CN112845541A - Fly ash washing and resource comprehensive utilization system - Google Patents
Fly ash washing and resource comprehensive utilization system Download PDFInfo
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- CN112845541A CN112845541A CN202110177112.4A CN202110177112A CN112845541A CN 112845541 A CN112845541 A CN 112845541A CN 202110177112 A CN202110177112 A CN 202110177112A CN 112845541 A CN112845541 A CN 112845541A
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- 239000010881 fly ash Substances 0.000 title claims abstract description 132
- 238000005406 washing Methods 0.000 title claims abstract description 39
- 238000011001 backwashing Methods 0.000 claims abstract description 70
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 56
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000011575 calcium Substances 0.000 claims abstract description 50
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 49
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 49
- 239000007788 liquid Substances 0.000 claims abstract description 47
- 239000000706 filtrate Substances 0.000 claims abstract description 35
- 238000007711 solidification Methods 0.000 claims abstract description 31
- 230000008023 solidification Effects 0.000 claims abstract description 30
- 238000006298 dechlorination reaction Methods 0.000 claims abstract description 28
- 239000003480 eluent Substances 0.000 claims abstract description 23
- 239000004568 cement Substances 0.000 claims abstract description 21
- 238000001035 drying Methods 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 14
- 230000008020 evaporation Effects 0.000 claims abstract description 14
- 239000002893 slag Substances 0.000 claims abstract description 14
- 150000003839 salts Chemical class 0.000 claims abstract description 11
- 238000004064 recycling Methods 0.000 claims abstract description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 40
- 238000006243 chemical reaction Methods 0.000 claims description 31
- 238000003825 pressing Methods 0.000 claims description 28
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 27
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 25
- 229910052717 sulfur Inorganic materials 0.000 claims description 24
- 239000011593 sulfur Substances 0.000 claims description 24
- 238000006477 desulfuration reaction Methods 0.000 claims description 23
- 230000023556 desulfurization Effects 0.000 claims description 23
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 229910021529 ammonia Inorganic materials 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 8
- 239000002253 acid Substances 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 238000001354 calcination Methods 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 230000000382 dechlorinating effect Effects 0.000 claims description 2
- 238000011282 treatment Methods 0.000 abstract description 12
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 11
- 239000000460 chlorine Substances 0.000 abstract description 11
- 229910052801 chlorine Inorganic materials 0.000 abstract description 11
- 239000002994 raw material Substances 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 abstract description 3
- 239000010865 sewage Substances 0.000 abstract description 2
- 238000010612 desalination reaction Methods 0.000 abstract 1
- BITYAPCSNKJESK-UHFFFAOYSA-N potassiosodium Chemical compound [Na].[K] BITYAPCSNKJESK-UHFFFAOYSA-N 0.000 abstract 1
- 238000001723 curing Methods 0.000 description 55
- 239000007787 solid Substances 0.000 description 17
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 15
- 239000007789 gas Substances 0.000 description 11
- 239000000203 mixture Substances 0.000 description 8
- 230000001502 supplementing effect Effects 0.000 description 6
- 239000013589 supplement Substances 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- AYJRCSIUFZENHW-UHFFFAOYSA-L barium carbonate Chemical compound [Ba+2].[O-]C([O-])=O AYJRCSIUFZENHW-UHFFFAOYSA-L 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000001125 extrusion Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 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 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 230000000087 stabilizing effect Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- 238000004056 waste incineration Methods 0.000 description 2
- JTNCEQNHURODLX-UHFFFAOYSA-N 2-phenylethanimidamide Chemical compound NC(=N)CC1=CC=CC=C1 JTNCEQNHURODLX-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910001294 Reinforcing steel Inorganic materials 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
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- WDIHJSXYQDMJHN-UHFFFAOYSA-L barium chloride Chemical compound [Cl-].[Cl-].[Ba+2] WDIHJSXYQDMJHN-UHFFFAOYSA-L 0.000 description 1
- 229910001626 barium chloride Inorganic materials 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- UHZZMRAGKVHANO-UHFFFAOYSA-M chlormequat chloride Chemical compound [Cl-].C[N+](C)(C)CCCl UHZZMRAGKVHANO-UHFFFAOYSA-M 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
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- GDVKFRBCXAPAQJ-UHFFFAOYSA-A dialuminum;hexamagnesium;carbonate;hexadecahydroxide Chemical compound [OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[OH-].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Mg+2].[Al+3].[Al+3].[O-]C([O-])=O GDVKFRBCXAPAQJ-UHFFFAOYSA-A 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 229960001545 hydrotalcite Drugs 0.000 description 1
- 229910001701 hydrotalcite Inorganic materials 0.000 description 1
