CN105478438B - A kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method - Google Patents

A kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method Download PDF

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CN105478438B
CN105478438B CN201510046384.5A CN201510046384A CN105478438B CN 105478438 B CN105478438 B CN 105478438B CN 201510046384 A CN201510046384 A CN 201510046384A CN 105478438 B CN105478438 B CN 105478438B
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flying dust
carnallite
water
bioxin
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CN105478438A (en
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刘宁生
王中华
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Huzhou Sano Environmental Technology Co Ltd
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Abstract

The present invention relates to a kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method, including tertiary effluent salt elution technique;Coagulating sedimentation goes removing heavy metals technique;Membrane distillation concentration technique;Go denier carnallite technique;Triple effect evaporation crystallization processes.Its three-level water elution salt technique can remove heavy metal and chlorion in flying dust, and flying dust becomes cement raw material after the flying dust of aqueous and bioxin flying dust and chloride ion-containing less than 1% is burned into cement kiln more than 1400 DEG C, and bioxin is cracked more than 800 DEG C;Coagulating sedimentation goes removing heavy metals technique to can remove many kinds of metal ions in flying dust, and sediment carries out entering cement kiln burning after pre- desiccation;Membrane distillation concentration technique can remove remaining chlorion and the distilled water reusable edible produced in solution;Denier carnallite technique is gone to remove denier carnallite and heat energy recoverable;High-salt concentrated liquid is evaporated isolated Nacl by triple effect evaporation crystallization processes is used for paper technology, Snow Agent and chlor-alkali industry.

Description

A kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method
Technical field:
The present invention relates to the handling process field of flying ash, more particularly to a kind of garbage flying ash cement kiln association With disposal and innoxious resource circulation utilization method.
Background technology:
With the development of the social economy, Process of Urbanization is aggravated, many big and medium-sized cities of China meet with the tired of " garbage-surrounded city " Disturb.Garbage disposal has 3 kinds of modes:Landfill, burn and compost, the garbage disposal of current China use based on landfill, compost with Measure supplemented by burning, this will take substantial amounts of land resource.With the continuous improvement that the rising of land price, urban environment are required, Garbage loading embeading becomes no longer economic and safety, and increasing city starts to consider incineration treatment of garbage.Burning disposal can make The volume of municipal refuse reduces 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 is produced " 90% all in flying dust.Not The flying dust of cured processing is dealt with improperly, wherein substantial amounts of heavy metal is Ji bioxin can cause serious contamination accident, harm is occupied People's health.Before, the whole nation only has several cities and is carrying out incineration of refuse flyash processing.One side flying dust processing cost is very high. On the other hand due to irregular marketing, not in place, the problem of there is harmful competition is supervised, " flying dust " is in " disorderly flying " state. Flying dust can not obtain safe disposal, will be environmentally hazardous very big hidden danger.
Because flying dust contains substantial amounts of chlorion, chlorion production normal to cement kiln produces very big influence, mainly Cement kiln skinning is shown, serious meeting produces quality accident, so, the key of cement kiln disposal flying dust is removed in flying dust A large amount of chlorions, washing process is the main method for removing chlorion in flying dust.
The content of the invention:
The purpose of the present invention be in view of the deficiencies of the prior art there is provided a kind of garbage flying ash cement kiln synergic processing and Innoxious resource circulation utilization method, this method realizes the innoxious and recycling treatment of flying dust, and flying ash can meet water Mud produces raw materials used standard, and membrane distillation concentration technique can remove in solution remaining chlorion and make the distilled water of generation Reusable edible;Denier carnallite technique is gone to remove denier carnallite and carried out the recycling of the energy;Triple effect evaporation crystallizes work Skill, which evaporates high-salt concentrated liquid, to be separated, and obtaining Nacl is used for paper technology, Snow Agent and chlor-alkali industry.
The technology solution of the present invention is as follows:
A kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method, it includes following technique mistake Journey:
(1) incineration of refuse flyash tertiary effluent salt elution technique;
(2) coagulating sedimentation goes removing heavy metals technique;
(3) membrane distillation concentration technique;
(4) denier carnallite technique is gone;
(5) triple effect evaporation crystallization processes.
