CN112479233A - Deep impurity removal and purification system and method for waste incineration fly ash washing liquid - Google Patents
Deep impurity removal and purification system and method for waste incineration fly ash washing liquid Download PDFInfo
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- CN112479233A CN112479233A CN202011512221.9A CN202011512221A CN112479233A CN 112479233 A CN112479233 A CN 112479233A CN 202011512221 A CN202011512221 A CN 202011512221A CN 112479233 A CN112479233 A CN 112479233A
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- water washing
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- 238000005406 washing Methods 0.000 title claims abstract description 163
- 239000010881 fly ash Substances 0.000 title claims abstract description 162
- 239000007788 liquid Substances 0.000 title claims abstract description 150
- 238000004056 waste incineration Methods 0.000 title claims abstract description 33
- 239000012535 impurity Substances 0.000 title claims abstract description 30
- 238000000746 purification Methods 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 124
- 238000001704 evaporation Methods 0.000 claims abstract description 62
- 230000008020 evaporation Effects 0.000 claims abstract description 62
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 45
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000011575 calcium Substances 0.000 claims abstract description 35
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 31
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 31
- 239000011777 magnesium Substances 0.000 claims abstract description 31
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 31
- 238000004062 sedimentation Methods 0.000 claims abstract description 31
- -1 fluorine ions Chemical class 0.000 claims abstract description 28
- 238000002425 crystallisation Methods 0.000 claims abstract description 26
- 230000008025 crystallization Effects 0.000 claims abstract description 26
- 150000002500 ions Chemical class 0.000 claims abstract description 20
- 230000007246 mechanism Effects 0.000 claims abstract description 13
- 229910002651 NO3 Inorganic materials 0.000 claims abstract description 10
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims abstract description 9
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 9
- 239000002957 persistent organic pollutant Substances 0.000 claims abstract description 9
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910001425 magnesium ion Inorganic materials 0.000 claims abstract description 7
- 238000010979 pH adjustment Methods 0.000 claims abstract description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 32
- 239000010802 sludge Substances 0.000 claims description 32
- 239000012452 mother liquor Substances 0.000 claims description 31
- 239000000835 fiber Substances 0.000 claims description 30
- 238000006115 defluorination reaction Methods 0.000 claims description 24
- 238000001914 filtration Methods 0.000 claims description 23
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 22
- 150000003839 salts Chemical class 0.000 claims description 17
- 229960002089 ferrous chloride Drugs 0.000 claims description 12
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 claims description 12
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 12
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 11
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 11
- 238000005273 aeration Methods 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 8
- 239000000706 filtrate Substances 0.000 claims description 8
- 239000012528 membrane Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 6
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 claims description 6
- 238000011001 backwashing Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 238000001556 precipitation Methods 0.000 claims description 4
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 claims description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 3
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims description 3
- 239000001095 magnesium carbonate Substances 0.000 claims description 3
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 238000003825 pressing Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 2
- 230000029219 regulation of pH Effects 0.000 claims description 2
- 229910052731 fluorine Inorganic materials 0.000 abstract description 5
- 239000011737 fluorine Substances 0.000 abstract description 5
- 238000006555 catalytic reaction Methods 0.000 abstract description 4
- 239000000428 dust Substances 0.000 abstract description 3
- 238000005260 corrosion Methods 0.000 abstract description 2
- 230000007797 corrosion Effects 0.000 abstract description 2
- 230000008569 process Effects 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000006004 Quartz sand Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- 229910052801 chlorine Inorganic materials 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000012982 microporous membrane Substances 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000010882 bottom ash Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 150000001804 chlorine Chemical class 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229940056932 lead sulfide Drugs 0.000 description 1