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910000343 potassium bisulfate Inorganic materials 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011150 reinforced concrete Substances 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- WBHQBSYUUJJSRZ-UHFFFAOYSA-M sodium bisulfate Chemical compound [Na+].OS([O-])(=O)=O WBHQBSYUUJJSRZ-UHFFFAOYSA-M 0.000 description 1
- 229910000342 sodium bisulfate Inorganic materials 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002699 waste material Substances 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B2101/00—Type of solid waste
- B09B2101/30—Incineration ashes
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The embodiment of the invention relates to a fly ash washing desalination treatment technology, and discloses a fly ash washing and resource comprehensive utilization system.A filter press residue outlet of a fly ash calcium and heavy metal solidification unit is connected with an inlet of a step backwashing dechlorination unit, and a filter press liquid outlet is connected with an inlet of a filter press liquid desulphurization unit; an eluent outlet of the step backwashing dechlorination unit is connected with an inlet of the fly ash calcium and heavy metal cooperative solidification unit, and a washing slag outlet of the backwashing dechlorination unit is connected with an inlet of the drying unit; the liquid outlet of the pressure filtrate desulphurization unit is connected with the inlet of the evaporation salt-making unit, and the eluent desulphurization slag outlet is connected with the inlet of the fly ash calcium and heavy metal cooperative solidification unit; the condensed water returns to the step backwashing dechlorination unit for recycling; the outlet of the slag washing and drying unit is connected with the inlet of the cement kiln, the chlorine in the fly ash is less than 1 percent, the fly ash can be directly used for cement raw materials, various indexes of eluent meet the GB8978 discharge standard, the fly ash can directly enter an industrial sewage treatment plant or be evaporated to prepare salt to obtain a potassium-sodium salt product, and the triple treatment of the fly ash is realized.
Description
Technical Field
The embodiment of the invention relates to a fly ash washing and desalting treatment technology, in particular to a fly ash washing and resource comprehensive utilization system.
Background
Fly ash harmless treatment waste incineration fly ash is a substance collected in a heat recovery and utilization system and a flue gas purification system after waste incineration. Industrial refuse incinerators generally use Ca (OH)2The incineration fly ash obtained after cloth bag dust removal contains heavy metals such as Pb, Zn, Cu and the like, dioxin and a large amount of soluble chloride, and if the incineration fly ash is not treated properly, the heavy metals and the strong brine can be migrated to pollute underground water, soil and air. Therefore, it must be handled. There are generally several treatments: the materials are appropriately treated and buried according to the hazardous waste. But the treatment cost is higher; ② curing and stabilizing. The main curing methods include cement curing, asphalt curing, melt curing, chemical agent curing and stabilizing, and the like. The solidified fly ash can be landfilled as common waste if meeting the requirement of leaching toxicity standard. The main function of the fly ash is to make the heavy metals and the pollution components thereof in the fly ash chemically inert or contained so as to be convenient for transportation and treatment, and can reduce the toxicity of pollutants and reduce the migration rate of the pollutants to an ecological circle; thirdly, the fly ash is washed and dechlorinated, and is directly used as a cement additive, heavy metals are dispersed in cement clinker to reach the safety standard, and harmless decomposition is realized by roasting the dioxin cement kiln. The third method has good economic benefit for resource utilization of pollutants in the fly ash and avoids the problem of secondary pollution of pollution components of the fly ash, and has obvious advantages.
The fly ash is burnt, washed and dechlorinated to be used as building material raw materials such as cement and the like, and is an important economic way for harmless treatment of the fly ash. The common method in the market is to remove chloride ions from fly ash by washing and the like, so as to reach the use standard of cement raw materials. Because too high chloride ions are easy to accelerate the corrosion of materials such as reinforcing steel bars in a cement reinforced concrete system. In the cement quality standard GB175-2007, the requirement on the content of chloride ions is less than 0.06%, and the content of chlorine as a cement raw material is less than 1%.
The inventor of the invention finds the following problems in the prior art: the existing equipment and process for performing harmless treatment on fly ash on the market and using the fly ash as a cement raw material exist: high residual chlorine content, high residue moisture content, large equipment energy consumption and large water consumption, and is easy to cause secondary environmental pollution. The market urgently needs a fly ash harmless treatment device which can effectively remove chloride ions and save energy consumption and water resources.
Disclosure of Invention
The invention aims to provide a fly ash washing and comprehensive resource utilization system, which can effectively remove chloride ions and save energy and water resources.
