CN215089715U - Fly ash water washing system and fly ash treatment system containing same - Google Patents
Fly ash water washing system and fly ash treatment system containing same Download PDFInfo
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- CN215089715U CN215089715U CN202121122361.5U CN202121122361U CN215089715U CN 215089715 U CN215089715 U CN 215089715U CN 202121122361 U CN202121122361 U CN 202121122361U CN 215089715 U CN215089715 U CN 215089715U
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- 238000005406 washing Methods 0.000 title claims abstract description 116
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 116
- 239000010881 fly ash Substances 0.000 title claims abstract description 80
- 150000003839 salts Chemical class 0.000 claims abstract description 51
- 239000000706 filtrate Substances 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 239000012452 mother liquor Substances 0.000 claims abstract description 14
- 239000010802 sludge Substances 0.000 claims description 63
- 238000004062 sedimentation Methods 0.000 claims description 21
- 238000004519 manufacturing process Methods 0.000 claims description 18
- 230000008018 melting Effects 0.000 claims description 17
- 238000002844 melting Methods 0.000 claims description 17
- 230000001112 coagulating effect Effects 0.000 claims description 15
- 239000000243 solution Substances 0.000 claims description 13
- 238000001035 drying Methods 0.000 claims description 12
- 238000002425 crystallisation Methods 0.000 claims description 11
- 230000008025 crystallization Effects 0.000 claims description 11
- 238000001728 nano-filtration Methods 0.000 claims description 9
- 239000011347 resin Substances 0.000 claims description 9
- 229920005989 resin Polymers 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 8
- 239000008237 rinsing water Substances 0.000 claims description 7
- 238000000108 ultra-filtration Methods 0.000 claims description 7
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 6
- 239000011552 falling film Substances 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 239000012267 brine Substances 0.000 claims description 5
- 238000005345 coagulation Methods 0.000 claims description 5
- 230000015271 coagulation Effects 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 5
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 5
- 238000001354 calcination Methods 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims description 4
- 238000009287 sand filtration Methods 0.000 claims description 4
- 239000012141 concentrate Substances 0.000 claims 4
- 230000004927 fusion Effects 0.000 claims 3
- 239000012492 regenerant Substances 0.000 claims 1
- 239000004568 cement Substances 0.000 abstract description 18
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 9
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract description 8
- 230000015572 biosynthetic process Effects 0.000 abstract description 4
- 238000012545 processing Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 239000013078 crystal Substances 0.000 abstract description 3
- 238000003786 synthesis reaction Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000003837 high-temperature calcination Methods 0.000 abstract description 2
- 239000013589 supplement Substances 0.000 abstract description 2
- 239000002956 ash Substances 0.000 abstract 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 238000004056 waste incineration Methods 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 238000006298 dechlorination reaction Methods 0.000 description 4
- 238000010828 elution Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000011010 flushing procedure Methods 0.000 description 3
- 239000002920 hazardous waste Substances 0.000 description 3
- 239000001103 potassium chloride Substances 0.000 description 3
- 235000011164 potassium chloride Nutrition 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000011737 fluorine Substances 0.000 description 2
- 229910052731 fluorine Inorganic materials 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 231100000357 carcinogen Toxicity 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000000382 dechlorinating effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The application provides a fly ash washing system, including multistage countercurrent washing device, filtrating processing apparatus to and biochemical system. By adopting the fly ash washing system, the fly ash can be dechlorinated more thoroughly before high-temperature calcination; the waste water from ash washing produces crystal salt which can be recycled through the filtrate treatment device, and the residual mother liquor and the condensate are treated by the biochemical system and enter the multi-stage countercurrent washing device again to be used as the eluting water to supplement water source instead of being used as the waste liquid to discharge the fly ash washing system, thereby really realizing zero discharge of the waste water from ash washing, low energy consumption and no pollution. The application also provides a fly ash treatment system comprising the fly ash washing system, heavy metals in the fly ash are completely solidified in cement clinker lattices after being melted at high temperature, and thorough treatment is free from aftereffects; the dioxin is decomposed thoroughly and does not have secondary synthesis conditions any more.