Preferably, the incineration of refuse flyash tertiary effluent salt elution technique comprises the following steps:
A, washing:Incineration of refuse flyash is blown into mixer from storage, adds a certain amount of water, and the weight ratio of flying dust and water is 1:3, quality is added in whipping process and is stirred 20 minutes for 1% chaotropic agent of flying dust, mud is obtained after stirring fully;
B, dehydration:Mud is dehydrated into one-level horizontal screw centrifuge, and mud is isolated into chloro ion-containing solution and aqueous The flying dust of Ji bioxin, the moisture content of the flying dust of aqueous Ji bioxin is 40%-50%, and chloro ion-containing solution enters coagulating sedimentation Pond, the flying dust of aqueous Ji bioxin is washed into the second level;
C, secondary washing:The fly ash carry of aqueous Ji bioxin is to secondary blender, and with the weight of initial flying dust and water Than for 1:3 addition water are stirred addition quality in washing, whipping process and are stirred 20 for 1% chaotropic agent of initial flying dust Minute;Secondary mud is obtained after stirring fully;
D, second dehydration:Secondary mud is dehydrated into two grades of horizontal screw centrifuges, and it is molten that mud is isolated into chloride ion-containing The flying dust of liquid and secondary aqueous Ji bioxin, the moisture content of the flying dust of secondary aqueous Ji bioxin is 40%-50%, chloride ion-containing Solution enters coagulative precipitation tank, and the flying dust of secondary aqueous Ji bioxin is washed into the third level;
E, the fly ash carry of secondary aqueous Ji bioxin are to three-level mixer, and using the weight ratio of initial flying dust and water as 1: 2 addition water are stirred addition quality in washing, whipping process and are stirred 20 minutes for 1% chaotropic agent of initial flying dust; Three mud are obtained after stirring fully;
F, three mud are dehydrated into three-level horizontal screw centrifuge, and mud is isolated into chloro ion-containing solution and three times contain Water is Ji the flying dust of bioxin, the moisture content of the flying dust of three aqueous Ji bioxin is 40%-50%, and chloro ion-containing solution enters mixed Solidifying sedimentation basin, the flying dust of three aqueous and bioxin flying dusts and chloride ion-containing less than 1% enter cement kiln 1400 DEG C with Flying dust becomes cement raw material , bioxin and cracked more than 800 DEG C after upper burning, so as to reduce the production of more than 99% bioxin It is raw.
Preferably, three times in the incineration of refuse flyash tertiary effluent salt elution technique add chaotropic agent to be using same Chemicals dosing plant is covered, and automatic control flow is respectively adopted and is delivered, alarm can be sent when dose is not enough.
Preferably, the coagulating sedimentation goes removing heavy metals technique to comprise the following steps:
The chloro ion-containing solution obtained in a, step 2 enters coagulative precipitation tank, and heavy metal coupling is added toward coagulative precipitation tank is interior Mixture is stirred, and the quality of heavy metal couplant accounts for 1 ‰~the 5 ‰ of chloro ion-containing solution quality, makes a variety of dispersed metal ions Macromolecular is formed after polymerization so as to precipitate, after static 0.5~1 hour, precipitates 85~95% heavy metal ion;
B, the clear liquid then taken out on coagulative precipitation tank enter more medium filter by the heavy metal not precipitated completely, impurity Filter out, obtain the solution that saliferous rate is 8-15%;
C, 85~95% heavy metal ion of precipitation are carried into sludge collecting pit carry out pre- desiccation, enter after pre- desiccation Cement kiln is burned, so as to solve the pollution of incineration of refuse flyash heavy metal.
Preferably, the membrane distillation concentration technique comprises the following steps:
A, saliferous rate deliver into heating water tank for 8-15% solution, and plant area's waste heat pair is utilized using volumetric heat exchanger Solution is heated, and solution temperature rise is to after 70 °, and solution enters operating water tank;
B, membrane distillation processing:Then solution is circulated into membrane distillation system, and solution passes through to be undergone phase transition in membrane module, Vapor is by the membrane tube in membrane distiller, then by the high corrosion-resistant condensing tube condensation of thermal conductivity factor into distilled water, distilled water For membrane module backwash and incineration of refuse flyash washing moisturizing;
C, the reduction with solution reclaimed water, solution concentration are increasing, and solution concentration reaches that saliferous rate 20%-30% closely satisfies After state, solution is without circulation, and nearly saturated solution enters concentration water tank, and operating water tank reaches low liquid level, and self-priming pump startup will Liquid Residue is all discharged into concentration water tank in membrane module and condensation pipe;
Backwash starts after d, emptying, carries out backwash to membrane module by the distilled water produced, backwash pipeline is by membrane module Mouth enters, and the micro crystalline solid from attachment in lower mouth discharge, membrane distillation system is clean;In backwash process, heating water tank is to work Water tank progress fluid infusion, which reaches, stops fluid infusion after high level, after backwash terminates, and operating water tank carries out next circulation concentration.
