CN105080935A - Rubbish flying ash cement kiln co-treatment and water resource utilization system - Google Patents
Rubbish flying ash cement kiln co-treatment and water resource utilization system Download PDFInfo
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Abstract
The invention relates to a rubbish flying ash cement kiln co-treatment and water resource utilization system. Washing water generated by a rubbish incineration flying ash three-level washing desalination system enters a coagulating sedimentation heavy metal removal system; a solution obtained by the coagulating sedimentation heavy metal removal system enters a sodium filtering and reverse osmosis pre-concentration system, wherein the salt content of the solution ranges from 1% to 2%; calcium and magnesium ions in the washing water are removed through the sodium filtering and reverse osmosis pre-concentration system, the solution with the salt content ranging from 1% to 2% is concentrated into a solution with the salt content ranging from 6% to 8%, and the solution with the salt content ranging from 6% to 8% is conveyed to a membrane distillation concentration system to circulate and generate distilled water for membrane component backwashing and rubbish incineration flying ash washing water replenishing; a nearly-saturated solution, with the salt content ranging from 20% to 30%, generated by the membrane distillation concentration system enters an infinitesimal abraum salt removal system for abraum salt removal and finally enters an MVR evaporative crystallization system for evaporative crystallization. The system is a device for carrying out cement kiln co-treatment on rubbish incineration flying ash, and therefore resource utilization can be achieved.
Description
Technical field:
The present invention relates to garbage flying ash and dispose field, relate to a kind of garbage flying ash cement kiln synergic processing in particular and recycling of water resource utilizes system.
Background technology:
Along with socioeconomic development, Process of Urbanization is aggravated, and a lot of big and medium-sized cities of China meet with the puzzlement of " garbage-surrounded city ".Garbage disposal has 3 kinds of modes: landfill, burning and compost, and the garbage disposal of current China adopts based on landfill, and compost and burning are auxiliary measure, and this will take a large amount of land resource.Along with the rising of land price, what urban environment required improves constantly, and garbage loading embeading becomes no longer economy and safety, and increasing city starts to consider incineration treatment of garbage.Burning disposal can make the volume of municipal refuse reduce 80-90%, and its waste residue produced can make recycling.
Flying dust is the residue of waste incineration, the carcinogenic substance “ bioxin that waste incineration produces " 90% all in flying dust.The flying dust of uncured process is dealt with improperly, and wherein a large amount of heavy metals, Ji bioxin can cause serious contamination accident, endangers residents ' health.Before, the whole nation only has several cities carrying out incineration of refuse flyash process.Flying dust processing cost is very high on the one hand.On the other hand due to irregular marketing, supervise not in place, there is the problem of harmful competition, make " flying dust " be in " disorderly flying " state.Flying dust can not obtain safe disposal, will be environmentally hazardous very big hidden danger.
Because flying dust contains a large amount of chlorions, chlorion is normally produced cement kiln and is produced very large impact, be mainly manifested in cement kiln skinning, serious meeting produces quality accident, so, the key that flying dust disposed by cement kiln removes a large amount of chlorions in flying dust, and water wash system is the main method removing chlorion in flying dust.
Summary of the invention:
The object of the invention is for the deficiencies in the prior art part, a kind of garbage flying ash cement kiln synergic processing and recycling of water resource is provided to utilize system, achieve the innoxious of flying dust and recycling treatment, flying ash can meet the raw materials used standard of manufacture of cement, and water resource can realize recycling.
Technology solution of the present invention is as follows:
A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, it comprise connect successively incineration of refuse flyash tertiary effluent salt elution system, coagulating sedimentation removal heavy metal system, sodium filter and counter-infiltration preconcentration technique, membrane distillation concentration system, go denier carnallite system and MVR evaporation and crystallization system; The washing water of described incineration of refuse flyash tertiary effluent salt elution system produce enters coagulating sedimentation removal heavy metal system by pipeline; The saliferous rate that coagulating sedimentation removal heavy metal system obtains is that the solution of 1-2% enters sodium filter and counter-infiltration preconcentration technique; Described sodium filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, be the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into membrane distillation concentration system and carries out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing; The saliferous rate of described membrane distillation concentration system produce is that the nearly saturated solution of 20%-30% enters denier carnallite system and removed by carnallite, and last nearly saturated solution enters MVR evaporation and crystallization system and carries out evaporative crystallization.
As preferably, described incineration of refuse flyash tertiary effluent salt elution system it comprise flying dust storage, the lower end of described flying dust storage is communicated with conveying worm a, and the outlet of described conveying worm is connected to first order washing desalter, and first order washing desalter comprises agitator tank a; Described agitator tank a is communicated with respectively water inlet pipe a and chemical feed pipe a; Flying dust in described agitator tank a, water become mud with medicinal liquid agitating, the lower end of agitator tank a is connected to slush pump a, mud in agitator tank a is conveyed into buffer tank a by slush pump a, and the mud in buffer tank a is conveyed into horizontal centrifuge a by slush pump b and dewaters; Mud is isolated chloro ion-containing solution and flying dust that is moisture and bioxin by described horizontal centrifuge a, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and flying dust that is moisture and bioxin enters second level washing desalter; Chloro ion-containing solution mud isolated by described second level washing desalter and secondary is moisture and the flying dust of bioxin, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and secondary flying dust that is moisture and bioxin enters third level washing desalter; The flying dust of chloro ion-containing solution and three moisture and bioxin isolated by third level washing desalter, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, the flying dust of three moisture Ji bioxin enters cement kiln, and after cement kiln burns, flying dust becomes cement raw material.