- 229910052981 lead sulfide Inorganic materials 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 239000002455 scale inhibitor Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- PVGBHEUCHKGFQP-UHFFFAOYSA-N sodium;n-[5-amino-2-(4-aminophenyl)sulfonylphenyl]sulfonylacetamide Chemical compound [Na+].CC(=O)NS(=O)(=O)C1=CC(N)=CC=C1S(=O)(=O)C1=CC=C(N)C=C1 PVGBHEUCHKGFQP-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/22—Preparation in the form of granules, pieces, or other shaped products
- C01D3/24—Influencing the crystallisation process
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention discloses a deep impurity removal and purification system for waste incineration fly ash washing liquid, which comprises a fly ash washing liquid collecting tank and a heavy metal removal reaction sedimentation tank which are sequentially connected; calcium and magnesium removal mechanism, PH adjustment back pond, evaporation crystallization system, electro-catalysis water processor connects flying dust washing system. Meanwhile, discloses a method for deeply removing impurities and purifying waste incineration fly ash washing liquid. The deep impurity removal and purification system and method for the waste incineration fly ash water washing liquid can effectively perform deep impurity removal and purification on the waste incineration fly ash water washing liquid, can effectively remove heavy metal ions, calcium and magnesium ions and suspended matters in the waste incineration fly ash water washing liquid, and can also remove other impurity ions such as fluorine ions, sulfate ions, ammonium ions, nitrate ions, organic pollutants TOC and the like, thereby avoiding the corrosion influence of the impurity ions on an evaporation crystallization system and ensuring the working efficiency of the evaporation crystallization system.
Description
Technical Field
The invention belongs to the technical field of water treatment, and particularly relates to a deep impurity removal and purification system and method for waste incineration fly ash washing liquid.
Background
The flue gas purification system of the household garbage incineration facility captures matters and bottom ash settled at the bottom of a flue and a chimney, which is called fly ash for short, mainly contains heavy metals, dioxins, chlorine salt and by-products generated in the flue gas denitration and denitration process, such as calcium oxide, calcium sulfate, nitrate, urea or ammonia and other pollutants.
According to the technical Specification for controlling pollution of fly ash from incineration of household garbage HJ1134-2020, when the fly ash from incineration of garbage is disposed by cooperation of a cement kiln, the soluble chlorine content in the fly ash is washed away by a water washing process, so that the soluble chlorine content in the fly ash is reduced to be within 1%; for the treatment of the fly ash washing liquid, the patent discloses measures mainly including evaporation crystallization after pretreatment, wherein the pretreatment process mainly comprises calcium and magnesium removal, heavy metal removal, suspended matter removal of a quartz sand filter and flocculating agent removal of an activated carbon filter; and (4) feeding the pretreated water washing liquid into an evaporation system, and crystallizing to produce salt. These pretreatment measures only treat heavy metals and calcium and magnesium in the fly ash washing liquid, but not treat other dissolved ions, such as fluoride ions, sulfate ions, ammonium ions, nitrate ions and organic pollutants TOC, and the existence of these impurity ions mainly causes the following problems: 1) the concentration of fluorine ions in the evaporation mother liquor is accumulated continuously, and an evaporator body and a pipeline are corroded; 2) organic pollutants, suspended solids and the like in the mother liquor influence the evaporation and crystallization process, the evaporation and concentration efficiency is reduced, and the discharge amount of the mother liquor is increased; 3) the existence of sulfate, nitrate, ammonium salt and the like influences the evaporation salt separation process, reduces the salt purity, and causes that the sodium salt purity can not reach the superior standard index of the industrial salt GB/T5462-2015 and the potassium salt purity can not reach the superior standard index of the potassium chloride GB 6549-2011.
In summary, the treatment process for the fly ash washing liquid disclosed in the prior patent only treats heavy metal ions, calcium and magnesium ions and suspended matters in the fly ash washing liquid, and generally does not treat other impurity ions, such as fluoride ions, sulfate ions, ammonium ions, nitrate ions, organic pollutants TOC and the like, so that the problems that the discharge amount of mother liquid is large due to the reduction of the efficiency of an evaporation system, the service life of equipment is seriously reduced, the salt purity is reduced and the quality of industrial salt cannot be achieved due to the unsatisfactory salt separation effect and the like occur in the actual project operation, and finally the project operation cost is increased, which becomes a technical problem to be solved urgently by technical personnel in the field.