In order to solve the above technical problems, an embodiment of the present invention provides a system for washing fly ash and comprehensively utilizing resources, including: the system comprises a fly ash bin, a fly ash calcium and heavy metal cooperative solidification unit, a step backwashing dechlorination unit, a drying unit, a filtrate pressing sulfur removal unit, an evaporation salt production unit and a cement kiln unit;
the fly ash calcium and heavy metal cooperative solidification unit is provided with a filter-pressing residue outlet and a filter-pressing liquid outlet, the filter-pressing residue outlet is connected with an inlet of the step backwashing dechlorination unit, and the filter-pressing liquid outlet is connected with an inlet of the filter-pressing liquid sulfur removal unit; an eluent outlet of the step backwashing dechlorination unit is connected with an inlet of the fly ash calcium and heavy metal cooperative solidification unit, and a washing slag outlet of the backwashing dechlorination unit is connected with an inlet of the drying unit; the liquid outlet of the pressure filtrate sulfur removal unit is connected with the inlet of the evaporation salt production unit, and the sulfur removal slag outlet of the eluent of the pressure filtrate sulfur removal unit is connected with the inlet of the fly ash calcium and heavy metal cooperative solidification unit; condensed water generated by the evaporation salt-making unit returns to the step backwashing dechlorination unit for recycling; and the outlet of the slag washing and drying unit is connected with the inlet of the cement kiln.
Further optionally, the fly ash calcium and heavy metal cooperative curing unit comprises a high-efficiency premixer, a calcium and heavy metal curing reaction kettle, a curing agent bin, an extrusion type filter press and an ammonia gas absorption tower;
the inlet of the high-efficiency premixer is respectively connected with the outlet of the fly ash metering device, the outlet of the water distribution metering device, the outlet of the curing agent bin and the desulphurizing slag outlet of the pressure filtrate desulphurizing unit, the outlet of the high-efficiency premixer is connected with the inlet of the calcium and heavy metal solidification reaction kettle, the material outlet of the calcium and heavy metal solidification reaction kettle is connected with the inlet of the extrusion type filter press, the pressure filtrate outlet of the extrusion type filter press is connected with the inlet of the eluent desulphurizing unit, the pressure filter residue outlet is connected with the inlet of the step backwashing dechlorinating unit, and the gas outlet of the calcium and heavy metal solidification reaction kettle is connected with the inlet of.
Further optionally, the step backwashing dechlorination unit comprises a high-efficiency rinsing bath and a backwashing filter press or a belt filter, an inlet of the high-efficiency rinsing bath is connected with an outlet of the filter pressing residue, an outlet of the high-efficiency rinsing bath is connected with an inlet of the backwashing filter press or the belt filter, a backwashing liquid of the backwashing filter press or the belt filter is connected with an inlet of the water distribution metering device of the fly ash calcium and heavy metal co-curing unit, and a filter residue of the backwashing filter press or the belt filter is connected with an inlet of the drying unit.
Further optionally, the eluent desulfurization unit comprises a sulfur fixation reaction kettle, a solid-liquid separation concentration device, a desulfurization agent bin and an acid storage tank, wherein an inlet of the sulfur fixation reaction kettle is respectively connected with an outlet of a filtrate pressed by a fly ash calcium and heavy metal cooperative curing unit filter press, an outlet of an acid preparation metering device and an outlet of the desulfurization agent bin, an inlet of the sulfur fixation reaction kettle is connected with an inlet of the solid-liquid separation concentration device, an outlet of a filtrate pressed by a third filter press or a precision filter is connected with an inlet of an evaporation salt making unit, and filter residue or concentrated phase of the third filter press or the precision filter is connected with an inlet of a high-efficiency premixer.
Further optionally, the drying unit includes a conveyor belt, a dryer, and a dry fly ash bin, an outlet of the conveyor belt is connected to an inlet of the dryer, an outlet of the dryer is connected to an inlet of the dry fly ash bin, and an outlet of the dry fly ash bin is connected to the kiln entering calcination unit.
The foregoing description is only an overview of the technical solutions of the present invention, and the embodiments of the present invention are described below in order to make the technical means of the present invention more clearly understood and to make the above and other objects, features, and advantages of the present invention more clearly understandable.
Drawings
One or more embodiments are illustrated by way of example in the accompanying drawings, which correspond to the figures in which like reference numerals refer to similar elements and which are not to scale unless otherwise specified.
FIG. 1 is a schematic diagram of a fly ash washing and comprehensive resource utilization system according to an embodiment of the present invention;
FIG. 2 is a schematic block diagram of an embodiment of the system of FIG. 1.