As preferably, the charging aperture of described horizontal centrifuge a is connected to the discharging opening of slush pump b; The slag notch of described horizontal centrifuge a is connected to conveying worm b, and the liquid outlet of horizontal centrifuge a is connected to coagulating sedimentation removal heavy metal system by fluid pipeline; Described conveying worm b is provided with two discharging openings; Described second level washing desalter comprises agitator tank b, the discharging opening of each conveying worm b is connected to an agitator tank b, slurries in each agitator tank b send into buffer tank b through slush pump c, and the slurry in buffer tank b is sent into horizontal centrifuge b through slush pump d and dewatered; The slag notch of described horizontal centrifuge b is connected to conveying worm c, and the liquid outlet of horizontal centrifuge b is connected to coagulative precipitation tank by fluid pipeline; Described conveying worm c is provided with two discharging openings; Third level washing desalter comprises agitator tank c, the discharging opening of each conveying worm c is connected to an agitator tank c, slurries in each agitator tank c send into buffer tank c through slush pump e, slurry in buffer tank c is sent into horizontal centrifuge c through slush pump f and is dewatered, and the charging aperture of described horizontal centrifuge c is connected to the discharging opening of slush pump f; The slag notch of described horizontal centrifuge c is connected to cement kiln.
As preferably, described each agitator tank b is connected to water inlet pipe b, each agitator tank c is connected to water inlet pipe c, described water inlet pipe a, water inlet pipe b are connected with inlet water tank respectively with water inlet pipe c; Described each agitator tank b is connected to chemical feed pipe b, each agitator tank c is connected to chemical feed pipe c, described chemical feed pipe a, chemical feed pipe b and chemical feed pipe c are connected on chemicals dosing plant; The liquid outlet parallel join of described chemicals dosing plant has three groups of automatic control flow devices, and three groups of automatic control flow devices control the flow in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, can send alarm when dose is not enough.
As preferably, described coagulating sedimentation removal heavy metal system comprises coagulative precipitation tank, and the left end of described coagulative precipitation tank is connected to two agitator tank d by delivery pump a, and each agitator tank d is communicated with liquid-feeding tube and chemical feed pipe; Described chemical feed pipe is connected with chemicals dosing plant by dosing pump, and chemicals dosing plant is connected with water pipe; Described coagulative precipitation tank bottom is connected with centrifugal dehydrator, and coagulative precipitation tank top is connected with Buffer Pool, and Buffer Pool is connected to delivery pump b, and delivery pump b is connected to composite bag type filter, and composite bag type filter lower end is connected to centrifugal dehydrator; The heavy metal precipitation thing of coagulative precipitation tank bottom transports into centrifugal dehydrator and dewaters, the clear liquid on coagulative precipitation tank top is conveyed into Buffer Pool, liquid in Buffer Pool is conveyed into composite bag type filter by delivery pump b, the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter, the heavy metal obtained and impurity transport into centrifugal dehydrator and dewater, and the saliferous rate obtained is that the solution of 8-15% enters membrane distillation concentration device and carries out desalting processing.
As preferably, described chemical feed pipe is provided with the dosing valve controlling dosing flow; Described liquid-feeding tube is provided with priming valve.
As preferably, described sodium filter and counter-infiltration preconcentration technique comprise sodium filter assembly, and described sodium is filtered on assembly and is communicated with chemicals dosing plant a, and chemicals dosing plant a is connected with water pipe a; The water inlet end of described sodium filter assembly is connected to filter a, and the condensed water of sodium filter assembly output is connected to intermediate water tank by pipeline, and the fresh water of sodium filter assembly output is connected to counter-infiltration water tank by pipeline; The bottom of described intermediate water tank is connected to feeding engine a, and the water side of feeding engine a is connected to filter b, and the port of export of filter b is connected to counter-infiltration pre-concentration device; Described counter-infiltration pre-concentration device is communicated with chemicals dosing plant b, and chemicals dosing plant b is connected with water pipe b; The condensed water of described counter-infiltration pre-concentration device output is connected in Membrane Materials system by water pipe, and the fresh water of counter-infiltration pre-concentration device output is connected in counter-infiltration water tank by water pipe.
As preferably, described membrane distillation concentration system comprises heating water tank, and described heating water tank is connected with volumetric heat exchanger, and the upper end of heating water tank is communicated with feed tube, and the lower end of heating water tank is communicated with two groups of operating water tanks side by side by feeding engine; The outlet pipe often organizing described operating water tank is connected to the hot water inlet pipe of distillation device and concentrated water tank by feeding circulating pump simultaneously, often organize on described operating water tank and be connected with dope evacuated tube and dope return pipe, the hot water outlet pipe of described distillation device is connected to dope return pipe; The cold water inlet tube of described distillation device is connected to cooling tower, and cooling tower is connected with CWR, and the cooling water outlet pipe of distillation device is connected to CWR; The condensate pipe of described distillation device is connected to product water tank; Described distillation device top is connected with backwash water feed pipe, distillation device bottom is connected with backwash water evacuated tube and dope evacuated tube a, backwash water feed pipe is connected to backwash water tank by backwashing pump, and backwash water tank and backwash water evacuated tube link together, the dope evacuated tube on dope evacuated tube a and operating water tank links together.
As preferably, described denier carnallite system of going comprises concentrate case, the upper end of described concentrate case is communicated with feed tube, the lower end of described concentrate case is communicated with drain pipe, described drain pipe is connected with separation feeding engine, and the discharge nozzle being separated feeding engine divides two-way, every road discharge nozzle is connected to separation ball valve, for being separated ball valve a and being separated ball valve b, be separated ball valve a and be connected to one-level carnallite release unit, be separated ball valve b and be connected to secondary carnallite release unit; The lower end of described one-level carnallite release unit is connected to carnallite collecting pit, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a is connected with concentrated material returning valve; The upper end of described secondary carnallite release unit is connected to and is separated ball valve d, and be separated ball valve d and be connected to pipeline a and pipeline b simultaneously, pipeline b is connected with crystallization and evaporation valve, crystallization and evaporation valve is connected to MVR evaporation and crystallization system.
As preferably, described MVR evaporation and crystallization system comprises feeding engine d, and feeding engine d is connected to evaporating chamber, and described evaporating chamber is communicated with heat exchanger, heat exchanger is connected with steam recompression pump; The bottom of described evaporating chamber is connected with suction filtration tank by discharging pump d, and the top of evaporating chamber is connected to Roots's steam recompression machine by pipeline; In described Roots's steam recompression machine, vavuum pump is installed; Described vavuum pump is connected to filtrate tank, filtrate tank is connected with suction filtration tank, and vavuum pump and steam recompress pump links together, the mother liquor under vavuum pump effect in filtrate tank is negative pressure state, and the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization.
