CN113245342B - Resource treatment method and treatment system for waste incineration fly ash water washing salt making based on seed crystal method - Google Patents
Resource treatment method and treatment system for waste incineration fly ash water washing salt making based on seed crystal method Download PDFInfo
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- 239000010881 fly ash Substances 0.000 title claims abstract description 223
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 211
- 229910001868 water Inorganic materials 0.000 title claims abstract description 211
- 238000005406 washing Methods 0.000 title claims abstract description 139
- 239000013078 crystal Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 63
- 150000003839 salts Chemical class 0.000 title claims abstract description 56
- 238000004056 waste incineration Methods 0.000 title claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 192
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 145
- 239000010440 gypsum Substances 0.000 claims abstract description 145
- 238000001704 evaporation Methods 0.000 claims abstract description 121
- 230000008020 evaporation Effects 0.000 claims abstract description 115
- 238000002425 crystallisation Methods 0.000 claims abstract description 113
- 230000008025 crystallization Effects 0.000 claims abstract description 113
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims abstract description 100
- 238000010828 elution Methods 0.000 claims abstract description 97
- 239000002002 slurry Substances 0.000 claims abstract description 91
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 80
- 238000000926 separation method Methods 0.000 claims abstract description 59
- 235000011164 potassium chloride Nutrition 0.000 claims abstract description 50
- 239000001103 potassium chloride Substances 0.000 claims abstract description 50
- 239000011780 sodium chloride Substances 0.000 claims abstract description 40
- 238000000746 purification Methods 0.000 claims abstract description 33
- 239000002994 raw material Substances 0.000 claims abstract description 26
- 238000004064 recycling Methods 0.000 claims abstract description 18
- 239000007791 liquid phase Substances 0.000 claims description 100
- 238000004537 pulping Methods 0.000 claims description 69
- 239000012452 mother liquor Substances 0.000 claims description 55
- 239000007790 solid phase Substances 0.000 claims description 53
- 229910001385 heavy metal Inorganic materials 0.000 claims description 43
- 238000001556 precipitation Methods 0.000 claims description 35
- 239000000047 product Substances 0.000 claims description 33
- 239000010802 sludge Substances 0.000 claims description 33
- 238000001914 filtration Methods 0.000 claims description 32
- 238000001035 drying Methods 0.000 claims description 31
- 239000006228 supernatant Substances 0.000 claims description 22
- 239000002245 particle Substances 0.000 claims description 15
- 238000005189 flocculation Methods 0.000 claims description 13
- 230000016615 flocculation Effects 0.000 claims description 13
- 239000007787 solid Substances 0.000 claims description 13
- 239000000243 solution Substances 0.000 claims description 13
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 239000003480 eluent Substances 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 6
- 239000013505 freshwater Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 239000012266 salt solution Substances 0.000 claims description 6
- 239000000706 filtrate Substances 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 239000003153 chemical reaction reagent Substances 0.000 claims description 3
- 239000012528 membrane Substances 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 230000001376 precipitating effect Effects 0.000 claims description 2
- 238000010979 pH adjustment Methods 0.000 claims 1
- 239000011575 calcium Substances 0.000 abstract description 8
- 229910001424 calcium ion Inorganic materials 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 3
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 abstract description 3
- 229910001425 magnesium ion Inorganic materials 0.000 abstract description 3
- 239000002956 ash Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 239000004568 cement Substances 0.000 description 5
- 238000002386 leaching Methods 0.000 description 5
- 239000010813 municipal solid waste Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000006298 dechlorination reaction Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000013049 sediment Substances 0.000 description 4
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 3
- 238000011278 co-treatment Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 description 3
- 238000012958 reprocessing Methods 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 229910052979 sodium sulfide Inorganic materials 0.000 description 3
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 3
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 description 3
- 235000019345 sodium thiosulphate Nutrition 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 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
- 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
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- 239000012267 brine Substances 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
- 230000000382 dechlorinating effect Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 241000607479 Yersinia pestis Species 0.000 description 1
- 239000012445 acidic reagent Substances 0.000 description 1
- 231100000357 carcinogen Toxicity 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000011268 retreatment Methods 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 229910052596 spinel Inorganic materials 0.000 description 1
- 239000011029 spinel Substances 0.000 description 1
- -1 sulfate radical Chemical class 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
-
- 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
-
- 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
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/468—Purification of calcium sulfates
-
- 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
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Materials Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a recycling treatment method and a treatment system for waste incineration fly ash water washing salt based on a seed crystal method. The recycling treatment method comprises the following steps: performing multistage elution on the fly ash slurry to obtain water-washed fly ash and water-washing liquid; the evaporation raw material liquid obtained by the purification treatment of the water washing liquid is sequentially subjected to preheating, evaporation concentration, evaporation crystallization, gypsum separation, sodium chloride separation and potassium chloride crystallization separation treatment, and finally gypsum, potassium chloride, sodium chloride and a dried fly ash finished product are obtained. According to the invention, the gypsum seed crystal method is introduced into the evaporation crystallization process of the washing liquid, so that the decalcification treatment link in the washing liquid purification process is omitted, the washing liquid purification cost is obviously reduced, the scaling of a heat exchanger and an evaporation crystallizer is effectively prevented, the mass transfer heat energy consumption is reduced, and the stable operation of the system is ensured. By organically combining multistage countercurrent elution, water washing liquid purification and gypsum seed crystal method evaporation crystallization, the problems of high consumption of water and calcium and magnesium ion remover, easy scaling in the evaporation crystallization process, poor quality of crystal salt and the like are solved.