Disclosure of Invention
The invention aims to solve the problem that evaporation desalination is influenced because the existing treatment process of the fly ash washing liquid only treats heavy metal ions, calcium and magnesium ions and suspended matters in the fly ash washing liquid and does not treat other impurity ions such as fluoride ions, sulfate ions, ammonium ions, nitrate ions, organic pollutant TOC and the like.
In order to solve the technical problems, the invention adopts the technical scheme that: the utility model provides a waste incineration fly ash washing liquid degree of depth edulcoration clean system, including connecting gradually the setting:
the fly ash water washing liquid collecting tank is used for collecting fly ash water washing liquid generated by the fly ash water washing system;
a heavy metal removal reaction sedimentation tank for removing heavy metal ions in the fly ash water washing liquid;
a calcium and magnesium removing mechanism for removing calcium ions and magnesium ions in the fly ash water washing liquid;
a PH adjusting tank for adjusting the PH value of the fly ash washing liquid;
an evaporative crystallization system;
an electro-catalytic water processor for processing the evaporation mother liquor generated by the evaporation crystallization system,
the electro-catalytic water processor is connected with the fly ash washing system.
Preferably, an aeration stirring device is arranged in the fly ash washing liquid collecting tank.
Preferably, the device further comprises a sludge dewatering machine, the sludge dewatering machine is used for dewatering sludge generated by precipitation in the heavy metal removal reaction sedimentation tank, the sludge dewatering machine comprises a filtrate outlet, and the filtrate outlet is connected with the fly ash water washing liquid collecting tank through a pipeline.
Preferably, in the above-described aspect, an automatic pH adjusting mechanism for adjusting pH by using concentrated hydrochloric acid and a sodium sulfide dosing tank for adding sodium sulfide to the heavy metal removal reaction sedimentation tank are installed near the heavy metal removal reaction sedimentation tank.
Preferably, the calcium and magnesium removing mechanism comprises a calcium and magnesium removing reaction tank, a membrane filter press and a fiber filtering device which are sequentially connected, a sodium carbonate dosing tank for adding sodium carbonate to the calcium and magnesium removing reaction tank and a ferrous chloride dosing tank for adding ferrous chloride to the calcium and magnesium removing reaction tank are arranged beside the calcium and magnesium removing reaction tank, the heavy metal removing reaction sedimentation tank is connected with the calcium and magnesium removing reaction tank, and the fiber filtering device is connected with a PH (potential of hydrogen) adjusting tank.
Preferably, the fiber filtering device is a fiber filter or a fiber filter, the fiber filter or the fiber filter comprises a backwash water outlet, and the backwash water outlet is connected with the fly ash washing liquid collecting tank through a pipeline.
Preferably, a hydrochloric acid dosing tank for adding hydrochloric acid to the PH adjustment tank is arranged beside the PH adjustment tank.
Preferably, an evaporation mother liquor storage tank and a defluorination tank are sequentially arranged between the evaporation crystallization system and the electro-catalytic water treatment machine, the evaporation mother liquor storage tank is connected with the evaporation crystallization system, the defluorination tank is connected with the electro-catalytic water treatment machine, and a fluoride ion remover dosing box for adding fly ash washing liquid generated by the fly ash washing system into the defluorination tank is arranged beside the defluorination tank.