Fly ash calcium and heavy metal cooperative solidification unit 1, step backwashing dechlorination unit 2, filtrate pressure desulfurization unit 3, drying unit 4, evaporation salt making unit 5 and cement kiln unit 6;
the device comprises a high-efficiency premixer 11, a curing reaction kettle 12, a curing agent bin 13, a (primary) squeezer 14, an ammonia absorption tower 15, a fly ash bin 16, a (secondary) high-efficiency rinsing bath 17, a secondary backwashing filter press or belt filter 18, a three-stage backwashing filter press or belt filter 19, a (three-stage) high-efficiency rinsing bath 20, a desulfurization and calcium fixation reactor 21, a filter 22, a desulfurizer bin 23 and a heavy metal curing agent bin 24.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, embodiments of the present invention will be described in detail below with reference to the accompanying drawings. However, it will be appreciated by those of ordinary skill in the art that numerous technical details are set forth in order to provide a better understanding of the present application in various embodiments of the present invention. However, the technical solution claimed in the present application can be implemented without these technical details and various changes and modifications based on the following embodiments. The following embodiments are divided for convenience of description, and should not constitute any limitation to the specific implementation manner of the present invention, and the embodiments may be mutually incorporated and referred to without contradiction.
The first embodiment of the present invention relates to a system for washing fly ash and comprehensively utilizing resources, which comprises: the system comprises a fly ash bin 16, a fly ash calcium and heavy metal cooperative solidification unit 1, a step backwashing dechlorination unit 2, a press filtrate desulphurization unit 3, a drying unit 4, an evaporation salt production unit 5 and a cement kiln unit 6;
the fly ash calcium and heavy metal cooperative solidification unit is provided with a filter-pressing residue outlet and a filter-pressing liquid outlet, the filter-pressing residue outlet is connected with an inlet of the step backwashing dechlorination unit, and the filter-pressing liquid outlet is connected with an inlet of the filter-pressing liquid sulfur removal unit; an eluent outlet of the step backwashing dechlorination unit is connected with an inlet of the fly ash calcium and heavy metal cooperative solidification unit, and a washing slag outlet of the backwashing dechlorination unit is connected with an inlet of the drying unit; a liquid outlet of the pressure filtrate sulfur removal unit is connected with an inlet of the evaporation salt making unit, and an eluent sulfur removal slag outlet of the pressure filtrate sulfur removal unit is connected with an inlet of the fly ash calcium and heavy metal cooperative solidification unit; condensed water generated by the evaporation salt-making unit returns to the step backwashing dechlorination unit for recycling; the outlet of the slag washing and drying unit is connected with the inlet of the cement kiln.
Further optionally, the fly ash calcium and heavy metal cooperative curing unit comprises an efficient premixer 11, a curing reaction kettle 12, a curing agent bin 13, a (primary) squeezer 14 and an ammonia absorption tower 15;
the entry of high-efficient premixer 11 respectively with the export of fly ash metering device, the export of water distribution metering device, the export of curing agent feed bin 13, the sulphur removal sediment export of pressure filtrate sulphur removal unit links to each other, the export of high-efficient premixer 11 links to each other with solidification reaction kettle 12 entry, solidification reaction kettle 12's material export links to each other with (one-level) squeezer 14 entry, (one-level) squeezer 14 presses the export of filtrate and links to each other with eluant sulphur removal unit import, the export of pressure filtration sediment links to each other with step backwash dechlorination unit import, solidification reaction kettle 12 gas outlet links to each other with ammonia absorption tower 15 entry, (one-level) squeezer 14 can adopt extrusion pressure filter.
As shown in fig. 2, the fly ash calcium and heavy metal co-solidification unit may include: a fly ash bin 16, a high-efficiency premixer 11, a (primary) squeezer 14, a curing agent bin 13, an ammonia absorption tower 15, a curing reaction kettle 12 and a water supplementing device.
The high-efficiency premixer 11 can pre-treat the fly ash, pre-mix the curing agent bin 13 and the fly ash, the curing agent can cure calcium and heavy metals in the fly ash, and the curing agent comprises one or more of ferrous sulfate heptahydrate, aluminum sulfate, potassium sulfate, sodium sulfate, ferric sulfate, sodium carbonate, sodium bisulfate, potassium bisulfate and magnesium sulfate. The high-efficiency premixer 11 is provided with a gas inlet, a liquid inlet, a material inlet, a gas outlet and a mixture outlet;
the fly ash bin 16 is used for carrying and conveying fly ash, the outlet of the fly ash bin 16 is communicated with the gas inlet of the high-efficiency premixer 11, and the fly ash bin 16 blows the fly ash into the high-efficiency premixer 11 in a gas form through a gas pressure conveying mode.
The inlet of the ammonia absorption tower 15 is communicated with the gas outlet of the high-efficiency premixer 11; the ammonia gas absorption tower 15 is used for absorbing ammonia gas in the fly ash so as to reduce the ammonia nitrogen content in the fly ash, and distilled water or weak hydrochloric acid is adopted as absorption liquid in the ammonia gas absorption tower 15.