Description
Technical Field
The invention relates to a treatment method and a treatment system of waste incineration fly ash, in particular to a recycling treatment method and a treatment system of waste incineration fly ash water washing salt based on a seed crystal method, belonging to the field of reprocessing and utilizing of waste incineration fly ash.
Background
Fly ash is a powder material with lighter volume weight and small particle size, which is collected at a flue gas pipeline, a flue gas purification device, a separator, a dust remover device and the like in the garbage incineration process. Fly ash is classified as a solid hazardous waste (code HW 18) because it is rich in heavy metal inorganic pests and high concentrations of dioxin organic carcinogens.
The main disposal technology of the waste incineration fly ash at present comprises the following steps: cement solidification, melt sintering solidification, chemical agent stabilization, and cement kiln co-treatment. The fly ash is subjected to landfill treatment after solidification or stabilization treatment, a large amount of land resources are occupied by the landfill treatment, landfill leachate is easy to pollute underground water and soil, and the environment is potentially threatened for a long time by the non-removed dioxin, heavy metals and salts. The cement kiln co-treatment technology is a new treatment means in the development of fly ash treatment technology, and can realize the harmless, decrement and recycling treatment of the household garbage incineration fly ash.
The fly ash must be subjected to dechlorination pretreatment before entering the kiln, otherwise, a large amount of chloride ions in the fly ash can affect the quality of clinker and cement, and the skinning in the kiln is easy to cause. The water washing pretreatment is a main method for removing chloride ions in the fly ash, and soluble substances (potassium, sodium and chloride ions) in the fly ash can be transferred into the water washing liquid. The fly ash water washing liquid contains about 6-15 wt% of potassium and sodium salt, and Chinese potassium salt resources are relatively scarce, and the potassium salt and sodium salt are prepared from the fly ash water washing liquid by an evaporation crystallization technology, so that the blank of the Chinese potassium salt is relieved.
Chinese patent (CN 108607870A) discloses a garbage fly ash treatment system and a treatment process, wherein the garbage fly ash treatment system comprises a fly ash washing system and a wastewater treatment system, and wastewater is subjected to heavy metal removal, activated carbon decontamination treatment and calcium ion removal in sequence, and finally the wastewater is utilized; the wastewater storage tank is connected with an evaporator, and the evaporator is connected with a centrifugal machine and a reaction water storage tank to realize the evaporation, crystallization and salt production of wastewater. The method can remove chloride ions in the fly ash, solves the negative influence of chloride salts on the cement kiln co-treatment process, simultaneously generates certain economic benefit, and reduces the high cost caused by imperfect fly ash treatment.
Although the prior art solves the pollution problem of fly ash, the evaporation crystallization process is simple, salt in the feed liquid is separated out into crystals in the evaporation process, and the crystals can be attached to the surface of the evaporator, so that uneven heat transfer and low heat transfer efficiency are caused, energy waste can be caused, and the production efficiency is seriously influenced because the periodic shutdown cleaning is needed.