Description
The application claims priority, wherein the application number of the priority is 202120729264.6, the application date is 2021, 04/09, and the accepting country is China.
Technical Field
The application relates to the field of hazardous waste treatment, in particular to a fly ash water washing system and a fly ash treatment system comprising the same.
Background
The fly ash is a residual substance generated after the waste incineration, and is a powder substance which is collected in a flue gas pipeline, a separator, a dust remover and the like in the waste incineration process and has light volume weight and fine particle size. The fly ash accounts for 0.5 to 3 percent of the total amount of the incineration waste. The fly ash contains a large amount of heavy metals such as Cd, Cr, Cu, Ni, Pb, Zn and the like, and also enriches high-concentration organic carcinogens such as dioxin with strong toxicity, belongs to hazardous waste specified in the national hazardous waste record, and causes damage which is difficult to repair to the ecological environment if the fly ash is improperly disposed.
The traditional fly ash treatment process is landfill after pretreatment by adopting a curing stabilizer, however, due to the shortage of national land resources and the harm of environmental pollution caused by heavy metal dissolution caused by improper treatment during landfill, the new method for treating the fly ash generated by waste incineration and realizing resource utilization is imperative.
SUMMERY OF THE UTILITY MODEL
The waste incineration fly ash in China has high content of soluble chloride salt, so that the melting and sintering process is difficult to control, hydrogen chloride gas is easy to escape, and secondary pollution is caused. The disposal method of direct injection into the cement kiln in the prior art is only suitable for fly ash with the content of chloride ions being below 3 percent, and poor control of the speed of the injection into the kiln can cause the crust in the kiln and corrode equipment and pipelines; meanwhile, the high-chlorine materials discharged by the bypass vent are difficult to dispose.
In order to solve the above problems, a first object of the present application is to provide a fly ash washing system for more thoroughly dechlorinating fly ash before high-temperature calcination. The fly ash washing system comprises a multi-stage countercurrent washing device, a filtrate treatment device and a biochemical system.
The multistage countercurrent water washing device comprises n water washing units, wherein n is more than or equal to 3, and each water washing unit comprises a water washing tank and a sludge dewatering machine. Each rinsing bath comprises a muddy water outlet, particularly, the rinsing bath of the 1-stage rinsing unit is also provided with a fly ash inlet, while the 2-n-stage rinsing units are not provided with fly ash inlets; the wash tank of the n-stage water wash unit also has an initial rinse water inlet, whereas the 1-n-1 stage water wash units do not. The fly ash is washed by the water washing tank to generate muddy water, and the muddy water is separated by the sludge dewatering machine to obtain sludge and filtrate, so that the sludge dewatering machine comprises a muddy water inlet, a sludge outlet and a filtrate outlet. That is, the fly ash enters the system from the 1-level water washing unit, and continuously enters the next-level water washing unit in the form of sludge after being eluted; clean rinsing water enters the system from the 5-stage water washing unit, and after the sludge is eluted, the rinsing water continuously flows into the upper-stage water washing unit in the form of filtrate.
In the multistage countercurrent water washing device, the sludge outlet of the 1-n-1 stage water washing unit is communicated with the water washing tank of the next stage water washing unit so as to send the sludge into the water washing tank of the next stage water washing unit. The sludge outlet of the n-stage water washing unit (i.e. the last stage water washing unit) is connected with a sludge conveying device to convey the sludge to a fly ash treatment unit of the next stage, such as a drying unit or a high-temperature melting unit. Filtrate outlets of the 2-n stages of water washing units are communicated with a water washing tank of the previous stage of water washing unit so as to guide the filtrate into the water washing tank of the previous stage of water washing unit.
The filtrate treatment device is used for obtaining crystallized salt and residual mother liquor, and comprises a filtrate pretreatment device and a salt making system.