Preferably, include 2~22 groups of membrane modules being connected in parallel in the membrane distillation system, each group of membrane module by 3~6 membrane distillers are in series.
Preferably, described go denier carnallite technique to comprise the following steps:
A, the dope of concentration water tank are heated up after entering flat ultra micro water filtration film one-level carnallite release unit, temperature It is upgraded to 80-110 DEG C to be handled, the carnallite for making solubility as temperature is raised using physical method and reducing is precipitated, dope point Not Jin Ru one-level impurity elimination brine tank a and one-level impurity elimination brine tank b, carnallite precipitation enter carnallite collecting pit, carnallite go landfill or Burn;
B, using heat pump by one-level impurity elimination brine tank b heat recovery to one-level impurity elimination brine tank a, one-level impurity elimination brine tank B solution is cooled after entering special flat board acupuncture membrane filtration two grades of carnallite release units of bag, and temperature is reduced at -2~2 DEG C Reason, the carnallite for making solubility as temperature is raised using physical method and reducing is precipitated, and dope, which enters, removes carnallite condensed water case, miscellaneous Salt precipitation enters carnallite collecting pit, and carnallite goes to fill or burned;
C, one-level impurity elimination brine tank a and except the finished product dope in carnallite condensed water case is exchanged heat by heat exchanger, make to remove Carnallite dope obtains heat heating and is evaporated crystallization into triple effect evaporation crystal system, it is to avoid the dirt in evaporation and crystal process Stifled phenomenon, the heat energy of recovery is so heated the finished product dope after cooling, improve the temperature of evaporative crystallization mother liquor, reduces energy Consumption.
Preferably, the triple effect evaporation crystallization processes comprise the following steps:
The evaporative crystallization mother liquor obtained in a, step 5 initially enters the first effect forced circulation crystallizing evaporator, while 90 DEG C Heating steam be introduced into the first effect forced circulation crystallizing evaporator, heat evaporative crystallization mother liquor therein, make its evaporate and Separated in vortex salt separator, the salt of solid-state, which is separated, enters the separation of solid and liquid that storage salt pond is achieved in salinity and dope;
In b, the evaporation and heat-exchange room of the first effect forced circulation crystallizing evaporator, it was heated under the reduction of negative pressure liquid boiling point Thermogenetic steam is introduced into the second effect forced circulation crystallizing evaporator as heating steam, makes the crystallization steaming of the second effect forced circulation Send out the dope in device to evaporate with the lower temperature than the first effect forced circulation crystallizing evaporator, this process repeats to the always Triple effect forced circulation crystallizing evaporator, the salt of solid-state is segregated into storage salt pond by vortex salt separator and is achieved in salinity and dope Separation of solid and liquid;
Condensed water in c, the first effect forced circulation crystallizing evaporator is returned at thermal source, the second effect forced circulation crystallization and evaporation The condensed water of device and triple effect forced circulation crystallizing evaporator is exported after collecting as distilled water;Evaporative crystallization mother liquor passes through simultaneously By the concentration successively of the first effect forced circulation crystallizing evaporator to triple effect forced circulation crystallizing evaporator, force to follow in triple effect Supersaturation is reached in ring crystallizing evaporator and crystallizes and separates out.
The beneficial effects of the present invention are:
The chloro ion-containing solution that the tertiary effluent salt elution technique of the present invention is produced enters coagulative precipitation tank, and three times aqueous and two Flying dust becomes cement raw after flying dust of the flying dust and chloride ion-containing of Evil English less than 1% is burned into cement kiln more than 1400 DEG C Material , bioxin is cracked more than 800 DEG C, so as to reduce the generation of more than 99% bioxin.Given birth to using cement kiln synergic processing Biomass fuel burn produce flying dust, be quality coal in cement kiln systems high temperature section put into flying dust, make full use of cement kiln hot environment and The formation of clinker mineral, on the one hand fully decomposes the toxic organic compound such as bioxin in flying dust, while toxic heavy metal is consolidated Change into clinker, cement kiln thermal capacity is big, stable working state, the refractory brick, raw material, kliner coating and clinker in cement kiln are equal For alkalescence, SO is can absorb2, so as to suppress its discharge.Other manufacture of cement amount is big, can largely dispose flying dust.