A deep impurity removal and purification method for waste incineration fly ash water washing liquid is provided, and the deep impurity removal and purification system for the waste incineration fly ash water washing liquid comprises the following steps:
1) discharging the fly ash water washing liquid generated by the fly ash water washing system into a fly ash water washing liquid collecting tank, and carrying out aeration stirring on the fly ash water washing liquid in the fly ash water washing liquid collecting tank by using an aeration stirring device;
2) the fly ash water washing liquid in the fly ash water washing liquid collecting pool enters a heavy metal removal reaction sedimentation pool, an automatic pH adjusting mechanism utilizes concentrated hydrochloric acid to adjust the pH of the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool, so that the pH of the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool is between 9.2 and 9.4, a sodium sulfide dosing box is utilized to add sodium sulfide to the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool, heavy metal ions in the fly ash water washing liquid are precipitated to form sludge, a sludge dewatering machine is utilized to dewater the sludge, liquid generated at a filtrate outlet of the sludge dewatering machine flows into the fly ash water washing liquid collecting pool, and the dewatered sludge is used as dangerous waste sludge for additional treatment;
3) the fly ash water washing liquid treated by the heavy metal removal reaction sedimentation tank enters a calcium and magnesium removal reaction tank, sodium carbonate is added into the calcium and magnesium removal reaction tank by using a sodium carbonate dosing tank, and ferrous chloride is added into the calcium and magnesium removal reaction tank by using a ferrous chloride dosing tank, so that the fly ash water washing liquid is subjected to chemical reaction to form a solid-liquid mixture containing calcium carbonate solid, magnesium carbonate solid and ferrous sulfide, the solid-liquid mixture enters a membrane filter press for filter pressing, a mud cake is separated, the fly ash water washing liquid enters a fiber filtering device for filtering and then is discharged into a PH (potential of hydrogen) callback tank, and the mud cake is conveyed to a fly ash water washing system for washing;
4) adding hydrochloric acid into the PH regulation tank by using a hydrochloric acid dosing tank to regulate the PH value of the fly ash water washing liquid and remove carbonate ions remained in the fly ash water washing liquid;
5) removing salt in the fly ash water washing liquid by using an evaporative crystallization system, and discharging the generated evaporation mother liquid into an evaporation mother liquid storage tank for storage and collection;
6) discharging the evaporation mother liquor in the evaporation mother liquor storage tank into a defluorination pool, filling part of fly ash washing liquor generated by a fly ash washing system into a fluoride ion remover dosing tank as a defluorination agent, and adding a certain amount of defluorination agent into the defluorination pool to remove fluoride ions and sulfate ions in the evaporation mother liquor;
7) treating the evaporation mother liquor by using an electro-catalytic water treatment machine, oxidizing an anode plate of the electro-catalytic water treatment machine to remove organic pollutants TOC and ammonia nitrogen in the evaporation mother liquor, and removing nitrate ions in the evaporation mother liquor by using a cathode plate;
8) and the evaporation mother liquor treated by the electro-catalytic water treatment machine is added into the fly ash washing system for washing the waste incineration fly ash to be used for washing the waste incineration fly ash.
Preferably, in the step 3), the fiber filtering device periodically performs backwashing operation, and the formed backwashing liquid is discharged into the fly ash washing liquid collecting tank.
