation tank, and described one-level aeration tank comprises aeration tank and settling tank.At first, the high strength aeration is adopted in described aeration tank, to the saponification waste-water oxygenation, sulfurous acid acid ion in the further oxidation saponification waste-water, the aeration tank also receives from the coal ash that is retained down in the settling tank simultaneously, under stirring action, flyash fully contacts with saponification waste-water, the organism in the absorption saponification waste-water.Adopting subsequently the vitriol oil to regulate pH value is 8-9, adds the PAM postprecipitation of 3-5PPM.Supernatant liquor after precipitating enters BAF, enter again described BAF before, can be introduced into the second Buffer Pool, further homogenizing water quality and stabilizing water quantity.
In the described step e, water outlet enters BAF, and filtration velocity is not higher than 2.0M/H, and gas-water ratio is 4-6:1, and described BAF comprises anaerobic filter and aerobic filter tank, saponification waste-water flow through respectively described anaerobic filter and aerobic filter tank.In each filter tank, add corresponding salt tolerant biological inoculum, comprise the scrubbing bacterium, remove ammonia bacterium, oil-removing bacteria, the Aerobic Pond water outlet is back to anaerobic pond by the 100-200% for the treatment of capacity, by the absorption of modified zeolite and biological ceramic particle (gac) and the salt-durable microbe that adheres to organism, ammonia nitrogen in the sewage is degraded.This system need to regularly carry out air-water backwashing operation, must add the adequate nutrition thing according to the difference of effluent of aeration biological filter water quality situations at different levels, such as glucose, phosphate fertilizer etc., also needs to mend and adds an amount of alkali, keeps the required basicity of nitration denitrification.The water outlet of described one-level aerated precipitation tank can be after the plant area sanitary sewage mixes together pump carry and enter BAF, by adding salt-durable microbe, the organism in the composite waste, ammonia nitrogen are adsorbed and biological degradation.
In the described step F, the effluent of aeration biological filter pump is carried and is entered break throwing chlorine reaction tower, about control water inlet PH=7, presses Cl
-: NN
4 +=8:1 adds clorox, and retention time of sewage is 30-50min.Described break is thrown the chlorine reaction tower and is adopted vertical type cylinder shape tank body, and material is steel lining glue.When the described desulfurization of processing for fire coal boiler fume is denitrogenated king-tower and is not needed described saponification waste-water, described saponification waste-water is after described break is thrown the water outlet of chlorine reaction tower, can enter dechlorination apparatus for subsequent use after the water outlet, described dechlorination apparatus for subsequent use can arrange two dechlorination reaction tanks, can fill gac in the described dechlorination reaction tank or coking coal carries out dechlorination, also can adopt to add the Sodium Pyrosulfite reductive agent, every tank residence time is 30-50min.Through after the dechlorination apparatus water outlet for subsequent use, qualified discharge behind flocculation sediment.
Among the described step G, higher through chlorine residue in the reacted saponification waste-water of break throwing chlorine, PH is greatly about about 7-8, going out water pump carries and enters desulfurization and denitrogenate king-tower, because basicity is not high, its sweetening effectiveness is general, but under the strong oxidizing property of clorox, accelerate the oxygenizement of the reducing substanceses such as the sulfurous gas in the flue gas, oxynitride, improved the desulfurization removing nitric efficient of smoke processing system.Because the chlorine residue in the saponification waste-water and the sulfurous gas in the flue gas, oxynitride, carbon dust etc. react, also reach the chlorine residue effect in the waste water of cutting down, further reduce simultaneously COD in the waste water.Also significantly cut down simultaneously the reduction dosage that reduces chlorine residue and need to use, reached the effect of the treatment of wastes with processes of wastes against one another.
Among the described step H, desulfurization is denitrogenated the king-tower water outlet and is entered the secondary aerated precipitation tank, described secondary aerated precipitation tank comprises aeration tank and settling tank, at first in the aeration tank, adopt the high strength aeration, to the saponification waste-water oxygenation, the sulfite ion in the further oxidation saponification waste-water, the aeration tank also receives the coal ash that is retained down from detritus pool simultaneously, under the stirring action, flyash fully contacts with waste water, the organism in the absorption waste water.