Beneficial effect of the present invention is:
The chloro ion-containing solution that tertiary effluent salt elution system of the present invention produces enters coagulative precipitation tank, moisture 40%-50% and containing CL ion lower than 1% flying dust enter the heavy metal that mud collecting pit carries out in microbial attack bioxin and flying dust, directly can be used as the raw material of construction material through the flying dust of microbial attack bioxin.This microorganism is reusable, namely completes flying dust water yield 1:8 tertiary effluent and washes system.Three grades of chemicals dosing plants are same set of chemicals dosing plant, and automatic control flow is thrown in respectively, can send alarm when dose is not enough.The leaching technology of microorganism applies the direct effect of specific microorganism or the heavy metal ion in solid phase material is dissolved the process discharging into liquid phase by redox complexing acidolysis etc. by the indirectly-acting of its metabolin under normal temperature and pressure conditions.
In bundle glue strengthening removal heavy metal system of the present invention, because incineration of refuse flyash contains many kinds of metal ions, coagulative precipitation tank adds solution mass ratio when stirring is the anion active agent of one thousandth to thousand/five, large molecule is formed thus precipitation after impelling the Van der Waals force polymerization between multiple dispersed metal ion, after static half an hour to one hour after most heavy metal ion precipitation, get supernatant and enter the heavy metal that composite bag type filter will not precipitate completely, contaminant filter falls.Coagulative precipitation tank precipitation enter mud collecting pit carry out pre-mummification laggard enter cement kiln burn, thus solve the pollution of incineration of refuse flyash heavy metal.In this system anion active agent after adding again sedimentation and filtration fall, therefore do not cause the secondary pollution of solution, to subsequent film system, evaporative crystallization etc. do not impact and obtain harmlessness disposing.
In nanofiltration system of the present invention, because of in the washing water after flying dust washing, containing a large amount of calcium ions and magnesium ions, make the blocking that can cause subsequent film system after concentrating.The separating mechanism of NF membrane is for screening and dissolve and spread and deposit, while there is again electrical charge rejection effect, effectively can remove all kinds of materials that divalence and multivalent ion, removal molecular weight are greater than 200, can partly remove monovalention and molecular weight lower than 200 material; The separating property of NF membrane is obviously better than ultrafiltration and micro-filtration, and first removed by the residue calcium magnesium in washing water with nanofiltration, the water of the dilute side of output enters intermediate water tank, can enter in counter-infiltration preconcentration technique.
In counter-infiltration preconcentration technique of the present invention, being motive force with pressure differential, is a kind of UF membrane operation of isolating solvent from solution, because it is contrary with the direction of naturally osmotic, therefore claims counter-infiltration.According to the different osmotic of various material, just can use the reverse osmosis pressure being greater than osmotic pressure, i.e. hyperfiltration, reach separation, extraction, purifying and concentrated object.Through the water of removing hardness, directly can enter counter-infiltration, by counter-infiltration pre-concentration, 6%-8% can be concentrated into washing water.The condensed water of output can enter membrane distillation concentration system, and the fresh water of output can enter water wash system water scouring water.
Membrane distillation concentration system of the present invention adopts Membrane Materials to carry out the chlorion of saliferous rate 6-8% in Treatment Solution, and make the distilled water reusable edible of generation, distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing, a large amount of distilled water enters water wash system, reducing the water yield of washing and consuming greatly, is that totally the ratio of washing reduces between 1:3-1:5.
Of the present inventionly go denier carnallite system can remove denier carnallite and carried out the recycling of the energy, due to the uncertainty of each supplied materials of incineration of refuse flyash, the blocking of the crystallizer that avoids evaporating, therefore set up before evaporative crystallization and go denier carnallite system.Carry out high temperature (temperature is upgraded to 80-110 DEG C) process after the dope of concentrated water tank enters flat ultra micro water filtration film one-level carnallite release unit the carnallite of high temperature section is removed, after utilize absorption principle to be removed by carnallite further through secondary carnallite release unit, the carnallite Song Weifei factory and office reason filtered out, processing cost is very low.
MVR evaporation and crystallization system of the present invention is also less because being concentrated into the nearly saturation state water yield through Membrane Materials system dope, so select forced-circulation evaporation crystallizer, dope enters evaporating chamber, heat exchanger passes into live steam and heats dope, in dope evaporation process two sections of steam of output can enter Roots's steam recompression machine steam temperature rise is continued enter heat exchanger to dope heating evaporation, original vol saturated vapor is supplemented without the need to continuing, dope carries out evaporation and reaches hypersaturated state crystallize out, then enter suction filtration tank from evaporating chamber discharge and carry out Separation of Solid and Liquid, mother liquor is got back to evaporating chamber and is continued evaporative crystallization.Because removing a large amount of carnallite, evaporative crystallization salt out contains sodium chloride and reaches more than 76% and can be used for papermaking, snow melting agent etc., processes this system and utilizes Roots's steam recompression technology, greatly save operation energy consumption.
Accompanying drawing illustrates:
Below in conjunction with accompanying drawing, the present invention is described further:
Fig. 1 is system flow chart of the present invention;
Fig. 2 is the flow chart of incineration of refuse flyash tertiary effluent salt elution system of the present invention;
Fig. 3 is the flow chart of bundle glue of the present invention strengthening removal heavy metal system;
Fig. 4 is the flow chart of nanofiltration system of the present invention and counter-infiltration preconcentration technique;
Fig. 5 is the flow chart of membrane distillation concentration system of the present invention;
Fig. 6 is the flow chart going denier carnallite system of the present invention;
Fig. 7 is the flow chart of MVR evaporation and crystallization system of the present invention.