The invention has the beneficial effects that: the deep impurity removal and purification system and method for the waste incineration fly ash water washing liquid can effectively perform deep impurity removal and purification on the waste incineration fly ash water washing liquid, can effectively remove heavy metal ions, calcium and magnesium ions and suspended matters in the waste incineration fly ash water washing liquid, and can also remove other impurity ions such as fluorine ions, sulfate ions, ammonium ions, nitrate ions, organic pollutants TOC and the like, thereby avoiding the corrosion influence of the impurity ions on an evaporation crystallization system and ensuring the working efficiency of the evaporation crystallization system.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in figure 1, a deep impurity removal and purification system for waste incineration fly ash washing liquid comprises:
a fly ash washing liquid collecting tank for collecting fly ash washing liquid generated by the fly ash washing system, wherein an aeration stirring device is arranged in the fly ash washing liquid collecting tank;
a heavy metal removing reaction sedimentation tank for removing heavy metal ions in the fly ash water washing liquid. An automatic pH adjusting mechanism and a sodium sulfide dosing tank are arranged beside the heavy metal removal reaction sedimentation tank. Sludge generated by precipitation in the heavy metal removal reaction sedimentation tank is dewatered by a sludge dewatering machine, and filtrate generated by the sludge dewatering machine returns to the fly ash water washing liquid collecting tank;
the calcium and magnesium removing mechanism is used for removing calcium ions and magnesium ions in fly ash water washing liquid and comprises a calcium and magnesium removing reaction tank, a membrane filter press and a fiber filtering device which are sequentially connected, a sodium carbonate dosing tank and a ferrous chloride dosing tank are arranged beside the calcium and magnesium removing reaction tank, the heavy metal removing reaction sedimentation tank is connected with the calcium and magnesium removing reaction tank, and the fiber filtering device is connected with a PH (potential of hydrogen) adjusting tank. The fiber filtering device is a fiber filter, the fiber filter comprises a back-flushing water outlet, and the back-flushing water outlet is connected with the fly ash washing liquid collecting tank through a pipeline;
a PH adjusting tank for adjusting the PH value of the fly ash washing liquid, wherein a hydrochloric acid dosing tank is arranged beside the PH adjusting tank;
an evaporative crystallization system;
a electro-catalysis water processor for handling evaporation mother liquor that evaporation crystal system produced, be equipped with evaporation mother liquor storage tank and defluorination pond between evaporation crystal system and the electro-catalysis water processor in proper order, evaporation mother liquor storage tank connection evaporation crystal system, defluorination pond connection electro-catalysis water processor, the other fluoride ion remover dosing tank that is arranged in adding the flying dust washing liquid that flying dust washing system produced to the defluorination pond that is equipped with of defluorination pond.
The electro-catalytic water processor is connected with the fly ash washing system.
The waste incineration fly ash water washing liquid deep impurity removal and purification system is used for treating waste incineration fly ash water washing liquid, and the specific process comprises the following steps:
1) and discharging the fly ash water washing liquid generated by the fly ash water washing system into the fly ash water washing liquid collecting tank, and carrying out aeration stirring on the fly ash water washing liquid in the fly ash water washing liquid collecting tank by utilizing an aeration stirring device. The capacity of the fly ash washing liquid collecting tank is preferably set to be capable of accommodating fly ash washing liquid which can be generated when the fly ash washing system operates for one day.
2) The fly ash water washing liquid in the fly ash water washing liquid collecting pool enters the heavy metal removal reaction sedimentation pool, the pH automatic regulating mechanism utilizes concentrated hydrochloric acid to regulate the pH of the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool, the fly ash water washing liquid with the pH of 11-12.4 originally in the heavy metal removal reaction sedimentation pool is regulated to the pH of 9.2-9.4, sodium sulfide is added into the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool by utilizing a sodium sulfide dosing box, heavy metal ions in the fly ash water washing liquid are precipitated to form sludge, the sludge is dewatered by utilizing a sludge dewatering machine, the liquid generated at a filtrate outlet of the sludge dewatering machine flows into the fly ash water washing liquid collecting pool, and the dewatered sludge is used as dangerous waste sludge for additional treatment. Sodium sulfide is used as a heavy metal capturing agent to capture heavy metal ions in the fly ash water washing liquid, and the sulfur ions and lead ions can form lead sulfide precipitate which is extremely insoluble in water. According to the invention, an organic re-catching agent is not adopted, because the organic re-catching agent can cause organic matter risks, the addition of the organic matter can cause the problems of reduced salt purity, high medicament adding cost and the like in the salt separation process of a subsequent evaporative crystallization system.