Among the described step I, enter flocculation sedimentation tank through the saponification waste-water behind the aeration and sedimentation, add the flocculation agent PAC(polymerize aluminum chloride of 50-80mg/L) and the coagulant aids PAM of coagulant aids 3mg/L, the supernatant liquor qualified discharge after the processing, the body refuse that precipitates enters the sludge press filtration system.
Also be provided for realizing the rare earth metallurgy treatment unit of above-mentioned rare earth metallurgy treatment process in the utility model, as shown in Figure 1, described rare earth metallurgy treatment unit combines with Dume desulfurizing denitrogenation appts, described Dume desulfurizing denitrogenation appts comprises that king-tower is denitrogenated in desulfurization and secondary tower is denitrogenated in desulfurization, desulfurization is denitrogenated king-tower and is denitrogenated secondary tower with desulfurization and link to each other by pipeline, particularly, described rare earth metallurgy treatment unit comprises:
Oil trap, air flotation pool, be used for rare earth metallurgy (being saponification waste-water) is carried out the equalizing tank of homogeneous, be used for and rare earth metallurgy in heavy metal and the neutralization reaction pond of acidic substance, be used for carrying out the Hhigh-efficient thickener of waste residue precipitation, be used for the sulfite ion of rare earth oxide smelting wastewater and the organic one-level aerated precipitation tank in the absorption rare earth metallurgy, be used for the organism to rare earth metallurgy, ammonia nitrogen adsorbs and the biological degradation BAF, be used for carrying out the break throwing chlorine reaction tower that break is thrown the ammonia nitrogen of chlorine reaction removal rare earth metallurgy, be used for the sulfite ion of rare earth oxide smelting wastewater and the organic secondary aerated precipitation tank in the absorption rare earth metallurgy, the flocculation sedimentation tank that is used for the body refuse of precipitating rare earth smelting wastewater;
Described oil trap, air flotation pool, equalizing tank, neutralization reaction pond, Hhigh-efficient thickener connect successively by pipeline; Described Hhigh-efficient thickener is denitrogenated secondary tower by pipeline with described desulfurization and is linked to each other, and described one-level aerated precipitation tank is denitrogenated secondary tower by pipeline with described desulfurization and linked to each other; Described one-level aerated precipitation tank, BAF, break are thrown the chlorine reaction tower and are linked to each other successively by pipeline; Described break throwing chlorine reaction tower is denitrogenated king-tower by pipeline with described desulfurization and is linked to each other, and described secondary aerated precipitation tank is denitrogenated king-tower by pipeline with described desulfurization and linked to each other, and described secondary aerated precipitation tank is connected by pipeline with flocculation sedimentation tank;
Described rare earth metallurgy treatment unit also comprises the pressure filter of the waste residue that produces for the described Hhigh-efficient thickener of press filtration, and described pressure filter is connected with Hhigh-efficient thickener.
Described rare earth metallurgy treatment unit also comprises the dechlorination apparatus for subsequent use for dechlorination, and described dechlorination apparatus is thrown the chlorine reaction tower by pipeline and described break and linked to each other with flocculation sedimentation tank.Described dechlorination apparatus for subsequent use can arrange two dechlorination reaction tanks, can fill gac in the described dechlorination reaction tank or coking coal carries out dechlorination, also can adopt to add the Sodium Pyrosulfite reductive agent.
Described one-level aerated precipitation tank and secondary aerated precipitation tank are respectively arranged with the gas blower for blast aeration, in the time of to the saponification waste-water oxygenation detritus pool floor coal lime-ash is refluxed, make and denitrogenate king-tower and desulfurization from desulfurization and denitrogenate the flyash that secondary tower brings out and fully contact with saponification waste-water.
Described rare earth metallurgy treatment unit also comprises first-level buffer pond, level 2 buffering pond and the three grades of Buffer Pools for homogenizing water quality and stabilizing water quantity, described first-level buffer pond is arranged on Hhigh-efficient thickener and desulfurization is denitrogenated between the secondary tower, described level 2 buffering pond is arranged between described one-level aerated precipitation tank and the BAF, and described three grades of Buffer Pools are arranged on BAF and break is thrown between the chlorine reaction tower.