An outlet of the curing agent bin 13 is communicated with a material inlet of the high-efficiency premixer 11, the curing agent bin 13 carries the curing agent, and the curing agent is conveyed and supplemented when the content of the curing agent in the high-efficiency premixer 11 is reduced.
The outlet of the water supplementing device is communicated with the liquid inlet of the high-efficiency premixer 11, and the water adding inlet of the water supplementing device is provided with a water quantity metering device. The water supplementing device is used for supplementing liquid water into the curing reaction kettle and calculating the water supplementing amount through the water amount metering device.
The mixture outlet of the high-efficiency premixer 11 is communicated with the inlet of the curing reaction kettle 12, and the curing reaction kettle 12 is a vertical stirrer or a horizontal stirrer. The mixture delivered by the high-efficiency premixer 11 is subjected to sufficient contact reaction in the curing reaction kettle 12. The outlet of the curing reaction kettle 12 is connected with the inlet of a (primary) presser 14; the (first stage) squeezer 14 filters the mixture discharged from the solidification reaction kettle 12, and the filtrate of the (first stage) squeezer 14 enters a water purification system, and the filter residue enters a water washing dechlorination reactor. The (primary) press 14 is selected from one of a filter press, a belt filter, a horizontal screw centrifuge, and a disk centrifuge.
Further optionally, the step backwashing dechlorination unit comprises a high-efficiency rinsing bath and a backwashing filter press or a belt filter, an inlet of the high-efficiency rinsing bath is connected with an outlet of filter pressing residues, an outlet of the high-efficiency rinsing bath is connected with an inlet of the backwashing filter press or the belt filter, a backwashing liquid of the backwashing filter press or the belt filter is connected with an inlet of a water distribution metering device of the fly ash calcium and heavy metal co-curing unit, and a filter residue of the backwashing filter press or the belt filter is connected with an inlet of a drying unit.
As shown in fig. 2, in some embodiments, the step backwash dechlorination unit mainly comprises: a fly ash bin 16, a high-efficiency premixer 11, a (primary) squeezer 14, a (secondary) high-efficiency washing tank 17, a secondary backwashing filter press or belt filter 18, a (tertiary) high-efficiency washing tank 20, a tertiary backwashing filter press or belt filter 19, a curing agent bin 13, an ammonia gas absorption tower 15 and the high-efficiency premixer 11.
When the fly ash is started for the first time, fly ash in a fly ash bin 16 enters the high-efficiency premixer 11 along with a conveying system, water is fed through a water replenishing port of the high-efficiency premixer 11 to complete fly ash and water premixing, and the fly ash and water enters the ammonia absorption tower 15 through a pipeline; the fly ash and water premix enters an efficient premixer 11, calcium element and heavy metal in the fly ash are synergistically solidified under the action of a curing agent added into a curing agent bin 13, and chloride ions are initially dissolved in water; the fly ash, chloride ions and the solidified mixture are separated from the heavy metal condensate and part of the chloride ions and the fly ash under the action of a (primary) squeezer 14; (first stage) the eluate from the press 14 is processed separately; the (first-stage) presser 14 presses and filters the solid matter into the (second-stage) high-efficiency washing tank 17 and mixes with the pressure filtrate of the three-stage backwashing filter press or belt filter 19; the mixture enters a secondary backwashing filter press or a belt filter 18, and the chlorine ion-containing filter press liquid is separated from the solid containing the fly ash, so that the chlorine content in the solid is further reduced; the solid containing the fly ash obtained by the second-stage filter pressing enters a (third-stage) high-efficiency rinsing bath 20, is mixed with make-up water and enters a third-stage backwashing filter press or a belt filter; the secondary filter pressing generates filter pressing liquid which flows back to the high-efficiency premixer 11; the three-stage backwashing filter press or belt filter 19 completes the separation of chlorine-containing pressure filtrate and solid matter containing fly ash, wherein the pressure filtrate flows back to the (second stage) high-efficiency washing tank 17, and the solid matter is dewatered and washed to obtain a fly ash concentrated product.
The high-efficiency premixer 11 is provided with a water replenishing port, and the outlet of the fly ash bin 16 is connected with the feed inlet of the high-efficiency premixer 11; the outlets of the high-efficiency premixer 11, the curing agent bin 13 and the filter-pressing liquid and backwash liquid of the secondary backwash type filter press or belt filter 18 are connected with the inlet of the high-efficiency premixer 11; the gas outlet of the high-efficiency premixer 11 is connected with the inlet of the ammonia absorption tower 15; after washing is finished, a slurry outlet of the high-efficiency premixer 11 is connected with an inlet of a (primary) squeezer 14 for solid-liquid separation; the (first-stage) presser 14 presses the filtrate outlet to connect with eluent purification system, the outlet of dehydration dregs enters the (second-stage) high-efficiency rinsing bath 17 through the conveying belt.