The inlet of the filtrate pretreatment device is connected with the filtrate outlet of the sludge dewatering machine of the 1-stage water washing unit, namely, the filtrate obtained by separating the mud water of the 1-stage water washing unit by the sludge dewatering machine enters the filtrate pretreatment device for pretreatment. The filtrate pretreatment device comprises a concentrated solution outlet and a brine preparation outlet, wherein the concentrated solution outlet is communicated with a rinsing bath of the 1-level rinsing unit, so that the concentrated solution and the fly ash of the filtrate pretreatment device are mixed for rinsing; and liquid discharged from the salt making water outlet enters a salt making system for salt formation.
And the inlet of the salt making system is communicated with a salt making water outlet of the filtrate pretreatment device, and the salt making system comprises a liquid outlet which is used for conveying condensate liquid and residual mother liquid generated in the salt making process.
The inlet of the biochemical system is communicated with the liquid outlet of the salt making system, and the water outlet of the biochemical system is communicated with the rinsing bath of the nth-level rinsing unit. That is, the salt production system produces condensate and residual mother liquor, which condensate can be used to dilute the residual mother liquor. The diluted residual enters a biochemical system, and the effluent treated by the biochemical system returns to a multi-stage countercurrent washing system to be combined with the initial rinsing water, and the effluent and the initial rinsing water are jointly used as washing water to recycle the water source; and the condensate liquid which is discharged after the rest mother liquid is diluted can be directly introduced into a rinsing bath of the 5-level rinsing unit without passing through a biochemical system.
According to the thirteen-five program, 1000 ten thousand tons of fly ash are produced in China every year, and after the technical scheme is subjected to washing dechlorination treatment, the fly ash can be completely converted into qualified cement clinker by only one tenth of the cement kiln capable of producing the cement clinker in China, so that raw materials are saved, and the recycling of the fly ash is realized. The multi-stage countercurrent elution technology is adopted, so that the dealkalization and dechlorination effects are good, and no dust is raised. Because the elution environment is alkaline, the transfer rate of heavy metal and dioxin is low in the environment, and secondary collection and recovery of heavy metal can be realized. And, wash grey waste water and produce crystalline salt through the filtrating processing apparatus of this application, the surplus mother liquor passes through biochemical system again and handles and get into multistage countercurrent washing device again, and as the supplementary water source of eluting water, rather than as waste liquid discharge fly ash washing system, really accomplished and washed grey waste water zero release, the energy consumption is low, pollution-free. The condensate can be used for diluting the residual mother liquor, and can also be directly fed into a multi-stage countercurrent water washing device to be combined for washing and dewatering, so that the water source is further saved.
Further, in the multistage countercurrent water washing apparatus, n is 5. That is to say, multistage countercurrent washing device has 5 washing units, adopts this technical scheme can make the percentage of dechlorination > 95%, and the water consumption is suitable. If more than 5 water washing units are used, the dechlorination effect is not remarkably improved, and the amount of eluted water is increased, resulting in an increase in the cost of water treatment.
Further, the salt preparation system comprises a nano-filtration salt separation device, an ozone oxidation device, a falling film concentration device and an evaporation crystallization system which are sequentially connected.
Further, the nanofiltration salt separation device can separate liquid received from the filtrate pretreatment device into a water production side and a concentrated water side, the concentrated water side is communicated with the washing tank of the 1-stage washing unit, and the water production side is communicated with the ozone oxidation device. Thus, the concentrated water side is continuously combined into muddy water, and the water producing side enters the subsequent salt making step. The total recovery rate of the salt in the technical scheme is more than 90 percent; the quality of the finally obtained sodium chloride product meets the requirements of 1 class I products in the industrial salt (GB5462-2015), and the quality of the potassium chloride product meets the requirements of 1 class I products in the potassium chloride (GB 6549-2011) standard, so that the aims of thorough harmlessness and recycling are fulfilled. The evaporation mother liquor can be used as the eluting water to supplement a water source together with the condensate after being treated by a biochemical system, and is not discharged outside.