Also arrange one between described air flotation pool and the neutralization reaction pond for the comprehensive wastewater collecting tank that mixes saponification waste-water and factory effluent, saponification waste-water through air flotation pool flows in the described comprehensive wastewater collecting tank, the factory effluents such as the precipitation waste water that produces in the utility model process and Cleaning Wastewater also enter in the described comprehensive wastewater collecting tank, mix with described saponification waste-water, enter again in the neutralization reaction pond and react.
Described rare earth metallurgy treatment unit also comprises liming throwing device, a PAM throwing device, caustic soda throwing device, deamidization throwing device, the 2nd PAM throwing device, sulfuric acid throwing device, nutrition throwing device, clorox throwing device, Sodium Pyrosulfite throwing device; Described liming throwing device links to each other with described neutralization reaction pond with a PAM throwing device, described caustic soda throwing device and deamidization throwing device are arranged on described first-level buffer pond and described desulfurization is denitrogenated between the secondary tower, described the 2nd PAM throwing device and sulfuric acid throwing device are arranged on described desulfurization and denitrogenate between secondary tower and the described one-level aerated precipitation tank, described nutrition throwing device links to each other with described BAF, described clorox throwing device is thrown the chlorine reaction tower with described break and is linked to each other, and described Sodium Pyrosulfite throwing device links to each other with described dechlorination apparatus for subsequent use.
King-tower is denitrogenated in described desulfurization and secondary tower is denitrogenated in desulfurization, and working shaft pressure is 35-50 rice, and tower body adopts cylindricity.As shown in Figure 2, break is thrown the reacted saponification waste-water of chlorine and is entered desulfurization and denitrogenate king-tower, and the Hhigh-efficient thickener water outlet enters desulfurization and denitrogenates secondary tower, and before desulfurization is denitrogenated king-tower and is arranged in flue gas is processed, after desulfurization is denitrogenated secondary tower and is arranged in.Desulfurization is denitrogenated king-tower 2 and is adopted bottom inflow, top exhaust mode, swirling inlet device 1 and multilayer is set without stopping up spiral type solid cone shaped tuyere arrangement 3 in the tower.Describedly throw the chlorine reaction tower by pipeline and described break and link to each other without stopping up spiral type solid cone shaped tuyere arrangement 3, the good fortune waste water of throwing the chlorine reaction tower through described break enters described desulfurization by pipeline and denitrogenates king-tower 2 interior deliming, desulfurization, deamination reaction.Minute parallel multiple-unit treatment system in the secondary tower 9 is denitrogenated in desulfurization, generally divides the 3-5 unit, and each unit is separated it with dividing plate 6, by air main 4 realizations each unit is carried out gas distribution.The mode of each unit employing bottom inflow in the secondary tower 9 is denitrogenated in desulfurization, single layer cloth device of air 5 and individual layer is set without stopping up spiral type hollow cone nozzles device 7 in each unit, by vapor pipe 8 flue gas is discharged at last, is provided with dewatering unit at exhaust side.Described nothing is stopped up spiral type hollow cone nozzles device 7 and is linked to each other with described Hhigh-efficient thickener by pipeline, and the saponification waste-water of process Hhigh-efficient thickener enters described desulfurization by pipeline and denitrogenates secondary tower 9, and the desulfurization that the participation desulfurization is denitrogenated in the secondary tower 9 remove ammonia react.
Described BAF adopts A/O technique, employing flows up into water, air contacts in the same way with sewage, be provided with packing layer in the described BAF, described packing layer is comprised of the active carbon layer and the clinoptilolite layer that arrange from top to bottom, described active carbon layer accounts for the 50-75% of total filler layer volume, and described clinoptilolite layer accounts for the 25-50% of total filler layer volume.Described BAF also comprises concrete filter, aerating apparatus, air water back washing device, circulation reflux device, nutrition supplementary device, basicity supplementary device etc., and this is prior art, is not repeated herein.
Add the higher biological inoculum of the tolerance of salinity in the described BAF, comprise the scrubbing bacterium, remove ammonia bacterium and oil-removing bacteria, the composition of biological inoculum is genus bacillus, Saccharomycodes, and micrococcus sps etc. have higher resisting chlorides toxicity, the salinity of the highest ability 4%.