Disclosure of Invention
The invention aims at providing a recycling treatment method for waste incineration fly ash water washing salt based on a seed crystal method;
the invention aims to provide a treatment system for realizing the garbage incineration fly ash water-washing salt-making recycling treatment method based on the seed crystal method;
the above object of the present invention is achieved by the following technical solutions:
the invention firstly provides a disposal method for recycling waste incineration fly ash water-washing salt-making based on a seed crystal method, which comprises the following steps: (1) Crushing the waste incineration fly ash, and stirring with pulping water to obtain fly ash slurry; (2) Carrying out multistage elution on the fly ash slurry by using water to obtain water-washed fly ash and water-washing liquid; (3) Purifying the water washing liquid to obtain clear liquid and precipitated slurry; adjusting the pH value of the clear solution by using an acid solution to evaporate the raw material liquid; (4) Sequentially carrying out preheating, evaporation concentration, evaporation crystallization, gypsum separation, sodium chloride separation and potassium chloride crystallization separation treatment on the evaporation raw material liquid to obtain gypsum, potassium chloride and sodium chloride products; wherein, gypsum seed crystal is added during evaporation and crystallization to lead Ca in crystallization feed liquid 2+ And SO 4 2- Condensing to form gypsum crystal precipitation on the solid gypsum crystal nucleus; (5) Desliming the precipitated slurry obtained in the step (3) to obtain sludge and clear liquid; and (3) drying the sludge and the water-washed fly ash generated in the step (2) to obtain a fly ash finished product.
As a preferred embodiment of the present invention, the crushing in the step (1) is to crush the waste incineration fly ash to particles with the particle size of less than 2 mm; wherein the mass ratio of the crushed waste incineration fly ash particles to the pulping water is preferably 1:2-1:4, and most preferably 1:3.
As a preferred embodiment of the present invention, the multi-stage elution in step (2) is preferably a three-stage elution; specifically, the fly ash slurry prepared in the step (1) enters a first-stage eluting and separating device to carry out first-stage elution to obtain first-stage washing fly ash and first-stage washing liquid; mixing the first-stage washing fly ash with pulping water to obtain first-stage fly ash pulp, and enabling the first-stage fly ash pulp to enter a second-stage eluting and separating device for second-stage eluting to obtain second-stage washing fly ash and second-stage washing liquid; mixing the secondary washing fly ash with pulping water to obtain secondary fly ash pulp, and enabling the secondary fly ash pulp to enter a tertiary elution separation device for tertiary elution to obtain tertiary washing fly ash and tertiary washing liquid; wherein the water content of the water washing fly ash obtained in each stage of elution step is not more than 40%, and the solid content of the water washing liquid is lower than 1%; finally, the three-stage water-washed fly ash is dried to obtain a fly ash finished product, for example, steam or hot air can be used as a drying medium to dry the three-stage water-washed fly ash to obtain the fly ash finished product; wherein the temperature of the drying medium is preferably below 300 ℃, most preferably 160-260 ℃; the water content of the obtained fly ash finished product is lower than 5%.
As a more preferable embodiment of the present invention, the secondary aqueous washing liquid is used as the pulping water in the step (1), and the tertiary aqueous washing liquid is used as the pulping water in the second-stage elution; the circulating water and the fresh water are used as the third-stage eluting pulping water, and the fresh water is used as the third-stage eluting pulping water in the initial work.
As a more preferable specific embodiment of the invention, the step (3) adopts the first-level water washing liquid in the step (2) to carry out purification treatment to obtain clear liquid and sediment slurry, wherein the purification treatment sequentially comprises heavy metal removal, flocculation precipitation treatment and multistage filtration treatment to finally obtain the clear liquid and sediment slurry.
As a more preferable specific embodiment of the invention, the heavy metal removal treatment can be carried out by adding a heavy metal capturing agent (sodium sulfide, sodium thiosulfate and special-purpose agent) into a heavy metal removal device; the flocculation precipitation treatment can be to add a flocculation precipitation reagent to perform flocculation precipitation reaction; the multistage filtration treatment can be carried out by sequentially filtering through filtration membranes with the filtration pore diameters of 10 mu m, 5 mu m and 1 mu m; the pH value is adjusted by using an acid solution to adjust the pH value of the filtrate to 6-8.