Furthermore, the salt manufacturing system can also comprise an electric boiler which is mainly used for providing heat energy, the electric boiler is used for generating steam, one part of the steam is used as a heat source of the falling film concentration device and the evaporation crystallization system, and the other part of the steam is used as a heat source of a dryer for drying crystallized salt.
Further, the filtrate pretreatment device comprises a coagulation sedimentation tank, a sand filtration tank, an ultrafiltration device and a resin adsorption device which are connected in sequence. The method is characterized in that a medicament is added into a coagulating sedimentation tank, and lime, soda ash, caustic soda flakes, sodium sulfate and the like are used as common softening medicaments to remove scale ions such as calcium, magnesium, fluorine and silicon. After the filtrate is treated by the filtrate pretreatment device, the total hardness of liquid entering a salt production system can be ensured to be less than or equal to 2.5mg/L, fluorine is less than or equal to 0.5mg/L, and total silicon is less than or equal to 0.05 mg/L; the turbidity of the ultrafiltration effluent is less than or equal to 2NTU, the SS of the effluent is less than or equal to 5ppm, and the SDI of the effluent is less than or equal to 5.
Furthermore, flushing water, concentrated solution and resin regenerated solution generated by the sand filter tank, the ultrafiltration tank and the resin adsorption device can enter a flushing tank of the grade 1 flushing unit through a concentrated solution outlet, are combined with fly ash to form muddy water, and are continuously cleaned.
Further, the coagulating sedimentation tank comprises a first-stage coagulating sedimentation tank and a second-stage coagulating sedimentation tank. A sludge water outlet of the primary coagulating sedimentation tank is connected with a sludge dewatering device, and sludge generated by the sludge dewatering device can enter a rinsing bath of the 1-level rinsing unit; filtrate generated by the sludge dewatering device can enter the secondary coagulating sedimentation tank, and muddy water generated by the secondary coagulating sedimentation tank can enter the rinsing bath of the 1-level rinsing unit. The sludge dewatering device can adopt a sludge dewatering machine which is the same as a multi-stage countercurrent water washing device.
Another objective of the present application is to provide a fly ash treatment system, which comprises a high temperature melting unit and the fly ash washing system according to any of the above technical solutions. The high-temperature melting unit is used for calcining the sludge washed by the fly ash washing system at high temperature, and the high-temperature melting unit comprises but is not limited to a cement kiln. By adopting the technical scheme, the heavy metal in the fly ash is completely solidified in the crystal lattice of the cement clinker after being melted at high temperature, and the fly ash is thoroughly treated without aftertroubles; the temperature of a cement kiln system is up to above 1400 ℃, the calcination time is long, the combustion is complete, and the kiln is in an alkaline environment, so that the dioxin is efficiently decomposed, and the dioxin does not have secondary synthesis conditions any more.
Further, a sludge drying device is arranged between the fly ash washing system and the high-temperature melting unit, and the sludge drying device is communicated with the high-temperature melting unit so as to dry the cement by using the waste heat of the high-temperature melting unit. By adopting the technical scheme, the interference of the moisture content of the fly ash entering the kiln to the high-temperature melting unit can be reduced, the processing capacity of the high-temperature melting unit is improved, and the production waste heat is effectively utilized.
The beneficial effect of this application does:
the long-acting risk of solidification and landfill of the fly ash is avoided; solves the problems of the fly ash in the prior art such as the crust in the kiln, the corrosion of equipment/pipelines and the like, and completely realizes the reduction, the reclamation and the harmlessness of the waste incineration fly ash disposal.
Drawings
The invention will be described in further detail with reference to the following drawings and detailed description:
fig. 1 is a schematic view of a fly ash washing system according to an embodiment of the present invention.