Described break is thrown chlorine except the ammonia tower, arranging multiplayer porous plate water-distributing device in the tower, and the residence time is not less than 30 minutes.Described dechlorination apparatus for subsequent use arranges two dechlorination reaction tanks, weighting material is coke (or gac), and supporting Sodium Pyrosulfite adds simultaneously, and two dechlorination reaction tank height designs are according to filling 3 meters coke (gac) design, each top of tower arranges automatic exhaust steam valve, and chlorine contained exhaust gas enters adsorber.
In sum, rare earth metallurgy treatment process provided by the utility model compared with prior art has following advantage and treatment effect:
(1) the utility model is according to the practical situation of Rare Earths smelting enterprise, boiler smoke is administered and factory effluent improvement combines, utility model a kind of comprehensive processing technique, effect is better aspect energy-saving and emission-reduction, the treatment of wastes with processes of wastes against one another, qualified discharge.
(2) adopt the biological chemistry integrated process to process, take full advantage of the adsorption of flyash, break is thrown chlorine except the ammonia effect, and organic effect falls in the ammonia that removes of BAF, and after treatment, the COD of water outlet, ammonia nitrogen index can satisfy emission request.
(3) process by introducing boiler smoke, by reactions such as factory effluent and carbon dioxide in flue gas, sulfurous gas, generate the throw outs such as calcium sulfate, calcium carbonate, reach significant reduction calcium ion concn, be conducive to reduce salinity, reduce the calcium dirt, replenish smoothly phosphate fertilizer, optimize the microorganism living environment.
(4) process by introducing boiler smoke, utilize the adsorption of coal ash can cut down organism in the saponification waste-water, remain in the saponification waste-water polymer such as P507, kerosene organic matter removal effect better, be conducive to follow-up microbiological deterioration.
(5) process by introducing boiler smoke, utilize temperature and the exhaust gas volumn of flue gas, be conducive to flue gas to the ammonia stripping, saved the heat power consumption of the required energy and the required blower fan of stripping of saponification waste-water.
(6) process by introducing boiler smoke, utilize the sulfurous gas in the flue gas, the reductibility of oxynitride that chlorine residue is absorbed, reduce adding of reductive agent, be conducive to simultaneously improve desulfurization removing nitric efficient.
(7) salt-durable microbe of suitable Rare Earths smelting wastewater supersalinity, high chlorine Gent point has been adopted in selection, comprises scrubbing bacterial classification, oil removing bacterial classification, removes ammonia bacterial classification etc., the saltiness of the highest ability 4%.By selecting suitable filler combination and guaranteeing the microorganism growth environment, guarantee that biological treatment system runs well.
Should be understood that; application of the present utility model is not limited to above-mentioned giving an example; for those of ordinary skills, can be improved according to the above description or conversion, all these improvement and conversion all should belong to the protection domain of the utility model claims.
Claims (9)
1. the treatment unit of a rare earth metallurgy, the treatment unit of described rare earth metallurgy combines with Dume desulfurizing denitrogenation appts, described Dume desulfurizing denitrogenation appts comprises that king-tower is denitrogenated in desulfurization and secondary tower is denitrogenated in desulfurization, desulfurization is denitrogenated king-tower and is denitrogenated secondary tower with desulfurization and link to each other by pipeline, it is characterized in that, described rare earth metallurgy treatment unit comprises: oil trap, air flotation pool, be used for rare earth metallurgy is carried out the equalizing tank of homogeneous, be used for and rare earth metallurgy in heavy metal and the neutralization reaction pond of acidic substance, be used for carrying out the Hhigh-efficient thickener of waste residue precipitation, be used for the sulfite ion of rare earth oxide smelting wastewater and the organic one-level aerated precipitation tank in the absorption rare earth metallurgy, be used for the organism to rare earth metallurgy, ammonia nitrogen adsorbs and the biological degradation BAF, be used for carrying out the break throwing chlorine reaction tower that break is thrown the ammonia nitrogen of chlorine reaction removal rare earth metallurgy, be used for the sulfite ion of rare earth oxide smelting wastewater and the organic secondary aerated precipitation tank in the absorption rare earth metallurgy, the flocculation sedimentation tank that is used for the body refuse of precipitating rare earth smelting wastewater;
Described oil trap, air flotation pool, equalizing tank, neutralization reaction pond, Hhigh-efficient thickener connect successively by pipeline; Described Hhigh-efficient thickener is denitrogenated secondary tower by pipeline with described desulfurization and is linked to each other, and described one-level aerated precipitation tank is denitrogenated secondary tower by pipeline with described desulfurization and linked to each other; Described one-level aerated precipitation tank, BAF, break are thrown the chlorine reaction tower and are linked to each other successively by pipeline; Described break throwing chlorine reaction tower is denitrogenated king-tower by pipeline with described desulfurization and is linked to each other, and described secondary aerated precipitation tank is denitrogenated king-tower by pipeline with described desulfurization and linked to each other, and described secondary aerated precipitation tank is connected by pipeline with flocculation sedimentation tank.