The sediment that the coagulating sedimentation of the present invention goes removing heavy metals technique to obtain, which enters sludge collecting pit, to be carried out after pre- desiccation Burned into cement kiln;Its technique solves the pollution of incineration of refuse flyash heavy metal.Heavy metal couplant is added in this technique Precipitation is filtered out again afterwards, therefore does not cause the secondary pollution of solution, and subsequent technique is not impacted, harmlessness disposing is obtained.
It is remaining chlorion in 8-15% solution that the membrane distillation concentration technique of the present invention, which can remove saliferous rate, and makes production Raw distilled water reusable edible, distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing, substantial amounts of distilled water Into water wash system, the consumed water of washing is greatly reduced.
The present invention's goes denier carnallite technique to have removed denier carnallite and carry out the recycling of the energy, one-level impurity elimination Heat pump is set up between brine tank a and one-level impurity elimination brine tank b, is because the cooling of secondary separation device is handled, if not by heat Great loss will be caused to heat by carrying out recovery, so as to carry out the recycling of the energy, can will reclaim energy heats simultaneously Dope after cooling, improves the temperature of evaporative crystallization mother liquor, reduces energy consumption.
The triple effect evaporation crystallization processes of the present invention are made up of three evaporators being serially connected, and a whole set of vapo(u)rization system is using company Continuous charging, the mode of production of continuous discharge, high-salt concentrated liquid is evaporated and separated, and obtaining Nacl is used for paper technology, Snow Agent And chlor-alkali industry.
Brief description of the drawings:
The present invention is described further below in conjunction with the accompanying drawings:
Fig. 1 is process chart of the invention;
Fig. 2 is the flow chart of the incineration of refuse flyash tertiary effluent salt elution technique of the present invention;
Fig. 3 removes the flow chart of removing heavy metals technique for the coagulating sedimentation of the present invention;
Fig. 4 is the flow chart of the membrane distillation concentration technique of the present invention;
Fig. 5 is the flow chart for going denier carnallite technique of the invention;
Fig. 6 is the flow chart of the triple effect evaporation crystallization processes of the present invention;
Fig. 7 is the structural representation of the membrane module of the present invention.
Embodiment:
Embodiment, is shown in accompanying drawing 1~7, a kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method, It includes following technical process:
(1) incineration of refuse flyash tertiary effluent salt elution technique;
(2) coagulating sedimentation goes removing heavy metals technique;
(3) membrane distillation concentration technique;
(4) denier carnallite technique is gone;
(5) triple effect evaporation crystallization processes.
(1) the incineration of refuse flyash tertiary effluent salt elution technique comprises the following steps:
A, washing:Incineration of refuse flyash is blown into mixer 2 from storage 1, and flying ash is one ton, adds a certain amount of water 3, and The weight ratio of flying dust and water is 1:3, i.e. it is the 1% of flying dust that the water of 3 tons of addition, which enters addition quality in mixer, whipping process, Chaotropic agent is stirred 20 minutes, and mud is obtained after stirring fully;
B, dehydration:Mud is dehydrated into one-level horizontal screw centrifuge 4, and mud is isolated into chloro ion-containing solution and aqueous The flying dust of Ji bioxin, the moisture content of the flying dust of aqueous Ji bioxin is 40%-50%, and chloro ion-containing solution enters coagulating sedimentation Pond 5, moisture content is washed for the flying dust of 40%-50% aqueous Ji bioxin into the second level;
C, secondary washing:The fly ash carry of aqueous Ji bioxin is to secondary blender 6, and with the weight of initial flying dust and water Than for 1:The water that 3 addition water are stirred washing, i.e., 3 ton enters in mixer, whipping process that to add quality be initial flying dust 1% chaotropic agent is stirred 20 minutes;Secondary mud is obtained after stirring fully;
D, second dehydration:Secondary mud is dehydrated into two grades of horizontal screw centrifuges 7, and it is molten that mud is isolated into chloride ion-containing The flying dust of liquid and secondary aqueous Ji bioxin, the moisture content of the flying dust of secondary aqueous Ji bioxin is 40%-50%, chloride ion-containing Solution enters coagulative precipitation tank, and the flying dust of secondary aqueous Ji bioxin is washed into the third level;
E, the fly ash carry of secondary aqueous Ji bioxin to three-level mixer 8, and using the weight ratio of initial flying dust and water as 1:The water that 2 addition water are stirred washing, i.e., 2 ton enters in mixer, whipping process add that quality is initial flying dust 1% Chaotropic agent is stirred 20 minutes;Three mud are obtained after stirring fully;
F, three mud are dehydrated into three-level horizontal screw centrifuge 9, and mud is isolated into chloro ion-containing solution and three times The flying dust of aqueous Ji bioxin, the moisture content of the flying dust of three aqueous Ji bioxin is 40%-50%, and chloro ion-containing solution enters Coagulative precipitation tank, the flying dust of flying dust and chloride ion-containing less than 1% of three aqueous Ji bioxin enters cement kiln 10 1400 Flying dust becomes cement raw material , bioxin and cracked more than 800 DEG C after being burned more than DEG C, so as to reduce more than 99% bioxin Produce, that is, it is 1 to complete flying dust with water:8 three-level water wash system.