Description of the element reference numerals
10: a multi-stage counter-current water washing device;
11: a stage 1 water washing unit; 12: a 2-stage water washing unit; 13: a 3-stage water washing unit; 14: grade 4 water washing sheet 15: a 5-stage water washing unit;
20 a filtrate treatment device; 21 a filtrate pretreatment device; 22 salt manufacturing system;
30 a biochemical system;
Detailed Description
The following description is provided for illustrative embodiments of the present invention, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein. While the invention will be described in conjunction with the preferred embodiments, it is not intended that features of the invention be limited to only those embodiments. On the contrary, the intention of implementing the novel features described in connection with the embodiments is to cover other alternatives or modifications which may be extended based on the claims of the present invention. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. The invention may be practiced without these particulars. Furthermore, some of the specific details are omitted from the description so as not to obscure or obscure the present invention. It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict.
In order to make the objects, technical solutions and advantages of the present invention clearer, embodiments of the present invention will be described in further detail below with reference to the accompanying drawings.
FIG. 1 shows a fly ash water wash system of one embodiment of the present application, including a multi-stage counter-current water wash apparatus 10, a filtrate treatment apparatus 20, and a biochemical system 30.
Specifically, in this embodiment, the multistage countercurrent water-washing apparatus 10 includes 5 water-washing units each provided with a washing tank and a sludge dehydrator, respectively. The level 1 washing unit 11 is provided with a fly ash inlet through which fly ash enters the washing tank of the level 1 washing unit 11 when the fly ash washing system is in use. The muddy water generated by the rinsing tank can enter the sludge dewatering machine through the muddy water inlet and is separated in the sludge dewatering machine to obtain sludge and filtrate. And then, the sludge can enter the rinsing bath of the 2-stage rinsing unit 12 through the sludge outlet, and so on, the sludge continuously enters the rinsing bath of the next-stage rinsing unit until the sludge is discharged from the sludge outlet of the 5-stage rinsing unit 15, and the sludge with the water content of about 40% is obtained. The sludge outlet of the 5-stage water washing unit 15 is connected to a sludge transfer device to send the sludge to a fly ash treatment unit of the next stage, such as a drying unit or a high-temperature melting unit.
The stage 5 water washing unit 15 is provided with an initial rinse water inlet through which initial rinse water enters the wash tank of the stage 5 rinse unit when the fly ash water washing system is in operation. Filtrate obtained by separating mud water in the 5-stage washing unit 15 by the sludge dewatering machine is conveyed to the washing tank of the 4-stage washing unit 14 through a filtrate outlet, and so on, the filtrate continuously enters the washing tank of the previous-stage washing unit until the filtrate is discharged from the filtrate outlet of the 1-stage washing unit 11 and enters the filtrate pretreatment device 21.
The residual chloride ion of the fly ash of the embodiment after multistage countercurrent elution is less than 10000mg/kg, the alkalinity is less than 100mg/kg, and no dust is generated. In the alkaline elution environment, the transfer rate of heavy metal and dioxin is low, and secondary collection and recovery of heavy metal can be carried out.
The filtrate treatment apparatus 20 includes a filtrate pretreatment apparatus 21 and a salt manufacturing system 22. In the embodiment shown in fig. 1, the filtrate pretreatment device 21 includes a coagulation sedimentation tank, a sand filtration tank, an ultrafiltration device, and a resin adsorption device, which are connected in this order. Specifically, the coagulating sedimentation tank comprises a primary coagulating sedimentation tank and a secondary coagulating sedimentation tank. A sludge water outlet of the first-stage coagulating sedimentation tank is connected with a sludge dewatering device, and sludge generated by the sludge dewatering device can enter a rinsing bath of the 1-stage rinsing unit 11; the filtrate produced by the sludge dewatering device can enter a secondary coagulating sedimentation tank, and muddy water produced by the secondary coagulating sedimentation tank also enters a rinsing bath of the 1-level rinsing unit 11. Liquid generated by the secondary sedimentation tank enters a sand filter tank, an ultrafiltration device and a resin adsorption device, and after treatment, washing water, concentrated solution and resin regeneration solution leave a filtrate pretreatment device 21 through a concentrated solution outlet and enter a washing tank of a 1-stage washing unit 11; the remaining liquid, as brine, leaves the filtrate pretreatment device 21 through a brine outlet and enters the brine production system 22.