As a preferred embodiment of the present invention, the preheating in the step (4) is to preheat the evaporation raw material liquid at a temperature of 90-110 ℃; the evaporation concentration in the step (4) is preferably that the preheated evaporation raw material liquid enters a forced circulation heat exchanger for evaporation concentration treatment, wherein the temperature of the forced circulation heat exchanger is controlled to be 100-120 ℃.
As a preferred embodiment of the present invention, in the step (4), the evaporative crystallization is carried out in an evaporative crystallizer, 5-30g/L gypsum seed crystal is added during the evaporative crystallization, and by utilizing the principle that the affinity of the same substance is greater than that of the different substance, the small solid gypsum particles are uniformly dispersed in the feed liquid in the evaporative crystallizer, and Ca in the feed liquid 2+ And SO 4 2- Will first condense on the solid gypsum nucleus to form gypsum crystal precipitation.
As a preferred embodiment of the present invention, in the step (4), crystal slurry having a gypsum content of 30wt% to 60wt%, concentrated brine and salt slurry having a salt content of 30wt% to 60wt%, respectively, are obtained at the time of performing the evaporative crystallization; separating gypsum and feed liquid in a gypsum separator to obtain feed liquid and crystalline gypsum with water content not more than 60wt%, conveying the separated feed liquid to a forced circulation heat exchanger for further evaporation and concentration treatment, and dechlorinating the crystalline gypsum in a gypsum dehydration device to obtain a gypsum product and a gypsum eluent, wherein the dechlorination is preferably carried out by adopting a gypsum water washing or leaching mode; the gypsum eluent can be used as pulping water in the multi-stage elution process in the step (2); conveying the concentrated salt solution to a forced circulation heat exchanger for evaporation concentration treatment; the salt slurry enters a sodium chloride crystallization separator for crystallization separation to obtain sodium chloride crystal salt, supernatant and sodium chloride mother liquor; cooling the supernatant in a potassium chloride crystallization separator, and separating out crystals when the temperature is reduced to 10-50 ℃ to obtain potassium chloride crystallization salt with water content not more than 6wt%, potassium chloride mother liquor and non-crystallized potassium chloride mother liquor; purifying the non-crystallized potassium chloride mother liquor; and conveying the sodium chloride mother liquor and the potassium chloride mother liquor into a forced circulation heat exchanger for evaporation concentration treatment.
The condensed water generated by the forced circulation heat exchanger is supplied to the multistage preheater for preheating, and the condensed water generated by the multistage preheater can be respectively used as pulping water of the fly ash eluting unit and water of the gypsum dewatering device.
As a preferred embodiment of the present invention, the clear solution described in the step (5) is repeatedly subjected to the treatment steps of (3) to (5).
The above-described methods can be accomplished by those skilled in the art using various conventional equipment for fly ash treatment and reuse, all of which are readily accomplished by those skilled in the art; as a preferred embodiment, the present invention further provides a special system for realizing the disposal method for recycling the waste incineration fly ash water-washing salt based on the seed crystal method, wherein the system comprises a fly ash pulping unit, a fly ash eluting unit, a water washing liquid purifying unit, an evaporation crystallization unit and a drying unit; wherein the fly ash pulping unit is provided with a fly ash slurry outlet, and the fly ash elution unit is provided with a fly ash slurry inlet, a solid-phase product outlet, a liquid-phase product outlet and a pulping water inlet; the washing liquid purification unit is provided with a liquid phase inlet, a liquid phase outlet and a solid phase outlet; the evaporation crystallization unit is provided with an evaporation raw material liquid inlet, an non-crystallization mother liquid outlet and a condensed water outlet;
The solid phase outlet of the water washing liquid purification unit is connected with the inlet of the drying unit, the non-crystallization mother liquor outlet of the evaporation crystallization unit is connected with the liquid phase inlet of the water washing liquid purification unit, and the condensed water outlet of the evaporation crystallization unit is connected with the pulping water inlet of the fly ash elution unit.
As a preferred embodiment of the present invention, the fly ash pulping unit may include a fly ash pretreatment device (i.e., a crushing device), a fly ash buffer device, a fly ash metering device, a water metering device, a pulping apparatus; wherein, the outlet of the fly ash pretreatment device (crushing device) is connected with the inlet of the fly ash buffer device, the outlet of the fly ash buffer device is connected with the inlet of the fly ash metering device, and the outlet of the fly ash metering device and the outlet of the water metering device are both connected with the inlet of the pulping equipment.