3) And the fly ash water washing liquid treated by the heavy metal removal reaction sedimentation tank enters a calcium and magnesium removal reaction tank, sodium carbonate is added into the calcium and magnesium removal reaction tank by using a sodium carbonate dosing tank, and ferrous chloride is added into the calcium and magnesium removal reaction tank by using a ferrous chloride dosing tank, so that the fly ash water washing liquid is subjected to chemical reaction to form a solid-liquid mixture containing calcium carbonate solid, magnesium carbonate solid and ferrous sulfide, the solid-liquid mixture enters a membrane filter press to be subjected to filter pressing, a mud cake is separated, and the fly ash water washing liquid enters a fiber filtering device again to be filtered and then is discharged into a PH callback tank. And (5) conveying the mud cakes to a fly ash washing system for washing. In order to reduce unnecessary drug addition, the invention only arranges a calcium and magnesium removal reaction tank for chemical reaction, does not arrange a flocculation unit and a precipitation unit, and adopts a membrane filter press to directly filter and separate sludge to prepare mud cakes. The method has the advantages that: 1. the method has the advantages that a flocculation sedimentation tank is not arranged, solid-liquid separation is directly carried out by a dehydrator, the risk of introducing organic matters caused by adding a polymeric flocculant is reduced, and the problems of reduced purity of salt generated in the salt separation process of a subsequent evaporative crystallization system, high medicament adding cost and the like are caused; 2. the diaphragm filter press is used for further reducing the moisture in the sludge, the sludge cake is washed by a fly ash washing system and added into the finished fly ash, and the reduction of the moisture content can reduce the chlorine ions entering the finished fly ash. The ferrous chloride is added to remove sulfur ions which are excessively added in the previous step, so that the influence of the sulfur ions on the evaporation crystallization salt separation process on the salt purity is avoided. And adopt the fiber filtration to replace traditional quartz sand filter, medium filter, tubular microporous membrane filter, ultrafiltration etc. in this application because the filterable filter fineness of fiber reaches 1 micron, can satisfy the requirement of evaporative crystallization system to the suspended solid of intaking. Compared with medium filtration or quartz sand filtration, the fiber filtration has higher filtration precision; compared with tubular microporous membrane filtration or ultrafiltration, the water yield is as high as 99% (minus 1% of backwashing water consumption rate), while the water yield of ultrafiltration or microfiltration is only about 90%, in addition, the operation cost of fiber filtration is low, no scale inhibitor needs to be added, and gravity flow filtration can be adopted without a lift pump.
4) Adding hydrochloric acid into a PH readjustment tank by using a hydrochloric acid dosing tank to adjust the PH value of the fly ash water washing liquid, wherein the PH value of the fly ash water washing liquid in the PH readjustment tank is controlled to be between 7 and 8, so that residual carbonate ions in the fly ash water washing liquid are removed, and the influence of enrichment of carbonate in an evaporative crystallization system on the purity of salt is prevented; meanwhile, the alkalinity of the waste water is reduced to be below 100mg/L, and the requirement of an evaporator on the alkalinity of inlet water is met.
5) And removing salt in the fly ash water washing liquid by using an evaporation crystallization system, and discharging the generated evaporation mother liquid into an evaporation mother liquid storage tank for storage and collection.
6) And the evaporation mother liquor in the evaporation mother liquor storage tank is discharged into a defluorination pool, part of the fly ash washing liquor generated by the fly ash washing system is filled into a fluoride ion remover dosing tank to be used as a defluorination agent, and a certain amount of the defluorination agent is added into the defluorination pool to remove fluoride ions and sulfate ions in the evaporation mother liquor. The untreated fly ash water washing liquid contains a certain amount of calcium ions, and the calcium ions in the untreated fly ash water washing liquid are utilized to remove fluorine ions and sulfate radicals in the evaporation mother liquid, so that the fluorine ions and the sulfate radicals are prevented from being accumulated in the mother liquid, and meanwhile, new substances are prevented from being introduced into the treated fly ash water washing liquid (the evaporation mother liquid).
7) Treating the evaporation mother liquor by using an electro-catalytic water treatment machine, oxidizing an anode plate of the electro-catalytic water treatment machine to remove organic pollutants TOC and ammonia nitrogen in the evaporation mother liquor, and removing nitrate ions in the evaporation mother liquor by using a cathode plate;
8) and the evaporation mother liquor treated by the electro-catalytic water treatment machine is added into the fly ash washing system for washing the waste incineration fly ash to be used for washing the waste incineration fly ash.