Meanwhile, when a second-level backwashing filter press or a third-level backwashing filter press or a belt filter in the system operates for a certain period, the filtering pressure is too large, and backwashing operation is required when the liquid output is small: the three-stage backwashing eluent generated by water supplement at the three-stage backwashing filter press or the belt filter 19 passes through the two-stage backwashing filter press or the belt filter 18 and is backwashed, and the generated two-stage backwashing eluent is converged into the (first-stage) squeezer.
In some alternative embodiments, the liquid-solid ratio can be set to 1:1-2:1, the water amount of the eluent to be purified is only 50% -150% of the mass of the fly ash, and the chlorine in the fly ash after washing is less than 1%, so that the eluent can be directly used for the cement raw material.
On the basis of the disclosed embodiments, the embodiment of the fly ash washing and resource comprehensive utilization system is preferably disclosed. The method mainly comprises the following steps: a fly ash bin 16, a high-efficiency premixer 11, a (primary) squeezer 14, a (secondary) high-efficiency washing tank 17, a secondary backwashing filter press or belt filter 18, a (tertiary) high-efficiency washing tank 20, a tertiary backwashing filter press or belt filter 19, a curing agent bin 13, an ammonia gas absorption tower 15 and the high-efficiency premixer 11.
In a stable operation state, fly ash in a fly ash bin 16 enters the high-efficiency premixer 11 along with a conveying system, a water replenishing port of the high-efficiency premixer 11 is closed, water enters a filter pressing liquid part through a secondary backwashing filter press or a belt filter 18 to complete fly ash and water premixing, and the fly ash and water enters an ammonia gas absorption tower 15 through a pipeline; the fly ash and water premix enters an efficient premixer 11, calcium element and heavy metal in the fly ash are synergistically solidified under the action of a curing agent added into a curing agent bin 13, and chloride ions are initially dissolved in water; the fly ash, chloride ions and the solidified mixture are separated from the heavy metal condensate and part of the chloride ions and the fly ash under the action of a (primary) squeezer 14; (first stage) the eluate from the press 14 is processed separately; the (first-stage) presser 14 presses and filters the solid matter into the (second-stage) high-efficiency washing tank 17 and mixes with the pressure filtrate of the three-stage backwashing filter press or belt filter 19; the mixture enters a secondary backwashing filter press or a belt filter 18, and the chlorine ion-containing filter press liquid is separated from the solid containing the fly ash, so that the chlorine content in the solid is further reduced; the solid containing the fly ash obtained by the second-stage filter pressing enters a (third-stage) high-efficiency rinsing bath 20, is mixed with make-up water and enters a third-stage backwashing filter press or a belt filter; the secondary filter pressing generates filter pressing liquid which flows back to the high-efficiency premixer 11; the three-stage backwashing filter press or belt filter 19 completes the separation of chlorine-containing pressure filtrate and solid matter containing fly ash, wherein the pressure filtrate flows back to the (second stage) high-efficiency washing tank 17, and the solid matter is dewatered and washed to obtain a fly ash concentrated product.
In some alternative embodiments, the liquid-solid ratio can be set to 1:1-2:1, the water amount of the eluent to be purified is only 50% -150% of the mass of the fly ash, and the chlorine in the fly ash after washing is less than 1%, so that the eluent can be directly used for the cement raw material.
Based on the disclosed embodiments, the specific parameters of the step backwashing dechlorination unit are as follows in some embodiments:
the liquid-solid ratio is 2:1, and the water amount of the eluent to be purified is only 120 percent of the mass of the fly ash; the feeding amount of fly ash is 15 t/h; when the system is started, the water inflow of the high-efficiency premixer is 30 t/h; the reflux amount of the filtrate and backwash liquid of the high-efficiency premixer is 30 t/h; the volume of the first-stage high-efficiency rinsing bath is 10 cubic meters; the processing capacity of a (primary) squeezer is 45 t/h; the volume of the second-stage efficient rinsing bath is 5 cubic; the processing capacity of the two-stage backwashing filter press or the belt filter is 45 t/h; the volume of the three-stage high-efficiency rinsing bath is 5 cubic; 45t/h of a three-stage backwashing filter press or a belt filter; the water supplement amount of the three-stage high-efficiency water washing tank is 15 t/h;
the backwashing water supplement amount is 15 t/h.