As a preferred embodiment of the present invention, the fly ash eluting unit comprises a primary eluting separator, a secondary eluting separator, and a tertiary eluting separator; wherein the first-stage elution and separation device is provided with a fly ash slurry inlet, a water washing liquid outlet and a solid phase outlet; the second-stage elution and separation device is provided with a slurry inlet, a solid phase outlet and a liquid phase inlet; the three-stage elution and separation device is provided with a slurry inlet, a solid phase outlet and a liquid phase outlet; the solid phase outlet of the three-stage elution and separation device is connected with the liquid phase inlet of the two-stage elution and separation device, and the solid phase outlet of the three-stage elution and separation device is connected with the inlet of the drying unit.
As a preferred embodiment of the present invention, the water washing liquid purifying unit may include a heavy metal removing device, a concentration and precipitation device, a multi-stage filtering device, a desliming device and a pH adjusting device; the heavy metal removing device is provided with a washing liquid inlet, a liquid phase outlet and a sludge outlet; the concentration and precipitation device is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the multistage filtering device is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the pH value adjusting device is provided with a liquid phase inlet and a liquid phase outlet; the desliming device is provided with a sludge inlet, a solid phase outlet and a liquid phase outlet; the liquid phase outlet of the heavy metal removal device is connected with the liquid phase inlet of the concentration and precipitation device, the liquid phase outlet of the concentration and precipitation device is connected with the liquid phase inlet of the multistage filtering device, and the liquid phase outlet of the multistage filtering device is connected with the liquid phase inlet of the pH value adjusting device; the sludge outlet of the heavy metal removing device, the sludge outlet of the concentration and precipitation device and the sludge outlet of the multi-stage filtering device are all connected with the sludge inlet of the desliming device; the solid phase outlet of the desliming device is connected with the inlet of the drying unit, the liquid phase outlet of the desliming device is connected with the liquid phase inlet of the heavy metal removing device, and the liquid phase outlet of the pH value adjusting device is connected with the inlet of the evaporative crystallization unit.
As a preferred embodiment of the present invention, the evaporative crystallization unit comprises a multistage preheater, a forced circulation heat exchanger, a gypsum seed tank, an evaporative crystallizer, a gypsum separator, a gypsum dewatering device, a sodium chloride crystallization separator and a potassium chloride crystallization separator; the multistage preheater is provided with an evaporation raw material liquid inlet, a preheated water inlet, a condensed water outlet and a liquid phase outlet; the forced circulation heat exchanger is provided with a feed liquid inlet, a condensed water outlet and an evaporated liquid outlet; the gypsum seed tank is provided with a gypsum seed inlet and a gypsum seed outlet; the evaporation crystallizer is provided with an evaporation liquid inlet, a gypsum seed crystal inlet, a crystal slurry outlet, a salt slurry outlet and a concentrated salt liquid outlet; the gypsum separator is provided with a crystal slurry inlet, a solid phase outlet and a mother liquor outlet; the gypsum dehydration equipment is provided with a solid phase inlet, a water inlet, a gypsum outlet and a liquid phase outlet; the sodium chloride crystallization separator is provided with a salt slurry inlet, a supernatant outlet, a solid phase outlet and a mother liquor outlet; the potassium chloride crystallization separator is provided with a supernatant inlet, a solid phase outlet and a non-crystallization mother liquor outlet;
the evaporation raw material liquid inlet of the multistage preheater is connected with the liquid phase outlet of the pH value adjusting device of the washing liquid purifying unit; the liquid phase outlet of the multistage preheater is connected with the feed liquid inlet of the forced circulation heat exchanger; the gypsum seed outlet of the gypsum seed tank is connected with the gypsum seed inlet of the evaporation crystallizer; the evaporation liquid outlet of the forced circulation heat exchanger is connected with the evaporation liquid inlet of the evaporation crystallizer, the condensed water outlet of the forced circulation heat exchanger is connected with the preheating water inlet of the multistage preheater, the crystal slurry outlet of the evaporation crystallizer is connected with the crystal slurry inlet of the gypsum separator, the salt slurry outlet of the evaporation crystallizer is connected with the salt slurry inlet of the sodium chloride separator, and the concentrated salt liquid outlet of the evaporation crystallizer is connected with the feed liquid inlet of the forced circulation heat exchanger; the mother liquor outlet of the gypsum separator and the mother liquor outlet of the sodium chloride crystallization separator are connected with the feed liquid inlet of the forced circulation heat exchanger through mother liquor return pipelines; the supernatant outlet of the sodium chloride crystallization separator is connected with the supernatant inlet of the potassium chloride crystallization separator; the mother liquor outlet of the potassium chloride crystallization separator is connected with the feed liquor inlet of the forced circulation heat exchanger through a mother liquor return pipeline, and the non-crystallization mother liquor outlet of the potassium chloride crystallization separator is connected with the inlet of the washing liquid purification unit; the solid phase outlet of the gypsum separator is connected with the solid phase inlet of the gypsum dehydration device, the liquid phase outlet of the gypsum dehydration device is connected with the fly ash slurry inlet of the fly ash elution unit, and the condensed water outlet of the multistage preheater is respectively connected with the pulping water inlet of the fly ash elution unit and the water inlet of the gypsum dehydration device.