In this embodiment, the salt production system 22 includes a nano-filtration salt separation device, an ozone oxidation device, a falling film concentration device, and an evaporative crystallization system, which are connected in sequence. Specifically, the salt manufacturing system of this embodiment further includes an electric boiler, and heat generated by the electric boiler is supplied to the falling film concentration device for evaporation concentration, the evaporation crystallization system for crystallization salt precipitation, and drying of the crystallized salt, respectively; also, the nano-filtration salt separation apparatus is exemplified by, but not limited to, a two-stage nano-filtration membrane system (two-stage NF membrane system) in the present embodiment. The liquid is divided into a water producing side and a concentrated water side by a nanofiltration salt separation device, wherein the concentrated water side is connected with a washing tank of a 1-level washing unit so as to inject concentrated water into the 1-level washing unit, and the water producing side is connected with an ozone oxidation device so as to carry out the subsequent salt making step; an evaporative crystallization system such as, but not limited to, the MVR evaporative crystallization system in this example. During the evaporative crystallization, KCl and NaCl crystallization salts, other mixed salts, residual mother liquor and condensate can be generated. Other mixed salt does not meet the latest landfill standard, so the mixed salt returns to the nano-filtration salt separation device again, and is continuously recycled for filtration and salt separation.
An inlet of the biochemical system 30 is in communication with a liquid outlet of the salt production system 22 and is capable of receiving the remaining mother liquor and condensate from the salt production system 22. The rest mother liquor can be diluted by condensate, and the diluted rest mother liquor enters a rinsing bath of the 5-level rinsing unit after being treated by the biochemical system 30; and condensate liquid which is excessive in diluting residual mother liquor can directly enter a rinsing bath of the 5-stage rinsing unit 15. As shown in fig. 1, a water outlet of the biochemical system 30 is communicated with a rinsing bath of the 5-stage rinsing unit 15, and effluent treated by the biochemical system 30 flows back to the multi-stage counter-current rinsing system; meanwhile, the condensate can directly flow back to the multistage countercurrent washing system without a biochemical system, is combined with the initial rinsing water and is jointly used as washing and dewatering, so that zero discharge of waste liquid is really realized, and the consumption of the initial rinsing water is reduced.
In the embodiment, the fly ash enters the fly ash washing system at a rate of about 25t/h (ton/hour), and the fly ash is washed and dechlorinated by the fly ash washing system according to 1000 ten thousand tons of annual fly ash, so that the fly ash can be completely converted into qualified cement clinker by the cement kiln with one tenth of the cement clinker production capacity in China, the raw materials are saved, and the resource utilization of the fly ash is realized.
The present application also provides an embodiment of a fly ash treatment system, comprising the fly ash washing system and the high temperature melting unit shown in the above examples. In the embodiment, the high-temperature melting unit is a cement kiln, heavy metals in the fly ash are completely solidified in the crystal lattice of the cement clinker after being melted by the cement kiln at high temperature, and the thorough treatment is free from aftereffects; the temperature of the cement kiln system is up to above 1400 ℃, the calcination time is long, and the combustion is complete; and the kiln is in an alkaline environment, so that the dioxin is efficiently decomposed, and the dioxin does not have secondary synthesis conditions any more.
In any of the embodiments of the fly ash treatment system of the present application, a sludge drying device is included between the fly ash washing system and the high temperature melting unit, and the sludge drying device is communicated with the high temperature melting unit to dry the sludge by using the residual heat of the high temperature melting unit. Therefore, the interference of the moisture content of the fly ash entering the kiln to the cement kiln can be reduced, the processing capacity of the cement kiln is improved, and the production waste heat is effectively utilized.
While the invention has been shown and described with reference to certain preferred embodiments thereof, it will be understood by those skilled in the art that the foregoing is a more detailed description of the invention, and the specific embodiments thereof are not to be considered as limiting. Various changes in form and detail, including simple deductions or substitutions, may be made by those skilled in the art without departing from the spirit and scope of the invention.