Detailed description of the invention:
Embodiment, see accompanying drawing 1 ~ 7, a kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, it comprise connect successively incineration of refuse flyash tertiary effluent salt elution system I, coagulating sedimentation removal heavy metal system II, sodium filter III and counter-infiltration preconcentration technique IV, membrane distillation concentration system V, go denier carnallite system VI and MVR evaporation and crystallization system VII; The washing water of described incineration of refuse flyash tertiary effluent salt elution system produce enters coagulating sedimentation removal heavy metal system by pipeline; The saliferous rate that coagulating sedimentation removal heavy metal system obtains is that the solution of 1-2% enters sodium filter and counter-infiltration preconcentration technique; Described sodium filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, be the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into membrane distillation concentration system and carries out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing; The saliferous rate of described membrane distillation concentration system produce is that the nearly saturated solution of 20%-30% enters denier carnallite system and removed by carnallite, and last nearly saturated solution enters MVR evaporation and crystallization system and carries out evaporative crystallization.
Described incineration of refuse flyash tertiary effluent salt elution system it comprise flying dust storage 1, the lower end of described flying dust storage is communicated with conveying worm a2, the outlet of described conveying worm is connected to first order washing desalter, and first order washing desalter comprises agitator tank a3; Add certain water gaging, and the weight ratio of flying dust and water is 1:3, flying dust 1000kg, water 3000kg, described agitator tank a is communicated with respectively water inlet pipe a4 and chemical feed pipe a5; The volume of agitator tank a is 1.35m
3the power of agitator tank a is 2.2kw, and to add quality in whipping process be that the chaotropic agent of 1% of flying dust carries out stirring 20 minutes, flying dust in described agitator tank a, water become mud with medicinal liquid agitating, the lower end of agitator tank a is connected to slush pump a6, the power of slush pump a is 5.5kw, and transfer rate is 0 ~ 50m
3/ h, the mud in agitator tank a is conveyed into buffer tank a7 by slush pump a, and the power of buffer tank a is 0.75kw, and the volume of buffer tank a is 1.35m
3; Mud in buffer tank a is conveyed into horizontal centrifuge a9 by slush pump b8 and dewaters; Mud is isolated the flying dust of chloro ion-containing solution and moisture Ji bioxin by described horizontal centrifuge a, the moisture content of the flying dust of moisture Ji bioxin is 40%-50%, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and moisture content is that the flying dust of the moisture of 40%-50% and bioxin enters second level washing desalter; Chloro ion-containing solution mud isolated by described second level washing desalter and secondary is moisture and the flying dust of bioxin, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and secondary flying dust that is moisture and bioxin enters third level washing desalter; The flying dust of chloro ion-containing solution and three moisture and bioxin isolated by third level washing desalter, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, the flying dust of three moisture Ji bioxin enters cement kiln, and after cement kiln burns, flying dust becomes cement raw material.
The charging aperture of described horizontal centrifuge a is connected to the discharging opening of slush pump b; The slag notch of described horizontal centrifuge a is connected to conveying worm b10, and the liquid outlet of horizontal centrifuge a is connected to the agitator tank d in coagulating sedimentation removal heavy metal system by fluid pipeline 11, the washing water in agitator tank d enters coagulative precipitation tank 12 and processes; Described conveying worm b is provided with two discharging openings; Described second level washing desalter comprises agitator tank b13, the flying dust of moisture Ji bioxin is conveyed into agitator tank b through conveying worm b, and carrying out stirring washing with the weight ratio of initial flying dust and water for 1:3 adds water, adding quality in whipping process is that the chaotropic agent of 1% of initial flying dust carries out stirring 30 minutes; Stir fully and obtain secondary mud; The discharging opening of each conveying worm b is connected to an agitator tank b, and the power of each agitator tank b is 2.2KW, and volume is 0.8m
3, stir fully and obtain secondary mud, the slurries in each agitator tank b send into buffer tank b15 through slush pump c14, and the power of slush pump c is 5.5kw, and transfer rate is 0 ~ 50m
3the power of/h, buffer tank b is 0.75kw, and the volume of buffer tank a is 1.35m
3, the slurry in buffer tank b is sent into horizontal centrifuge b17 through slush pump d16 and is dewatered; The power of slush pump d is 1.5kw, and transfer rate is 0 ~ 1.2m
3/ h.
The slag notch of described horizontal centrifuge b is connected to conveying worm c18, and the liquid outlet of horizontal centrifuge b is connected to coagulating sedimentation removal heavy metal system by fluid pipeline; Described conveying worm c is provided with two discharging openings; Third level washing desalter comprises agitator tank c19, the discharging opening of each conveying worm c is connected to an agitator tank c, slurries in each agitator tank c send into buffer tank c21 through slush pump e20, slurry in buffer tank c is sent into horizontal centrifuge c through slush pump f and is dewatered, and the charging aperture of described horizontal centrifuge c is connected to the discharging opening of slush pump f22; The slag notch of described horizontal centrifuge c is connected to cement kiln, mud is isolated the flying dust of chloro ion-containing solution and the moisture Ji bioxin of secondary, the moisture content of the flying dust of the moisture Ji bioxin of secondary is 40%-50%, chloro ion-containing solution enters coagulative precipitation tank, and the flying dust of the moisture Ji bioxin of secondary enters agitator tank c.The fly ash carry of the moisture Ji bioxin of secondary to agitator tank c, and carries out stirring washing with the weight ratio of initial flying dust and water for 1:2 adds water, and adding quality in whipping process is that the chaotropic agent of 1% of initial flying dust carries out stirring 20 minutes; Stirring fully and obtain three mud. three mud enter horizontal centrifuge c23 and dewater, and the charging aperture of horizontal centrifuge c is connected to the discharging opening of slush pump f; The slag notch of described horizontal centrifuge c is connected to cement kiln 24.Mud is isolated the flying dust of chloro ion-containing solution and three moisture Ji bioxin, the moisture content of the flying dust of three moisture Ji bioxin is 40%-50%, chloro ion-containing solution enters coagulative precipitation tank, the flying dust of three moisture Ji bioxin and chloride ion-containing enter lower than the flying dust of 1% heavy metal that mud collecting pit carries out in microbial attack bioxin and ash, flying dust through microbial attack bioxin can directly as the raw material of construction material, this microorganism is reusable, and the tertiary effluent namely completing flying dust and water yield 1:8 washes system.