According to the invention, the gypsum seed crystal method is introduced into the evaporation crystallization process of the washing liquid, so that the decalcification treatment link in the washing liquid purification process is omitted, the washing liquid purification cost is obviously reduced, the scaling of a heat exchanger and an evaporation crystallizer can be effectively prevented, the mass transfer and heat transfer energy consumption is reduced, and the system operation is ensured to be stable in the evaporation salt production process of the washing liquid based on the gypsum seed crystal method; secondly, sulfate radical, calcium ions and calcium sulfate in the water washing liquid are adhered to the gypsum seed crystal to form crystalline gypsum, so that the content of the sulfate radical and the calcium ions in the crystalline salt is effectively reduced, and the quality of the crystalline salt is further improved; thirdly, the spinel paste is subjected to water washing treatment, soluble impurities in gypsum are removed, the added value of gypsum products is improved, and gypsum eluent returns to a fly ash eluting unit to be used as eluting process water, so that the water consumption in the fly ash eluting process and the energy consumption in the evaporating and crystallizing process are effectively reduced.
The invention solves the problems of high water consumption in the fly ash elution process, high consumption of a calcium and magnesium ion remover in the water washing liquid purification process, easy scaling in the evaporation crystallization process and poor quality of crystal salt by organically combining multistage countercurrent elution, water washing liquid purification and gypsum seed crystal method evaporation crystallization.
Compared with the prior art, the invention has the following advantages and outstanding technical effects:
1. The fly ash elution unit adopts multistage countercurrent and alkaline water washing technology, so that the water consumption is low, dust is avoided, the dechlorination effect is good, and the leaching rate of heavy metals is low.
2. The gypsum seed crystal method is adopted, calcium and magnesium ions are not required to be removed in the water quality purification stage, and the water quality purification cost is reduced.
3. The evaporation crystallization process of the fly ash water washing liquid based on the gypsum seed crystal method can effectively prevent the scaling of an evaporator and ensure the stable operation of the system; the technical problem that sulfate radical affects the quality of crystallized salt is solved, and the quality of the salt product can be improved; the condensed water is recycled, so that the energy consumption is reduced.
4. The non-crystallization mother liquor generated by the evaporation crystallization unit is discharged to the water washing liquid purification unit, so that the consumption of forced circulation evaporation equipment can be reduced to a certain extent, and the salt yield of the system can be improved more efficiently.
5. The method utilizes a water washing or leaching mode to dechlorinate the crystal gypsum, thereby improving the value of gypsum products and having good economic benefit.
Drawings
FIG. 1 is a process flow diagram of the method of the present invention.
FIG. 2 is a schematic diagram of the composition and connection of the units of the system of the present invention.
FIG. 3 is a schematic diagram of the composition and connection of the devices in the system of the present invention.