Three times in the incineration of refuse flyash tertiary effluent salt elution technique plus chaotropic agent are to use same set of chaotropic agent Chemicals dosing plant 11, and automatic control flow is respectively adopted is delivered, it can send alarm when dose is not enough.
(2) coagulating sedimentation goes removing heavy metals technique to comprise the following steps:
7 tons of chloro ion-containing solutions enter coagulative precipitation tank 5 after a, the washing of step 1 three-level, interior by going toward coagulative precipitation tank Removing heavy metals device 12 adds the stirring of heavy metal couplant, and the quality of heavy metal couplant accounts for chloro ion-containing solution quality 1 ‰~5 ‰, make to be formed macromolecular after a variety of dispersed metal ionic polymerizations so as to precipitating, after static 0.5~1 hour, make 85~ 95% heavy metal ion precipitation;
B, then take out clear liquid on coagulative precipitation tank and enter more medium filter 13 by the heavy metal not precipitated completely, miscellaneous Matter is filtered out, and obtains the solution 14 that saliferous rate is 8-15%;
C, 85~95% heavy metal ion of precipitation are carried into sludge collecting pit 15 carry out pre- desiccation, pre- desiccation is laggard Enter cement kiln 16 to burn, so as to solve the pollution of incineration of refuse flyash heavy metal.Coagulating sedimentation removes a huge sum of money in removing heavy metals technique Category couplant is precipitated and filtered out again after adding, therefore does not cause the secondary pollution of solution, to follow-up membrane distillation concentration technique, evaporation knot Brilliant technique etc. is not impacted, and has obtained harmlessness disposing.
(3) the membrane distillation concentration technique comprises the following steps:
A, by the saliferous rate obtained in step (2) for 8-15% solution deliver into heating water tank 17, use positive displacement Heat exchanger 18 is heated using plant area's waste heat to solution, and solution temperature rise is to after 70 °, and solution enters operating water tank 19;
B, membrane distillation processing:Then saliferous rate is circulated for 8-15% solution into membrane distillation system 20, the film Include 2~22 groups of membrane modules 21 being connected in parallel in Distallation systm, each group of membrane module is connected by 3~6 membrane distillers 22 Into (producing 40 kilograms to 5 tons distilled water per hour), its membrane module uses one kind of Huzhou Sen Nuo membrane technologies Engineering Co., Ltd Normal pressure anti-soil blocks up energy-saving membrane distiller, Patent No. 201420465882.4.Solution in membrane module by undergoing phase transition, and water steams Gas is by the membrane tube in membrane distiller, then by the high corrosion-resistant condensing tube condensation of thermal conductivity factor into distilled water, and output is solution Volume 60-70% is 4-5 tons of distilled water, and distilled water is stored in backwash water tank 23, and distilled water is used for membrane module backwash and rubbish Rubbish flying ash washes moisturizing, and substantial amounts of distilled water enters water wash system, greatly reduces the consumed water of washing, is overall Washing ratio is reduced to 1:3~1:Between 5;
C, the reduction with solution reclaimed water, solution concentration are increasing, and solution concentration reaches that saliferous rate 20%-30% closely satisfies After state, solution is without circulation, and nearly saturated solution enters concentration water tank 24, and operating water tank reaches low liquid level, self-priming pump startup Liquid Residue in membrane module and condensation pipe is all discharged into concentration water tank;
Backwash starts after d, emptying, carries out backwash to membrane module by the distilled water produced, backwash pipeline is by membrane module Mouth enters, and the micro crystalline solid from attachment in lower mouth discharge, membrane distillation system is clean;In backwash process, heating water tank is to work Water tank progress fluid infusion, which reaches, stops fluid infusion after high level, after backwash terminates, and operating water tank carries out next circulation concentration, so both The stability of membrane module can be ensure that, while between the quiet stopping time for having agreed with coagulative precipitation tank again.During one section of membrane distillation system operation Between after (3-6 month) in order to maintain the lasting hydrophobicity of part film, can also supporting independent film regenerating device carry out periodically quantitative film Reproduction operation ensures membrane stability.