Described each agitator tank b is connected to water inlet pipe b, each agitator tank c is connected to water inlet pipe c, described water inlet pipe a, water inlet pipe b are connected with inlet water tank 25 respectively with water inlet pipe c; Described each agitator tank b is connected to chemical feed pipe b, each agitator tank c is connected to chemical feed pipe c, described chemical feed pipe a, chemical feed pipe b and chemical feed pipe c are connected on chemicals dosing plant 26; The flow that the liquid outlet parallel join of described chemicals dosing plant has three groups of automatic control flow devices, 27, three groups of automatic control flow devices to control in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, can send alarm when dose is not enough.
Described coagulating sedimentation removal heavy metal system comprises coagulative precipitation tank 12, and the left end of described coagulative precipitation tank is connected to two agitator tank d29 by delivery pump a28, and each agitator tank d is communicated with liquid-feeding tube 30 and chemical feed pipe 31; Liquid-feeding tube place enters tertiary effluent and washes rear chloro ion-containing solution, chemical feed pipe place adds anion active agent and stirs, and the quality of anion active agent accounts for 1 ‰ ~ 5 ‰ of chloro ion-containing solution quality, large molecule is formed thus precipitation after making multiple dispersed metal ionic polymerization, after static 0.5 ~ 1 hour, the heavy metal ion of 85 ~ 95% is precipitated; Liquid-feeding tube is provided with priming valve 32, chemical feed pipe is provided with the dosing valve 33 controlling dosing flow.Described chemical feed pipe is connected with chemicals dosing plant 35 by dosing pump 34, and the power of dosing pump is 0.37KW, and chemicals dosing plant is connected with water pipe 36, and the nearly running water in water pipe place is convenient to mix with liquid, described coagulative precipitation tank bottom is connected with centrifugal dehydrator 37, coagulative precipitation tank top is connected with Buffer Pool 38, Buffer Pool is connected to delivery pump b39, delivery pump b is connected to composite bag type filter 40, composite bag type filter has two, each composite bag type filter top is provided with inlet, bottom is provided with liquid outlet, lower end is provided with sewage draining exit, the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter, the heavy metal obtained and impurity transport into centrifugal dehydrator by sewage draining exit and dewater, the saliferous rate obtained is that the solution of 1-2% enters next treatment system by liquid outlet, the clear liquid on coagulative precipitation tank top is conveyed into Buffer Pool, and the liquid in Buffer Pool is conveyed into composite bag type filter by delivery pump b, and the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter.
Described sodium filter and counter-infiltration preconcentration technique comprise sodium filter assembly 41, described sodium filter assembly is communicated with chemicals dosing plant a, and chemicals dosing plant a is connected with water pipe a; Chemicals dosing plant a enters antisludging agent, and the water inlet end of described sodium filter assembly is connected to filter a, and the condensed water of sodium filter assembly output is connected to intermediate water tank 42 by pipeline, and the fresh water of sodium filter assembly output is connected to counter-infiltration water tank by pipeline; The bottom of described intermediate water tank is connected to feeding engine a, and the water side of feeding engine a is connected to filter b, and the port of export of filter b is connected to counter-infiltration pre-concentration device 43; Described counter-infiltration pre-concentration device is communicated with chemicals dosing plant b, and chemicals dosing plant b is connected with water pipe b; The condensed water of described counter-infiltration pre-concentration device output is connected in Membrane Materials system by water pipe, and the fresh water of counter-infiltration pre-concentration device output is connected in counter-infiltration water tank by water pipe.The water of intermediate water tank is sent into reverse osmosis membrane assembly 43 with feeding engine again and is carried out counter-infiltration pre-concentration, enter antisludging agent by chemicals dosing plant c in reverse osmosis membrane assembly simultaneously, water can be concentrated into 6% ~ 8% by reverse osmosis membrane assembly, reverse osmosis membrane assembly output fresh water enters reverse osmosis produced water tank, and the water in reverse osmosis produced water tank can enter incineration of refuse flyash washing moisturizing and use.
Described membrane distillation concentration system comprises heating water tank 44, and the volume of heating water tank is 16m
3, described heating water tank is connected with volumetric heat exchanger, and the upper end of heating water tank is communicated with feed tube, feed tube is provided with charging valve a; The lower end of heating water tank is communicated with two groups of operating water tanks 45 side by side by feeding engine, and the volume of operating water tank is 8m
3, the power of feeding engine is 4KW, and flow is 80m
3/ h, and charging line between heating water tank and operating water tank is provided with charging valve b.
The outlet pipe often organizing described operating water tank is connected to hot water inlet pipe and the concentrated water tank 47 of distillation device 46 simultaneously by feeding circulating pump, the volume of concentrated water tank is 3m
3, hot water inlet pipe is provided with distillation ball valve, the water inlet pipe of concentrated water tank is provided with Filtering ball valve, and the power of feeding circulating pump is 4KW, and flow is 54m
3/ h, often organizes on described operating water tank and is connected with dope evacuated tube and dope return pipe.Include the 12 groups of membrane modules be connected in parallel in described distillation device, each group membrane module is in series by 4 Membrane Materials devices, and the temperature entering the hot water of distillation device is 67 DEG C.Its membrane module adopts a kind of normal pressure anti-soil of Huzhou Sen Nuo membrane technology Engineering Co., Ltd to block up energy-saving Membrane Materials device, and the patent No. is 201420465882.4.
The hot water outlet pipe of described distillation device is connected to dope return pipe, and the hot water temperature that hot water outlet pipe is flowed out is 57 DEG C, and the hot water that hot water outlet pipe is flowed out gets back to operating water tank by dope return pipe again, recycles.
The cold water inlet tube of described distillation device is connected to cooling tower, and cooling tower is connected with CWR, and the cooling water outlet pipe of distillation device is connected to CWR; The cold water temperature that cold water inlet tube enters is 25 DEG C, and the temperature of cooling water outlet pipe water is out 35 DEG C, and cooling water outlet pipe water out gets back to cooling tower by CWR again, and the water cooling of 35 DEG C to 25 DEG C, then continues to recycle by cooling tower.