2. the treatment unit of rare earth metallurgy according to claim 1, it is characterized in that, the multilayer that described desulfurization is denitrogenated and is provided with from the bottom to top the swirling inlet device that enters for flue gas in the king-tower, is used for discharging the gas barrier of flue gas and being used for the spray flue gas is without stopping up spiral type solid cone shaped tuyere arrangement; Described multilayer links to each other by pipeline and described break throwing chlorine reaction tower without stopping up spiral type solid cone shaped tuyere arrangement.
3. the treatment unit of rare earth metallurgy according to claim 1, it is characterized in that, desulfurization is denitrogenated and is provided with 3-5 in the secondary tower for the treatment of the processing unit of flue gas, is provided with from the bottom to top in each processing unit for the single layer cloth device of air of air inlet and the individual layer that is used for the spray flue gas without stopping up spiral type hollow cone nozzles device; Described individual layer links to each other with described Hhigh-efficient thickener by pipeline without stopping up spiral type hollow cone nozzles device.
4. the treatment unit of rare earth metallurgy according to claim 1, it is characterized in that, the treatment unit of described rare earth metallurgy also comprises the dechlorination apparatus for subsequent use for dechlorination, and described dechlorination apparatus is thrown the chlorine reaction tower by pipeline and described break and linked to each other with flocculation sedimentation tank; Be filled with gac or coking coal for dechlorination in the described dechlorination apparatus for subsequent use.
5. the treatment unit of rare earth metallurgy according to claim 1, it is characterized in that, the treatment unit of described rare earth metallurgy also comprises first-level buffer pond, level 2 buffering pond and the three grades of Buffer Pools for homogenizing water quality and stabilizing water quantity, described first-level buffer pond is arranged on Hhigh-efficient thickener and desulfurization is denitrogenated between the secondary tower, described level 2 buffering pond is arranged between described one-level aerated precipitation tank and the BAF, and described three grades of Buffer Pools are arranged on BAF and break is thrown between the chlorine reaction tower.
6. the treatment unit of rare earth metallurgy according to claim 5, it is characterized in that, described rare earth metallurgy treatment unit also comprises liming throwing device, a PAM throwing device, caustic soda throwing device, deamidization throwing device, the 2nd PAM throwing device, sulfuric acid throwing device, nutrition throwing device, clorox throwing device, Sodium Pyrosulfite throwing device; Described liming throwing device links to each other with described neutralization reaction pond with a PAM throwing device, described caustic soda throwing device and deamidization throwing device are arranged on described first-level buffer pond and described desulfurization is denitrogenated between the secondary tower, described the 2nd PAM throwing device and sulfuric acid throwing device are arranged on described desulfurization and denitrogenate between secondary tower and the described one-level aerated precipitation tank, described nutrition throwing device links to each other with described BAF, described clorox throwing device is thrown the chlorine reaction tower with described break and is linked to each other, and described Sodium Pyrosulfite throwing device links to each other with described dechlorination apparatus for subsequent use.
7. the treatment unit of rare earth metallurgy according to claim 1 is characterized in that, a comprehensive wastewater collecting tank for mishmetal smelting wastewater and factory effluent also is set between described air flotation pool and the neutralization reaction pond.