The test shows that the output of the treated fly ash is 12t/h, and the residual chlorine in the washed fly ash is 0.5 percent
Based on the disclosed embodiments, the specific parameters of the step backwashing dechlorination unit are as follows in some embodiments:
the liquid-solid ratio is 1:1, and the water amount of the eluent to be purified is only 50 percent of the mass of the fly ash; the feeding amount of fly ash is 10 t/h; when the system is started, the water inflow of the high-efficiency premixer is 10 t/h; the reflux amount of the filter pressing liquid and the backwash liquid of the high-efficiency premixer is 10 t/h; the volume of the first-stage high-efficiency rinsing bath is 5 cubic; the processing capacity of a (primary) squeezer is 20 t/h; the volume of the second-stage efficient rinsing bath is 3 cubic; the processing capacity of the two-stage backwashing filter press or the belt filter is 20 t/h; the volume of the three-stage high-efficiency rinsing bath is 3 cubic; 20t/h of a three-stage backwashing filter press or a belt filter; the water supplement amount of the three-stage efficient rinsing bath is 6 t/h;
the backwashing water supplement amount is 4 t/h.
The test shows that the output of the treated fly ash is 8t/h, and the residual chlorine in the washed fly ash is 0.98 percent
Further optionally, the eluent desulfurization unit comprises a sulfur fixation reaction kettle, a solid-liquid separation concentration device, a desulfurization agent bin and an acid storage tank, wherein an inlet of the sulfur fixation reaction kettle is respectively connected with a filtrate outlet of a fly ash calcium and heavy metal synergistic curing unit filter press, an outlet of an acid preparation metering device and an outlet of the desulfurization agent bin, an inlet of the sulfur fixation reaction kettle is connected with an inlet of the solid-liquid separation concentration device, a filtrate outlet of a third filter press or a precision filter is connected with an inlet of an evaporation salt making unit, and filter residue or concentrated phase of the third filter press or the precision filter is connected with an inlet of the high-efficiency premixer 11.
As shown in fig. 2, in some alternative embodiments, the pressure filtrate sulfur removal unit comprises: a fly ash washing liquid storage tank, a desulfurization calcium fixation reactor 21, a filter 22, a desulfurizer bin 23 and a heavy metal curing agent bin 24.
The desulfurization calcium fixation reactor 21 bears a heavy metal curing agent and a desulfurizer, and can cure sulfur, calcium and heavy metals in fly ash, and the heavy metal curing agent comprises one or more of sodium sulfide, micro-nano zero-valent iron, polyaluminium chloride, PAM and polyferric sulfate; the desulfurizer comprises one or more of hydrotalcite, witherite, barium chloride, barium carbonate and sodium aluminate. The curing reaction kettle is provided with a gas inlet, a liquid inlet, a material inlet, a gas outlet and a slurry outlet.
The fly ash washing liquid storage tank is used for carrying and conveying fly ash washing liquid, and an outlet of the fly ash washing liquid storage tank is communicated with an inlet of the desulfurization calcium fixation reactor 21.
The outlet of the desulfurizer bin 23 is communicated with the inlet of the desulfurization and calcium fixation reactor 21; the desulfurizer silo 23 is provided with a weight metering device capable of metering the weight of the desulfurizer input from the desulfurizer silo 23 to the desulfurization calcium fixation reactor 21.
The outlet of the heavy metal curing agent bin 24 is communicated with the inlet of the desulfurization calcium fixation reactor 21, the heavy metal curing agent is loaded in the heavy metal curing agent bin 24, a weight metering device is arranged on the heavy metal curing agent bin 24, and the weight of the desulfurizer input into the desulfurization calcium fixation reactor 21 from the heavy metal curing agent bin 24 can be metered. The weight metering devices of the heavy metal curing agent bin 24 and the desulfurizer bin 23 can accurately calculate the weight ratio of the heavy metal curing agent to the desulfurizer, and the effects of desulfurization and heavy metal curing are improved.
The outlet of the desulfurization and calcium fixation reactor 21 is connected with the inlet of a filtering machine; the filter 22 filters the liquid discharged from the desulfurization and calcium fixation reactor 21, the filtrate of the filter 22 enters an evaporative crystallization system or a sewage treatment system, and the filtered concentrated phase liquid returns to the fly ash washing process section, namely returns to the desulfurization and calcium fixation reactor 21 for desulfurization and calcium fixation to remove solids. The filter 22 is selected from one of a precision filter, a horizontal screw centrifuge, a disk centrifuge, and a filter press.
Further optionally, the drying unit includes a conveyor belt, a dryer, and a dry fly ash bin, an outlet of the conveyor belt is connected to an inlet of the dryer, an outlet of the dryer is connected to an inlet of the dry fly ash bin, and an outlet of the dry fly ash bin is connected to the kiln calcining unit.