(4) it is described to go denier carnallite technique to comprise the following steps:
A, the dope of concentration water tank enter the flat ultra micro water filtration film (patent No.:2013103087676) one-level carnallite Heated up after release unit 25, temperature is upgraded to 80-110 DEG C and handled, make solubility with temperature liter using physical method Carnallite that is high and reducing is precipitated, and dope respectively enters one-level impurity elimination brine tank a26 and one-level impurity elimination brine tank b27, carnallite precipitation Into carnallite collecting pit 28, carnallite goes to fill or burned;
B, using heat pump 29 by one-level impurity elimination brine tank b heat recovery to one-level impurity elimination brine tank a, one-level impurity elimination salt solution Case b solution is cooled after entering special flat board acupuncture membrane filtration two grades of carnallite release units 30 of bag, and temperature is reduced to -2~2 DEG C and entered Row processing, the carnallite for making solubility as temperature is raised using physical method and reducing is precipitated, and dope, which enters, removes carnallite condensed water Case 31, carnallite precipitation enters carnallite collecting pit, and carnallite goes to fill or burned;
C, one-level impurity elimination brine tank a and except the finished product dope in carnallite condensed water case is exchanged heat by heat exchanger, make to remove Carnallite dope obtains heat heating and is evaporated crystallization into triple effect evaporation crystal system, it is to avoid the dirt in evaporation and crystal process Stifled phenomenon, the heat energy of recovery is so heated the finished product dope after cooling, make the temperature of finished product dope (i.e. evaporative crystallization mother liquor) Degree is improved, and reduces energy consumption.
(5) the triple effect evaporation crystallization processes comprise the following steps:
The evaporative crystallization mother liquor obtained in a, step 4 initially enters the first effect forced circulation crystallizing evaporator 32, while 90 DEG C heating steam be introduced into the first effect forced circulation crystallizing evaporator, heat evaporative crystallization mother liquor therein, make its evaporation simultaneously Separated in vortex salt separator 33, the salt of solid-state, which is separated, enters the solid-liquid point that storage salt pond 34 is achieved in salinity and dope From;
In b, the evaporation and heat-exchange room of the first effect forced circulation crystallizing evaporator, it was heated under the reduction of negative pressure liquid boiling point Thermogenetic steam is introduced into the second effect forced circulation crystallizing evaporator 35 as heating steam, crystallizes the second effect forced circulation Dope in evaporator is evaporated with the lower temperature than the first effect forced circulation crystallizing evaporator, and this process is repeated to always Triple effect forced circulation crystallizing evaporator 36, the salt of solid-state by vortex salt separator be segregated into storage salt pond be achieved in salinity with The separation of solid and liquid of dope;
Condensed water in c, the first effect forced circulation crystallizing evaporator is returned at thermal source, the second effect forced circulation crystallization and evaporation The condensed water of device and triple effect forced circulation crystallizing evaporator is exported after collecting as distilled water;Evaporative crystallization mother liquor passes through simultaneously By the concentration successively of the first effect forced circulation crystallizing evaporator to triple effect forced circulation crystallizing evaporator, force to follow in triple effect Supersaturation is reached in ring crystallizing evaporator and crystallizes and separates out.
Through purity salt more than 70% made from step (5), it is used for paper technology, Snow Agent and chlor-alkali row as Nacl Industry.
Above-described embodiment is the specific descriptions carried out to the present invention, simply the present invention is further described, it is impossible to manage Solve as limiting the scope of the present invention, it is nonessential that those skilled in the art makes some according to the content of foregoing invention Modifications and adaptations are each fallen within protection scope of the present invention.