8. the treatment unit of rare earth metallurgy according to claim 1 is characterized in that, described rare earth metallurgy treatment unit also comprises the pressure filter of the waste residue that produces for the described Hhigh-efficient thickener of press filtration, and described pressure filter is connected with Hhigh-efficient thickener.
9. the treatment unit of rare earth metallurgy according to claim 1, it is characterized in that, be provided with packing layer in the described BAF, described packing layer is comprised of the active carbon layer and the clinoptilolite layer that arrange from top to bottom, described active carbon layer accounts for the 50-75% of total filler layer volume, and described clinoptilolite layer accounts for the 25-50% of total filler layer volume.
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| CN 201220536969 CN202849212U (en) | 2012-10-19 | 2012-10-19 | Rear earth metallurgy wastewater treatment device |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103693788A (en) * | 2014-01-06 | 2014-04-02 | 昆山工研院华科生物高分子材料研究所有限公司 | Industrial sewage treatment method and integrated apparatus for same |
| CN105084327A (en) * | 2014-05-20 | 2015-11-25 | 上海三卿环保科技有限公司 | Method for preparing high-purity double salt by crystallization of desulfurization and denitrification liquid |
| CN105601013A (en) * | 2015-12-24 | 2016-05-25 | 南京格洛特环境工程股份有限公司 | Zero emission and recycling co-treatment method for copper smelting dirty acid water and magnesium desulfurization sludge |
| CN106045200A (en) * | 2016-06-27 | 2016-10-26 | 深圳市翰唐环保科技有限公司 | Coking wastewater treatment technique |
| CN106673373A (en) * | 2017-01-19 | 2017-05-17 | 西藏神州瑞霖环保科技股份有限公司 | Sustainable and efficient sewage treatment system |
| CN109081464A (en) * | 2018-10-10 | 2018-12-25 | 信丰县包钢新利稀土有限责任公司 | A kind of rare earth extraction sewage-treatment plant |
| CN112121468A (en) * | 2020-09-19 | 2020-12-25 | 周力 | Easy-to-clean rare earth feed liquid deoiling device |
| CN113461260A (en) * | 2021-07-02 | 2021-10-01 | 江西理工大学 | Method for recycling and denitrifying ion type rare earth mine tail water rare earth |
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- 2012-10-19 CN CN 201220536969 patent/CN202849212U/en not_active Expired - Lifetime
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103693788A (en) * | 2014-01-06 | 2014-04-02 | 昆山工研院华科生物高分子材料研究所有限公司 | Industrial sewage treatment method and integrated apparatus for same |
| CN103693788B (en) * | 2014-01-06 | 2015-10-21 | 昆山工研院华科生物高分子材料研究所有限公司 | A kind of Industrial Waste Water Treatments integrative machine |
| CN105084327A (en) * | 2014-05-20 | 2015-11-25 | 上海三卿环保科技有限公司 | Method for preparing high-purity double salt by crystallization of desulfurization and denitrification liquid |
| CN105601013A (en) * | 2015-12-24 | 2016-05-25 | 南京格洛特环境工程股份有限公司 | Zero emission and recycling co-treatment method for copper smelting dirty acid water and magnesium desulfurization sludge |
| CN106045200A (en) * | 2016-06-27 | 2016-10-26 | 深圳市翰唐环保科技有限公司 | Coking wastewater treatment technique |
| CN106673373A (en) * | 2017-01-19 | 2017-05-17 | 西藏神州瑞霖环保科技股份有限公司 | Sustainable and efficient sewage treatment system |
| CN109081464A (en) * | 2018-10-10 | 2018-12-25 | 信丰县包钢新利稀土有限责任公司 | A kind of rare earth extraction sewage-treatment plant |
| CN109081464B (en) * | 2018-10-10 | 2021-04-06 | 信丰县包钢新利稀土有限责任公司 | Sewage treatment plant for rare earth extraction |
| CN112121468A (en) * | 2020-09-19 | 2020-12-25 | 周力 | Easy-to-clean rare earth feed liquid deoiling device |
| CN113461260A (en) * | 2021-07-02 | 2021-10-01 | 江西理工大学 | Method for recycling and denitrifying ion type rare earth mine tail water rare earth |
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