The above description is only a preferred embodiment of the application and is illustrative of the principles of the technology employed. It will be appreciated by those skilled in the art that the scope of the invention herein disclosed is not limited to the particular combination of features described above, but also encompasses other arrangements formed by any combination of the above features or their equivalents without departing from the inventive concept. For example, the above features may be replaced with (but not limited to) features having similar functions disclosed in the present application.
Claims (5)
1. A fly ash washing and resource comprehensive utilization system is characterized by comprising: the system comprises a fly ash bin, a fly ash calcium and heavy metal cooperative solidification unit, a step backwashing dechlorination unit, a filtrate pressure desulphurization unit, a drying unit, an evaporation salt production unit and a cement kiln unit;
the fly ash calcium and heavy metal cooperative solidification unit is provided with a filter-pressing residue outlet and a filter-pressing liquid outlet, the filter-pressing residue outlet is connected with an inlet of the step backwashing dechlorination unit, and the filter-pressing liquid outlet is connected with an inlet of the filter-pressing liquid sulfur removal unit; an eluent outlet of the step backwashing dechlorination unit is connected with an inlet of the fly ash calcium and heavy metal cooperative solidification unit, and a washing slag outlet of the backwashing dechlorination unit is connected with an inlet of the drying unit; the liquid outlet of the pressure filtrate sulfur removal unit is connected with the inlet of the evaporation salt production unit, and the sulfur removal slag outlet of the eluent of the pressure filtrate sulfur removal unit is connected with the inlet of the fly ash calcium and heavy metal cooperative solidification unit; condensed water generated by the evaporation salt-making unit returns to the step backwashing dechlorination unit for recycling; and the outlet of the slag washing and drying unit is connected with the inlet of the cement kiln.
2. The system of claim 1, wherein the fly ash calcium and heavy metal cooperative solidification unit comprises a high-efficiency premixer, a calcium and heavy metal solidification reaction kettle, a curing agent bin, a filter press and an ammonia absorption tower;
the inlet of the high-efficiency premixer is respectively connected with the outlet of the fly ash metering device, the outlet of the water distribution metering device, the outlet of the curing agent bin and the desulphurizing slag outlet of the pressure filtrate desulphurizing unit, the outlet of the high-efficiency premixer is connected with the inlet of the calcium and heavy metal solidification reaction kettle, the material outlet of the calcium and heavy metal solidification reaction kettle is connected with the inlet of a pressure filter, the pressure filtrate outlet of the pressure filter is connected with the inlet of the eluent desulphurizing unit, the pressure filter residue outlet is connected with the inlet of the step backwashing dechlorinating unit, and the gas outlet of the calcium and heavy metal solidification reaction kettle is connected with the inlet of an ammonia.
3. The system as claimed in claim 2, wherein the step backwashing dechlorination unit comprises a high-efficiency rinsing bath and a backwashing filter press or a belt filter, an inlet of the high-efficiency rinsing bath is connected with a filter pressing residue outlet of the fly ash and calcium solidification unit, an outlet of the high-efficiency rinsing bath is connected with an inlet of the backwashing filter press or the belt filter, a backwashing liquid and a filtrate of the backwashing filter press or the belt filter are connected with an inlet of a water distribution metering device of the fly ash calcium and heavy metal cooperative solidification unit, and a filtered residue of the backwashing filter press or the belt filter is connected with an inlet of the drying unit.
4. The system of claim 2, wherein the eluent desulfurization unit comprises a sulfur fixation reaction kettle, a solid-liquid separation concentration device, a desulfurization agent bin and an acid storage tank, wherein an inlet of the sulfur fixation reaction kettle is respectively connected with an outlet of a filtrate pressed by a fly ash calcium and heavy metal cooperative curing unit filter press, an outlet of an acid preparation metering device and an outlet of the desulfurization agent bin, an outlet of the sulfur fixation reaction kettle is connected with an inlet of the solid-liquid separation concentration device, an outlet of a filtrate of a third filter press or a precision filter is connected with an inlet of an evaporation salt making unit, and filter residue or concentrated phase of the third filter press or the precision filter is connected with an inlet of a high-efficiency premixer.
5. The system according to claim 3, wherein the drying unit comprises a conveyor belt, a dryer and a dry fly ash silo, wherein an outlet of the conveyor belt is connected with an inlet of the dryer, an outlet of the dryer is connected with an inlet of the dry fly ash silo, and an outlet of the dry fly ash silo is connected with the kiln-entering calcination unit.
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| CN114538473A (en) * | 2022-01-26 | 2022-05-27 | 陈坚栋 | Incineration fly ash treatment method and device |
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