Claims (4)

1. a kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method, it is characterised in that:It is included such as Lower technical process:
(1) incineration of refuse flyash tertiary effluent salt elution technique, comprises the following steps,
A, washing:Incineration of refuse flyash is blown into mixer from storage, adds a certain amount of water, and the weight ratio of flying dust and water is 1:3, Quality is added in whipping process to be stirred 20 minutes for 1% chaotropic agent of flying dust, and mud is obtained after stirring fully;
B, dehydration:Mud is dehydrated into one-level horizontal screw centrifuge, and mud is isolated into chloro ion-containing solution and aqueous and two The flying dust of Evil English, the moisture content of the flying dust of aqueous Ji bioxin is 40%-50%, and chloro ion-containing solution enters coagulative precipitation tank, The flying dust of aqueous Ji bioxin is washed into the second level;
C, secondary washing:The fly ash carry of aqueous Ji bioxin to secondary blender, and using the weight ratio of initial flying dust and water as 1:3 addition water are stirred addition quality in washing, whipping process and are stirred 20 points for 1% chaotropic agent of initial flying dust Clock;Secondary mud is obtained after stirring fully;
D, second dehydration:Secondary mud is dehydrated into two grades of horizontal screw centrifuges, by mud isolate chloro ion-containing solution and The flying dust of secondary aqueous Ji bioxin, the moisture content of the flying dust of secondary aqueous Ji bioxin is 40%-50%, chloro ion-containing solution Into coagulative precipitation tank, the flying dust of secondary aqueous Ji bioxin is washed into the third level;
E, the fly ash carry of secondary aqueous Ji bioxin are to three-level mixer, and using the weight ratio of initial flying dust and water as 1:2 add Enter water and be stirred in washing, whipping process to add quality and be stirred 20 minutes for 1% chaotropic agent of initial flying dust;Stirring Three mud are obtained after fully;
F, three mud are dehydrated into three-level horizontal screw centrifuge, by mud isolate chloro ion-containing solution and three times it is aqueous and The flying dust of bioxin, the moisture content of the flying dust of three aqueous Ji bioxin is 40%-50%, and chloro ion-containing solution is heavy into coagulation Shallow lake pond, the flying dust of flying dust and chloride ion-containing less than 1% of three aqueous Ji bioxin burns into cement kiln more than 1400 DEG C Flying dust becomes cement raw material , bioxin and cracked more than 800 DEG C after burning, so as to reduce the generation of more than 99% bioxin;
(2) coagulating sedimentation goes removing heavy metals technique:Chloro ion-containing solution enters coagulative precipitation tank, and weight is added toward coagulative precipitation tank is interior Precipitate 85~95% heavy metal ion after metal Coupling agent stirring reaction;Take out the clear liquid on coagulative precipitation tank and enter many Jie Mass filter falls the heavy metal not precipitated completely, contaminant filter, obtains the solution that saliferous rate is 8-15%;
(3) membrane distillation concentration technique, comprises the following steps,
A, saliferous rate deliver into heating water tank for 8-15% solution, using volumetric heat exchanger using plant area's waste heat to solution Heating, solution temperature rise is to after 70 °, and solution enters operating water tank;
B, membrane distillation processing:Then solution is circulated into membrane distillation system, and solution in membrane module by undergoing phase transition, and water steams Gas is by the membrane tube in membrane distiller, then by the high corrosion-resistant condensing tube condensation of thermal conductivity factor into distilled water, and distilled water is used for Membrane module backwash and incineration of refuse flyash washing moisturizing;
C, the reduction with solution reclaimed water, solution concentration are increasing, and solution concentration reaches the nearly saturation shapes of saliferous rate 20%-30% After state, solution is without circulation, and nearly saturated solution enters concentration water tank, and operating water tank reaches low liquid level, and self-priming pump startup is by film group Liquid Residue is all discharged into concentration water tank in part and condensation pipe;
Backwash starts after d, emptying, and backwash is carried out to membrane module by the distilled water that produces, backwash pipeline by membrane module it is suitable for reading enter Enter, from the discharge of lower mouth, the micro crystalline solid of attachment is cleaned in membrane distillation system;In backwash process, heating water tank is to operating water tank Progress fluid infusion, which reaches, stops fluid infusion after high level, after backwash terminates, and operating water tank carries out next circulation concentration;
(4) denier carnallite technique is gone:Comprise the following steps,
A, the dope of concentration water tank are heated up after entering flat ultra micro water filtration film one-level carnallite release unit, and temperature is upgraded to 80-110 DEG C is handled, and the carnallite for making solubility as temperature is raised using physical method and reducing is precipitated, and dope enters respectively Enter one-level impurity elimination brine tank a and one-level impurity elimination brine tank b, carnallite precipitation enters carnallite collecting pit, and carnallite goes to fill or burned;
