CN105107820A - Cement kiln co-processing system for waste incineration fly ash - Google Patents
Cement kiln co-processing system for waste incineration fly ash Download PDFInfo
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- CN105107820A CN105107820A CN201510524264.1A CN201510524264A CN105107820A CN 105107820 A CN105107820 A CN 105107820A CN 201510524264 A CN201510524264 A CN 201510524264A CN 105107820 A CN105107820 A CN 105107820A
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Abstract
The invention relates to a cement kiln co-processing system for waste incineration fly ash. Washing water generated by a waste incineration fly ash three-stage washing desalination system enters a coagulating sedimentation heavy-metal removal system through a pipeline; a solution with the salt content of 1-2 percent, obtained by the coagulating sedimentation heavy-metal removal system, enters a sodium filtration and reverse osmosis pre-concentration system; and the sodium filtration and reverse osmosis pre-concentration system removes calcium and magnesium ions in washing water and concentrates the solution with the salt content of 1-2 percent into a concentrated liquor with the salt content of 6-8 percent, which is conveyed into a slight trace carnallite removal system for carnallite removal, and finally, a nearly saturated liquid enters an MVR (Mechanical Vapor Recompression) evaporative crystallization system for evaporative crystallization. The cement kiln co-processing system for waste incineration fly ash is a device for cement kiln co-processing of waste incineration fly ash, can dispose a great amount of fly ash, is high in cement output, realizes innocent treatment, and obtains industrial salt through evaporative crystallization, which is used in paper making process, snow-melting agents and the chlor-alkali industry.
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 system in particular.
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, there is provided a kind of garbage flying ash cement kiln synergic processing system, achieve the innoxious of flying dust and recycling treatment, flying ash can meet the raw materials used standard of manufacture of cement, can dispose flying dust in a large number, manufacture of cement amount is large.
Technology solution of the present invention is as follows:
A kind of garbage flying ash cement kiln synergic processing 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, 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, it is the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into denier carnallite system and is 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 1-2% enters next system and processes.
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 recoverable of described counter-infiltration pre-concentration device output, the fresh water of counter-infiltration pre-concentration device output is connected in counter-infiltration water tank by water pipe.
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 recoverable of output, the fresh water of output can enter water wash system water scouring water.
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.
The nearly saturation state water yield is also less because dope has been concentrated into for MVR evaporation and crystallization system of the present invention, 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 going denier carnallite system of the present invention;
Fig. 6 is the flow chart of MVR evaporation and crystallization system of the present invention.
Detailed description of the invention:
Embodiment, see accompanying drawing 1 ~ 6, a kind of garbage flying ash cement kiln synergic processing 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, go denier carnallite system V, MVR evaporation and crystallization system VI; 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, it is the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into denier carnallite system and is 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 recoverable of described counter-infiltration pre-concentration device output, 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 denier carnallite system of going comprises concentrate case 44, 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 45, the discharge nozzle being separated feeding engine divides two-way, and every road discharge nozzle is connected to separation ball valve, for being separated ball valve a46 and being separated ball valve b47, be separated ball valve a and be connected to one-level carnallite release unit 48, be separated ball valve b and be connected to secondary carnallite release unit 49; The lower end of described one-level carnallite release unit is connected to carnallite collecting pit 50, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c51, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a52 is connected with concentrated material returning valve 53; The upper end of described secondary carnallite release unit is connected to and is separated ball valve d54, and be separated ball valve d and be connected to pipeline a and pipeline b55 simultaneously, pipeline b is connected with crystallization and evaporation valve 56, 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 d57, and feeding engine d is connected to evaporating chamber 58, described evaporating chamber is communicated with heat exchanger 59, heat exchanger is connected with steam recompression pump 60; The bottom of described evaporating chamber is connected with suction filtration tank 62 by discharging pump d61, and the top of evaporating chamber is connected to Roots's steam recompression machine 63 by pipeline; In described Roots's steam recompression machine, vavuum pump 64 is installed; Described vavuum pump is connected to filtrate tank 65, 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 66.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 (9)
1. a garbage flying ash cement kiln synergic processing system, 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, 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, it is the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into denier carnallite system and is 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 system according to claim 1, 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 system according to claim 2, 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 system according to claim 3, 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 system according to claim 1, 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 1-1% enters next step process.
6. a kind of garbage flying ash cement kiln synergic processing system according to claim 5, 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 system according to claim 1, 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 recycled 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 system according to claim 1, 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.
9. a kind of garbage flying ash cement kiln synergic processing system according to claim 1, it is characterized in that: described MVR evaporation and crystallization system comprises feeding engine d, 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.
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| CN107309251A (en) * | 2017-08-07 | 2017-11-03 | 安徽今朝环保科技有限公司 | The innoxious transhipment of industrial slag salt, processing unit and application method |
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| CN109054750A (en) * | 2018-09-17 | 2018-12-21 | 丁仲军 | A kind of technique using garbage flying ash preparation deicing salt |
| CN109054750B (en) * | 2018-09-17 | 2021-03-02 | 杭州秀澈环保科技有限公司 | Process for preparing snow-melting agent by utilizing garbage fly ash |
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| CN112030000A (en) * | 2020-08-18 | 2020-12-04 | 殷实 | Recovery system of low-melting-point heavy metal in gasification and melting state and implementation method |
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| CN112275764A (en) * | 2020-08-31 | 2021-01-29 | 光大绿色环保管理（深圳）有限公司 | Hazardous waste incineration fly ash water washing utilization method and device |
| CN112225370A (en) * | 2020-09-01 | 2021-01-15 | 湖南博一环保科技有限公司 | Water washing and heavy metal removing process suitable for steel mill fly ash |
| CN113105138A (en) * | 2021-04-16 | 2021-07-13 | 北京中科国润环保科技有限公司 | Method and system for water washing dechlorination of waste incineration fly ash and evaporation mass-separation crystallization of water washing liquid |
| CN113105138B (en) * | 2021-04-16 | 2023-09-19 | 北京中科国润环保科技有限公司 | Treatment method and system for water washing and dechlorination of waste incineration fly ash and evaporation, quality separation and crystallization of water washing liquid |
| CN114230070A (en) * | 2021-11-21 | 2022-03-25 | 江苏卓博环保科技有限公司 | Incineration fly ash washing water recycling treatment device and method |
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