Claims (10)
1. A fly ash water wash system, comprising:
multistage countercurrent water washing device, including n washing unit, and n is greater than or equal to 3, the washing unit includes:
the washing tank is provided with a muddy water outlet; the rinsing bath of the 1-level water washing unit is provided with a fly ash inlet, and the rinsing bath of the n-level water washing unit is provided with an initial rinsing water inlet; and the number of the first and second groups,
the sludge dewatering machine is used for separating mud and water which are washed by the water washing tank to obtain sludge and filtrate, and comprises a mud and water inlet, a sludge outlet and a filtrate outlet; wherein, the sludge outlet of the 1 to n-1 level washing unit is communicated with the washing tank of the next level washing unit, and the sludge outlet of the n level washing unit is connected with the sludge conveying device; filtrate outlets of the 2-n stages of water washing units are communicated with a water washing tank of the upper stage of water washing unit;
filtrate treatment apparatus for obtaining crystalline salt and residual mother liquor comprising:
the inlet of the filtrate pretreatment device is connected with the filtrate outlet of the sludge dewatering machine of the grade 1 water washing unit, the filtrate pretreatment device comprises a concentrated solution outlet and a brine making outlet, and the concentrated solution outlet is communicated with the water washing tank of the grade 1 water washing unit; and the number of the first and second groups,
the inlet of the salt making system is communicated with the salt making water outlet of the filtrate pretreatment device, and the salt making system comprises a liquid outlet which is used for conveying condensate and residual mother liquor generated in the salt making process;
the inlet of the biochemical system is communicated with the liquid outlet of the salt making system, and the water outlet of the biochemical system is communicated with the rinsing bath of the n-level rinsing unit.
2. A fly ash water wash system as claimed in claim 1, wherein in the multistage counter-current water wash apparatus n-5.
3. A fly ash washing system according to claim 1, wherein the salt making system comprises a nano-filtration salt separation device, an ozone oxidation device, a falling film concentration device, and an evaporative crystallization system, connected in series.
4. A fly ash washing system as claimed in claim 3, wherein the nano filtration salt separation device is capable of separating the liquid received from the filtrate pretreatment device into a water production side and a concentrate side, the concentrate side being in communication with the wash tank of the stage 1 wash unit and the water production side being in communication with the ozone oxidation device.
5. A fly ash water wash system as claimed in claim 3 wherein the salt production system comprises an electric boiler, the heat energy generated by the electric boiler being used partly as a heat source for the falling film concentration device and the evaporative crystallization system and partly as a heat source for drying the crystallized salt.
6. A fly ash washing system as claimed in claim 1, wherein the filtrate pretreatment device comprises a coagulation sedimentation tank, a sand filtration tank, an ultrafiltration device and a resin adsorption device connected in sequence.
7. A fly ash washing system as claimed in claim 6, wherein the wash water, the concentrate and the resin regenerant produced by the sand filtration tank, the ultrafiltration tank and the resin adsorption device can enter the wash tank of the stage 1 washing unit through the concentrate outlet.
8. A fly ash washing system according to claim 6, wherein the coagulation sedimentation tank comprises:
the sludge water outlet of the primary coagulation sedimentation tank is connected with a sludge dewatering device; the sludge generated by the sludge dewatering device can enter a rinsing bath of the grade 1 rinsing unit;
and the filtrate generated by the sludge dewatering device can enter the secondary coagulating sedimentation tank, and the muddy water generated by the secondary coagulating sedimentation tank can enter the rinsing bath of the 1-level rinsing unit.
9. A fly ash treatment system is characterized by comprising
A fly ash water washing system as claimed in any one of claims 1 to 8; and the number of the first and second groups,
and the high-temperature melting unit is used for calcining the sludge washed by the fly ash washing system at high temperature.
10. A fly ash treatment system as claimed in claim 9, comprising a sludge drying device between the fly ash washing system and the high temperature fusion unit, the sludge drying device being in communication with the high temperature fusion unit, the sludge drying device using the residual heat of the high temperature fusion unit to dry the sludge.
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