B, using heat pump by one-level impurity elimination brine tank b heat recovery to one-level impurity elimination brine tank a, one-level impurity elimination brine tank b's Solution is cooled after entering special flat board acupuncture membrane filtration two grades of carnallite release units of bag, and temperature is reduced to -2~2 DEG C and handled, The carnallite for making solubility as temperature is raised using physical method and reducing is precipitated, and dope, which enters, removes carnallite condensed water case, carnallite Precipitation enters carnallite collecting pit, and carnallite goes to fill or burned;
C, one-level impurity elimination brine tank a and except the finished product dope in carnallite condensed water case is exchanged heat by heat exchanger, make to remove carnallite Dope obtains heat heating and is evaporated crystallization into triple effect evaporation crystal system, it is to avoid dirt in evaporation and crystal process is stifled to be showed As the heat energy of recovery so to be heated to the finished product dope after cooling, the temperature of evaporative crystallization mother liquor is improved, energy consumption is reduced;
(5) triple effect evaporation crystallization processes:Comprise the following steps:
The evaporative crystallization mother liquor obtained in a, step 5 initially enters the first effect forced circulation crystallizing evaporator, at the same 90 DEG C plus Heat steam is introduced into the first effect forced circulation crystallizing evaporator, heats evaporative crystallization mother liquor therein, it is evaporated and in vortex Separated in salt separator, the salt of solid-state, which is separated, enters the separation of solid and liquid that storage salt pond is achieved in salinity and dope;
In b, the evaporation and heat-exchange room of the first effect forced circulation crystallizing evaporator, overheat production is heated under the reduction of negative pressure liquid boiling point Raw steam is introduced into the second effect forced circulation crystallizing evaporator as heating steam, makes the second effect forced circulation crystallizing evaporator Interior dope is evaporated with the lower temperature than the first effect forced circulation crystallizing evaporator, and this process repeats to triple effect always Forced circulation crystallizing evaporator, the salt of solid-state is segregated into storage salt pond by vortex salt separator and is achieved in consolidating for salinity and dope Liquid is separated;
C, first effect forced circulation crystallizing evaporator in condensed water return thermal source at, second effect forced circulation crystallizing evaporator and The condensed water of triple effect forced circulation crystallizing evaporator is exported after collecting as distilled water;Evaporative crystallization mother liquor passes through by the simultaneously One imitates forced circulation crystallizing evaporator to the concentration successively of triple effect forced circulation crystallizing evaporator, in triple effect forced circulation knot Supersaturation is reached in brilliant evaporator and crystallizes and separates out.
2. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and innoxious resource circulation utilization method, It is characterized in that:Three times in the incineration of refuse flyash tertiary effluent salt elution technique plus chaotropic agent are to use same set of dosing Device, and automatic control flow is respectively adopted is delivered, it can send alarm when dose is not enough.
3. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and innoxious resource circulation utilization method, It is characterized in that:The coagulating sedimentation goes removing heavy metals technique to comprise the following steps:
The chloro ion-containing solution obtained in a, step 2 enters coagulative precipitation tank, and heavy metal couplant is added toward coagulative precipitation tank is interior Stirring, and the quality of heavy metal couplant accounts for 1 ‰~the 5 ‰ of chloro ion-containing solution quality, makes a variety of dispersed metal ionic polymerizations Macromolecular is formed afterwards so as to precipitate, and after static 0.5~1 hour, precipitates 85~95% heavy metal ion;
B, the clear liquid then taken out on coagulative precipitation tank enter more medium filter by the heavy metal not precipitated completely, contaminant filter Fall, obtain the solution that saliferous rate is 8-15%;
C, 85~95% heavy metal ion of precipitation are carried into sludge collecting pit carry out pre- desiccation, cement is entered after pre- desiccation Kiln is burned, so as to solve the pollution of incineration of refuse flyash heavy metal.
4. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and innoxious resource circulation utilization method, It is characterized in that:Include 2~22 groups of membrane modules being connected in parallel in the membrane distillation system, each group of membrane module is by 3~6 Membrane distiller is in series.
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JP6222316B1 (en) * 2016-09-06 2017-11-01 栗田工業株式会社 Device for determining the amount of heavy metal fixing agent added
CN107597795B (en) * 2017-09-07 2020-12-01 中洁蓝环保科技有限公司 System and method for recycling and treating household garbage incineration fly ash
CN108607870B (en) * 2018-04-26 2019-11-12 杭州秀澈环保科技有限公司 A kind of garbage flying ash processing system and treatment process
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
CN109575880A (en) * 2018-11-01 2019-04-05 杭州秀澈环保科技有限公司 A method of I type deicing salt is prepared using garbage flying ash
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JP4306394B2 (en) * 2003-10-01 2009-07-29 宇部興産株式会社 Cement kiln extraction dust processing method
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