Further, the fiber filtering device in the step 3) performs backwashing operation periodically, and formed backwash liquid is discharged into the fly ash washing liquid collecting tank.
It should be noted that the technical features of the fly ash washing system, the evaporative crystallization system, the electro-catalytic water treatment machine, the fiber filter, the pH automatic adjustment mechanism, the membrane filter press, and various dosing boxes according to the present invention application are regarded as the prior art, and the specific structure, the operation principle, the control mode and the spatial arrangement mode of the technical features may be selected conventionally in the field, and should not be regarded as the invention point of the present invention patent, and the present invention patent is not further specifically described.
Having described preferred embodiments of the present invention in detail, it is to be understood that modifications and variations may be resorted to without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. The utility model provides a waste incineration fly ash washing liquid degree of depth edulcoration clean system which characterized in that, including connecting gradually the setting:
the fly ash water washing liquid collecting tank is used for collecting fly ash water washing liquid generated by the fly ash water washing system;
a heavy metal removal reaction sedimentation tank for removing heavy metal ions in the fly ash water washing liquid;
a calcium and magnesium removing mechanism for removing calcium ions and magnesium ions in the fly ash water washing liquid;
a PH adjusting tank for adjusting the PH value of the fly ash washing liquid;
an evaporative crystallization system;
an electro-catalytic water processor for processing the evaporation mother liquor generated by the evaporation crystallization system,
the electro-catalytic water processor is connected with a fly ash washing system or an evaporative crystallization system or a fly ash washing liquid collecting tank.
2. The deep impurity removal and purification system for fly ash washing liquid generated in waste incineration of claim 1, wherein an aeration stirring device is arranged in the fly ash washing liquid collecting tank.
3. The deep impurity removal and purification system for waste incineration fly ash washing liquid according to claim 2, further comprising a sludge dewatering machine, wherein the sludge dewatering machine is used for dewatering sludge generated by precipitation in the heavy metal removal reaction sedimentation tank, the sludge dewatering machine comprises a filtrate outlet, and the filtrate outlet is connected with the fly ash washing liquid collection tank through a pipeline.
4. The deep impurity removal and purification system for waste incineration fly ash washing liquid according to claim 3, wherein an automatic pH adjustment mechanism for adjusting the pH by using concentrated hydrochloric acid and a sodium sulfide dosing tank for adding sodium sulfide to the heavy metal removal reaction sedimentation tank are installed beside the heavy metal removal reaction sedimentation tank.
5. The deep impurity removal and purification system for waste incineration fly ash washing liquid according to claim 4, wherein the calcium and magnesium removal mechanism comprises a calcium and magnesium removal reaction tank, a membrane filter press and a fiber filtering device which are sequentially connected, a sodium carbonate dosing tank for adding sodium carbonate to the calcium and magnesium removal reaction tank and a ferrous chloride dosing tank for adding ferrous chloride to the calcium and magnesium removal reaction tank are arranged beside the calcium and magnesium removal reaction tank, the heavy metal removal reaction sedimentation tank is connected with the calcium and magnesium removal reaction tank, and the fiber filtering device is connected with the PH adjustment tank.
6. The deep impurity removal and purification system for the waste incineration fly ash washing liquid as claimed in claim 5, wherein the fiber filtering device is a fiber filter or a fiber filter, the fiber filter or the fiber filter comprises a back flush water outlet, and the back flush water outlet is connected with the fly ash washing liquid collecting tank through a pipeline.
7. The deep impurity removal and purification system for waste incineration fly ash washing liquid according to claim 6, wherein a hydrochloric acid dosing tank for adding hydrochloric acid to the PH adjustment tank is arranged beside the PH adjustment tank.