The condensate pipe of described distillation device is connected to and produces water tank 48, and the volume producing water tank is 2m
3, the condensed water producing water tank is used for membrane module backwash and incineration of refuse flyash washing moisturizing, and a large amount of distilled water recoverables, saves water resource.
Described distillation device top is connected with backwash water feed pipe, and distillation device bottom is connected with backwash water evacuated tube and dope evacuated tube a, and backwash water feed pipe is connected to backwash water tank 49 by backwashing pump, and the volume of backwash water tank is 3m
3, and backwash water tank and backwash water evacuated tube link together, and the dope evacuated tube on dope evacuated tube a and operating water tank links together.
Saliferous rate is that the solution of 6-8% delivers into heating water tank, and use volumetric heat exchanger to utilize plant area's waste heat to heat to solution, after solution temperature rise to 70 °, solution enters operating water tank; Then solution enters distillation device and circulates, solution undergoes phase transition in membrane module, steam is by the film pipe in Membrane Materials device, distilled water is become again by the corrosion-resistant condensing tube condensation that thermal conductivity factor is high, distilled water enters product water tank, and distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing; Along with the minimizing of water in solution, solution concentration is increasing, after solution concentration reaches the nearly saturation state of saliferous rate 20%-30%, solution does not circulate, nearly saturated solution enters operating water tank, operating water tank reaches liquid level lower limit position, and Liquid Residue in membrane module and condensation pipe is all entered concentrated water tank by self priming pump startup; Emptying rear backwash starts, and carry out backwash by the distilled water produced to membrane module, backwash pipeline enters by membrane module is suitable for reading, discharges, the micro-crystalline solid adhered to cleaned in distillation device from end opening; In backwash process, heating water tank carries out stopping fluid infusion after fluid infusion reaches liquid level upper limit position place to operating water tank, and after backwash terminates, it is concentrated that operating water tank carries out next one circulation.
Described denier carnallite system of going comprises concentrate case 50, the water of the concentrated water tank in membrane distillation concentration system enters concentrate case, the upper end of described concentrate case is communicated with feed tube, the lower end of described concentrate case is communicated with drain pipe, described drain pipe is connected with and is separated feeding engine 51, the discharge nozzle being separated feeding engine divides two-way, every road discharge nozzle is connected to separation ball valve, for being separated ball valve a52 and being separated ball valve b53, be separated ball valve a and be connected to one-level carnallite release unit 54, be separated ball valve b and be connected to secondary carnallite release unit 55; The lower end of described one-level carnallite release unit is connected to carnallite collecting pit 56, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c57, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a58 is connected with concentrated material returning valve 59; The upper end of described secondary carnallite release unit is connected to and is separated ball valve d60, and be separated ball valve d and be connected to pipeline a and pipeline b61 simultaneously, pipeline b is connected with crystallization and evaporation valve 62, crystallization and evaporation valve is connected to MVR evaporation and crystallization system.
Heat up after the dope of concentrated water tank enters flat ultra micro water filtration film one-level carnallite release unit by separation feeding engine, temperature is upgraded to 80-110 DEG C and carries out high temperature circulation process 5 ~ 10 minutes, the carnallite of high temperature section is removed, carnallite precipitation enters carnallite collecting pit, and the dope obtained turns back to concentrated water tank by dope material returning valve; Then the dope obtained through the process of one-level carnallite release unit in concentrated water tank to be sent in secondary carnallite release unit circular treatment 5 ~ 10 minutes, utilize absorption principle to be removed by carnallite further, make to heat up and enter MVR evaporation and crystallization system except carnallite dope obtains heat and carry out evaporative crystallization.
Described MVR evaporation and crystallization system comprises feeding engine d63, and feeding engine d is connected to evaporating chamber 64, described evaporating chamber is communicated with heat exchanger 65, heat exchanger is connected with steam recompression pump 66; The bottom of described evaporating chamber is connected with suction filtration tank 68 by discharging pump d67, and the top of evaporating chamber is connected to Roots's steam recompression machine 69 by pipeline; In described Roots's steam recompression machine, vavuum pump 70 is installed; Described vavuum pump is connected to filtrate tank 71, filtrate tank is connected with suction filtration tank, and vavuum pump and steam recompress pump links together, the mother liquor under vavuum pump effect in filtrate tank is negative pressure state, and the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization.
First evaporating chamber is entered by feeding engine d by the dope going denier carnallite technique to obtain, heat exchanger passes into live steam and heats dope, in dope evaporation process two sections of steam of output can enter Roots's steam recompression machine by vapor (steam) temperature raise continue to enter heat exchanger to dope heating evaporation, supplement original vol saturated vapor without the need to continuing, the water that Roots's steam recompression machine produces enters condensation water tank 72.Dope carries out evaporation and reaches hypersaturated state crystallize out, then enter suction filtration tank from evaporating chamber by discharging pump d discharge and carry out Separation of Solid and Liquid, vavuum pump is provided with in Roots's steam recompression machine, vavuum pump filtrate tank connects, mother liquor under vavuum pump effect in filtrate tank is negative pressure state, the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization, and evaporative crystallization salt out contains sodium chloride and reaches more than 76% and can be used for papermaking, snow melting agent or chlor-alkali industry.
Above-described embodiment is the specific descriptions of carrying out the present invention; just the present invention is further described; can not be interpreted as limiting the scope of the present invention, those skilled in the art makes some nonessential improvement according to the content of foregoing invention and adjustment all falls within protection scope of the present invention.
Claims (10)
1. garbage flying ash cement kiln synergic processing and recycling of water resource utilize a system, it is characterized in that: it comprises the incineration of refuse flyash tertiary effluent salt elution system, coagulating sedimentation removal heavy metal system, the sodium filter that connect successively and counter-infiltration preconcentration technique, membrane distillation concentration system, goes denier carnallite system and MVR evaporation and crystallization system; The washing water of described incineration of refuse flyash tertiary effluent salt elution system produce enters coagulating sedimentation removal heavy metal system by pipeline; The saliferous rate that coagulating sedimentation removal heavy metal system obtains is that the solution of 1-2% enters sodium filter and counter-infiltration preconcentration technique; Described sodium filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, be the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into membrane distillation concentration system and carries out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing; The saliferous rate of described membrane distillation concentration system produce is that the nearly saturated solution of 20%-30% enters denier carnallite system and removed by carnallite, and last nearly saturated solution enters MVR evaporation and crystallization system and carries out evaporative crystallization.
2. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described incineration of refuse flyash tertiary effluent salt elution system it comprise flying dust storage, the lower end of described flying dust storage is communicated with conveying worm a, the outlet of described conveying worm is connected to first order washing desalter, and first order washing desalter comprises agitator tank a; Described agitator tank a is communicated with respectively water inlet pipe a and chemical feed pipe a; Flying dust in described agitator tank a, water become mud with medicinal liquid agitating, the lower end of agitator tank a is connected to slush pump a, mud in agitator tank a is conveyed into buffer tank a by slush pump a, and the mud in buffer tank a is conveyed into horizontal centrifuge a by slush pump b and dewaters; Mud is isolated chloro ion-containing solution and flying dust that is moisture and bioxin by described horizontal centrifuge a, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and flying dust that is moisture and bioxin enters second level washing desalter; Chloro ion-containing solution mud isolated by described second level washing desalter and secondary is moisture and the flying dust of bioxin, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and secondary flying dust that is moisture and bioxin enters third level washing desalter; The flying dust of chloro ion-containing solution and three moisture and bioxin isolated by third level washing desalter, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, the flying dust of three moisture Ji bioxin enters cement kiln, and after cement kiln burns, flying dust becomes cement raw material.
3. a kind of garbage flying ash cement kiln synergic processing according to claim 2 and recycling of water resource utilize system, it is characterized in that: the charging aperture of described horizontal centrifuge a is connected to the discharging opening of slush pump b; The slag notch of described horizontal centrifuge a is connected to conveying worm b, and the liquid outlet of horizontal centrifuge a is connected to coagulating sedimentation removal heavy metal system by fluid pipeline; Described conveying worm b is provided with two discharging openings; Described second level washing desalter comprises agitator tank b, the discharging opening of each conveying worm b is connected to an agitator tank b, slurries in each agitator tank b send into buffer tank b through slush pump c, and the slurry in buffer tank b is sent into horizontal centrifuge b through slush pump d and dewatered; The slag notch of described horizontal centrifuge b is connected to conveying worm c, and the liquid outlet of horizontal centrifuge b is connected to coagulative precipitation tank by fluid pipeline; Described conveying worm c is provided with two discharging openings; Third level washing desalter comprises agitator tank c, the discharging opening of each conveying worm c is connected to an agitator tank c, slurries in each agitator tank c send into buffer tank c through slush pump e, slurry in buffer tank c is sent into horizontal centrifuge c through slush pump f and is dewatered, and the charging aperture of described horizontal centrifuge c is connected to the discharging opening of slush pump f; The slag notch of described horizontal centrifuge c is connected to cement kiln.
4. a kind of garbage flying ash cement kiln synergic processing according to claim 3 and recycling of water resource utilize system, it is characterized in that: described each agitator tank b is connected to water inlet pipe b, each agitator tank c is connected to water inlet pipe c, and described water inlet pipe a, water inlet pipe b are connected with inlet water tank respectively with water inlet pipe c; Described each agitator tank b is connected to chemical feed pipe b, each agitator tank c is connected to chemical feed pipe c, described chemical feed pipe a, chemical feed pipe b and chemical feed pipe c are connected on chemicals dosing plant; The liquid outlet parallel join of described chemicals dosing plant has three groups of automatic control flow devices, and three groups of automatic control flow devices control the flow in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, can send alarm when dose is not enough.
5. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described coagulating sedimentation removal heavy metal system comprises coagulative precipitation tank, the left end of described coagulative precipitation tank is connected to two agitator tank d by delivery pump a, and each agitator tank d is communicated with liquid-feeding tube and chemical feed pipe; Described chemical feed pipe is connected with chemicals dosing plant by dosing pump, and chemicals dosing plant is connected with water pipe; Described coagulative precipitation tank bottom is connected with centrifugal dehydrator, and coagulative precipitation tank top is connected with Buffer Pool, and Buffer Pool is connected to delivery pump b, and delivery pump b is connected to composite bag type filter, and composite bag type filter lower end is connected to centrifugal dehydrator; The heavy metal precipitation thing of coagulative precipitation tank bottom transports into centrifugal dehydrator and dewaters, the clear liquid on coagulative precipitation tank top is conveyed into Buffer Pool, liquid in Buffer Pool is conveyed into composite bag type filter by delivery pump b, the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter, the heavy metal obtained and impurity transport into centrifugal dehydrator and dewater, and the saliferous rate obtained is that the solution of 8-15% enters membrane distillation concentration device and carries out desalting processing.
6. a kind of garbage flying ash cement kiln synergic processing according to claim 5 and recycling of water resource utilize system, it is characterized in that: described chemical feed pipe is provided with the dosing valve controlling dosing flow; Described liquid-feeding tube is provided with priming valve.
7. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described sodium filter and counter-infiltration preconcentration technique comprise sodium filter assembly, described sodium filter assembly is communicated with chemicals dosing plant a, and chemicals dosing plant a is connected with water pipe a; The water inlet end of described sodium filter assembly is connected to filter a, and the condensed water of sodium filter assembly output is connected to intermediate water tank by pipeline, and the fresh water of sodium filter assembly output is connected to counter-infiltration water tank by pipeline; The bottom of described intermediate water tank is connected to feeding engine a, and the water side of feeding engine a is connected to filter b, and the port of export of filter b is connected to counter-infiltration pre-concentration device; Described counter-infiltration pre-concentration device is communicated with chemicals dosing plant b, and chemicals dosing plant b is connected with water pipe b; The condensed water of described counter-infiltration pre-concentration device output is connected in Membrane Materials system by water pipe, and the fresh water of counter-infiltration pre-concentration device output is connected in counter-infiltration water tank by water pipe.
8. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described membrane distillation concentration system comprises heating water tank, described heating water tank is connected with volumetric heat exchanger, the upper end of heating water tank is communicated with feed tube, and the lower end of heating water tank is communicated with two groups of operating water tanks side by side by feeding engine; The outlet pipe often organizing described operating water tank is connected to the hot water inlet pipe of distillation device and concentrated water tank by feeding circulating pump simultaneously, often organize on described operating water tank and be connected with dope evacuated tube and dope return pipe, the hot water outlet pipe of described distillation device is connected to dope return pipe; The cold water inlet tube of described distillation device is connected to cooling tower, and cooling tower is connected with CWR, and the cooling water outlet pipe of distillation device is connected to CWR; The condensate pipe of described distillation device is connected to product water tank; Described distillation device top is connected with backwash water feed pipe, distillation device bottom is connected with backwash water evacuated tube and dope evacuated tube a, backwash water feed pipe is connected to backwash water tank by backwashing pump, and backwash water tank and backwash water evacuated tube link together, the dope evacuated tube on dope evacuated tube a and operating water tank links together.
9. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described in go denier carnallite system to comprise concentrate case, the upper end of described concentrate case is communicated with feed tube, the lower end of described concentrate case is communicated with drain pipe, described drain pipe is connected with separation feeding engine, the discharge nozzle being separated feeding engine divides two-way, every road discharge nozzle is connected to separation ball valve, for being separated ball valve a and being separated ball valve b, be separated ball valve a and be connected to one-level carnallite release unit, be separated ball valve b and be connected to secondary carnallite release unit, the lower end of described one-level carnallite release unit is connected to carnallite collecting pit, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a is connected with concentrated material returning valve, the upper end of described secondary carnallite release unit is connected to and is separated ball valve d, and be separated ball valve d and be connected to pipeline a and pipeline b simultaneously, pipeline b is connected with crystallization and evaporation valve, crystallization and evaporation valve is connected to MVR evaporation and crystallization system.
10. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described MVR evaporation and crystallization system comprises feeding engine d, feeding engine d is connected to evaporating chamber, described evaporating chamber is communicated with heat exchanger, heat exchanger is connected with steam recompression pump; The bottom of described evaporating chamber is connected with suction filtration tank by discharging pump d, and the top of evaporating chamber is connected to Roots's steam recompression machine by pipeline; In described Roots's steam recompression machine, vavuum pump is installed; Described vavuum pump is connected to filtrate tank, filtrate tank is connected with suction filtration tank, and vavuum pump and steam recompress pump links together, the mother liquor under vavuum pump effect in filtrate tank is negative pressure state, and the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111265809A (en) * | 2020-03-29 | 2020-06-12 | 浙江红狮环保股份有限公司 | Preparation and application of high-chlorine fly ash washing agent |
| CN111589837A (en) * | 2020-04-12 | 2020-08-28 | 北京锐上思环保科技有限公司 | Reinforced desalting method for water washing pretreatment of fly ash |
| CN113023989A (en) * | 2021-03-13 | 2021-06-25 | 宝钢湛江钢铁有限公司 | Method for treating silicon-containing sludge by using wastewater zero discharge system |
| CN113231446A (en) * | 2021-05-24 | 2021-08-10 | 南京工业大学 | Treatment and disposal system for incineration fly ash of household garbage |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1724413A (en) * | 2005-06-24 | 2006-01-25 | 华南理工大学 | Process for degrading high chlorodioxin kinds pollutant by combined biological ecological system |
| CN104084415A (en) * | 2014-07-02 | 2014-10-08 | 天津壹鸣环境工程有限公司 | Technology for reducing waste incineration fly ash via water logging pretreatment |
| JP2015031661A (en) * | 2013-08-06 | 2015-02-16 | 株式会社神鋼環境ソリューション | Method for cleaning incineration fly ash |
| CN104803537A (en) * | 2015-05-11 | 2015-07-29 | 北京中科国润环保科技有限公司 | Washing softening technology for MSWI (Municipal Solid Waste Incineration) fly ash |
| CN204912255U (en) * | 2015-08-25 | 2015-12-30 | 湖州森诺膜技术工程有限公司 | Rubbish flying dust cement kiln is dealt with and water utilization system in coordination |
-
2015
- 2015-08-25 CN CN201510525997.7A patent/CN105080935B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1724413A (en) * | 2005-06-24 | 2006-01-25 | 华南理工大学 | Process for degrading high chlorodioxin kinds pollutant by combined biological ecological system |
| JP2015031661A (en) * | 2013-08-06 | 2015-02-16 | 株式会社神鋼環境ソリューション | Method for cleaning incineration fly ash |
| CN104084415A (en) * | 2014-07-02 | 2014-10-08 | 天津壹鸣环境工程有限公司 | Technology for reducing waste incineration fly ash via water logging pretreatment |
| CN104803537A (en) * | 2015-05-11 | 2015-07-29 | 北京中科国润环保科技有限公司 | Washing softening technology for MSWI (Municipal Solid Waste Incineration) fly ash |
| CN204912255U (en) * | 2015-08-25 | 2015-12-30 | 湖州森诺膜技术工程有限公司 | Rubbish flying dust cement kiln is dealt with and water utilization system in coordination |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111265809A (en) * | 2020-03-29 | 2020-06-12 | 浙江红狮环保股份有限公司 | Preparation and application of high-chlorine fly ash washing agent |
| CN111589837A (en) * | 2020-04-12 | 2020-08-28 | 北京锐上思环保科技有限公司 | Reinforced desalting method for water washing pretreatment of fly ash |
| CN113023989A (en) * | 2021-03-13 | 2021-06-25 | 宝钢湛江钢铁有限公司 | Method for treating silicon-containing sludge by using wastewater zero discharge system |
| CN113231446A (en) * | 2021-05-24 | 2021-08-10 | 南京工业大学 | Treatment and disposal system for incineration fly ash of household garbage |
| CN113231446B (en) * | 2021-05-24 | 2022-08-12 | 南京工业大学 | Treatment and disposal system for incineration fly ash of household garbage |
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