8. The deep impurity removal and purification system for the waste incineration fly ash washing liquid as claimed in claim 7, wherein an evaporation mother liquid storage tank and a defluorination tank are sequentially arranged between the evaporation crystallization system and the electro-catalytic water treatment machine, the evaporation mother liquid storage tank is connected with the evaporation crystallization system, the defluorination tank is connected with the electro-catalytic water treatment machine, and a fluoride ion remover dosing box for adding the fly ash washing liquid generated by the fly ash washing system into the defluorination tank is arranged beside the defluorination tank.
9. A method for deeply removing impurities and purifying waste incineration fly ash water washing liquid, which is characterized by using the system for deeply removing impurities and purifying waste incineration fly ash water washing liquid as defined in claim 8, and comprising the following steps:
1) discharging the fly ash water washing liquid generated by the fly ash water washing system into a fly ash water washing liquid collecting tank, and carrying out aeration stirring on the fly ash water washing liquid in the fly ash water washing liquid collecting tank by using an aeration stirring device;
2) the fly ash water washing liquid in the fly ash water washing liquid collecting pool enters a heavy metal removal reaction sedimentation pool, an automatic pH adjusting mechanism utilizes concentrated hydrochloric acid to adjust the pH of the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool, so that the pH of the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool is between 9.2 and 9.4, a sodium sulfide dosing box is utilized to add sodium sulfide to the fly ash water washing liquid in the heavy metal removal reaction sedimentation pool, heavy metal ions in the fly ash water washing liquid are precipitated to form sludge, a sludge dewatering machine is utilized to dewater the sludge, liquid generated at a filtrate outlet of the sludge dewatering machine flows into the fly ash water washing liquid collecting pool, and the dewatered sludge is used as dangerous waste sludge for additional treatment;
3) the fly ash water washing liquid treated by the heavy metal removal reaction sedimentation tank enters a calcium and magnesium removal reaction tank, sodium carbonate is added into the calcium and magnesium removal reaction tank by using a sodium carbonate dosing tank, and ferrous chloride is added into the calcium and magnesium removal reaction tank by using a ferrous chloride dosing tank, so that the fly ash water washing liquid is subjected to chemical reaction to form a solid-liquid mixture containing calcium carbonate solid, magnesium carbonate solid and ferrous sulfide, the solid-liquid mixture enters a membrane filter press for filter pressing, a mud cake is separated, the fly ash water washing liquid enters a fiber filtering device for filtering and then is discharged into a PH (potential of hydrogen) callback tank, and the mud cake is conveyed to a fly ash water washing system for washing;
4) adding hydrochloric acid into the PH regulation tank by using a hydrochloric acid dosing tank to regulate the PH value of the fly ash water washing liquid and remove carbonate ions remained in the fly ash water washing liquid;
5) removing salt in the fly ash water washing liquid by using an evaporative crystallization system, and discharging the generated evaporation mother liquid into an evaporation mother liquid storage tank for storage and collection;
6) discharging the evaporation mother liquor in the evaporation mother liquor storage tank into a defluorination pool, filling part of fly ash washing liquor generated by a fly ash washing system into a fluoride ion remover dosing tank as a defluorination agent, and adding a certain amount of defluorination agent into the defluorination pool to remove fluoride ions and sulfate ions in the evaporation mother liquor;
7) treating the evaporation mother liquor by using an electro-catalytic water treatment machine, oxidizing an anode plate of the electro-catalytic water treatment machine to remove organic pollutants TOC and ammonia nitrogen in the evaporation mother liquor, and removing nitrate ions in the evaporation mother liquor by using a cathode plate;
8) and the evaporation mother liquor treated by the electro-catalytic water treatment machine is added into the fly ash washing system for washing the waste incineration fly ash to be used for washing the waste incineration fly ash.
10. The method for deeply removing impurities and purifying the fly ash washing liquid generated by incinerating the garbage according to claim 9, wherein the fiber filtering device in 3) is periodically subjected to back washing operation, and the formed back washing liquid is discharged into the fly ash washing liquid collecting tank.
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