Reference numerals: the device comprises a fly ash pulping unit, a 2 fly ash elution unit, a 3 water washing liquid purification unit, a 4-evaporation crystallization unit, a 5 drying unit, a 1-1 fly ash pretreatment device, a 1-2 fly ash buffer device, a 1-3 fly ash metering device, a 1-4 pulping device, a 1-5 water metering device, a 2-1 primary elution separation device, a 2-2 secondary elution separation device, a 2-3 tertiary elution separation device, a 3-1 heavy metal removal device, a 3-2 concentration precipitation device, a 3-3 multi-stage filtration device, a 3-4pH adjustment device, a 3-5 desliming device, a 4-1 multi-stage preheater, a 4-2 forced circulation heat exchanger, a 4-3 gypsum seed crystal tank, a 4-4 evaporation crystallizer, a 4-5 gypsum separator, a 4-6 gypsum dehydration device, a 4-7 sodium chloride crystal separator and a 4-8 potassium chloride crystal separator.
Detailed Description
The invention will be further described with reference to specific embodiments, and advantages and features of the invention will become apparent from the description. It should be understood that the embodiments described are exemplary only and should not be construed as limiting the scope of the invention in any way. It will be understood by those skilled in the art that various changes and substitutions can be made in the details and form of the technical solution of the present invention without departing from the spirit and scope of the invention, but these changes and substitutions fall within the scope of the present invention.
In the description of the embodiments of the present application, it should be noted that, the indicated orientation or positional relationship is based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship that is conventionally put when the product of the application is used, or the orientation or positional relationship that is conventionally understood by those skilled in the art, or the orientation or positional relationship that is conventionally put when the product of the application is used, which is merely for convenience of describing the application and simplifying the description, and is not indicative or implying that the device or element to be referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the application. In the description of the embodiments of the present application, it should also be noted that, unless explicitly specified and limited otherwise, the terms "disposed," "mounted," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; may be directly connected or indirectly connected through an intermediate medium. The specific meaning of the terms in this application will be understood by those of ordinary skill in the art in a specific context.
In the description of embodiments of the present application, a description of reference to the terms "one embodiment," "some embodiments," "examples," "particular examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
Referring to fig. 1, the invention firstly provides a disposal method for recycling waste incineration fly ash water-washing salt-making based on a seed crystal method, which comprises the following steps: (1) Crushing the waste incineration fly ash, and stirring with pulping water to obtain fly ash slurry; (2) Carrying out multistage elution on the fly ash slurry by using water to obtain water-washed fly ash and water-washing liquid; (3) Purifying the water washing liquid to obtain clear liquid and precipitated slurry; adjusting the pH value of the clear solution by using an acid solution to evaporate the raw material liquid; (4) Sequentially carrying out preheating, evaporation concentration, evaporation crystallization, gypsum separation, sodium chloride separation and potassium chloride crystallization separation treatment on the evaporation raw material liquid to obtain gypsum, potassium chloride and sodium chloride products; wherein, During evaporation and crystallization, gypsum seed crystal is added to make Ca in crystallization liquid 2+ And SO 4 2- Condensing to form gypsum crystal precipitation on the solid gypsum crystal nucleus; (5) Desliming the precipitated slurry obtained in the step (3) to obtain sludge and clear liquid; and (3) drying the sludge and the water-washed fly ash generated in the step (2) to obtain a fly ash finished product.
As a preferred embodiment of the present invention, the crushing in the step (1) is to crush the waste incineration fly ash to particles with the particle size of less than 2 mm; wherein the mass ratio of the crushed waste incineration fly ash particles to the pulping water is preferably 1:2-1:4, and most preferably 1:3.
As a preferred embodiment of the present invention, the multi-stage elution in step (2) is preferably a three-stage elution; specifically, the fly ash slurry prepared in the step (1) enters a first-stage eluting and separating device to carry out first-stage elution to obtain first-stage washing fly ash and first-stage washing liquid; mixing the first-stage washing fly ash with pulping water to obtain first-stage fly ash pulp, and enabling the first-stage fly ash pulp to enter a second-stage eluting and separating device for second-stage eluting to obtain second-stage washing fly ash and second-stage washing liquid; mixing the secondary washing fly ash with pulping water to obtain secondary fly ash pulp, and enabling the secondary fly ash pulp to enter a tertiary elution separation device for tertiary elution to obtain tertiary washing fly ash and tertiary washing liquid; wherein the water content of the water washing fly ash obtained in each stage of elution step is not more than 40%, and the solid content of the water washing liquid is lower than 1%; finally, the three-stage water-washed fly ash is dried to obtain a fly ash finished product, for example, steam or hot air can be used as a drying medium to dry the three-stage water-washed fly ash to obtain the fly ash finished product; wherein the temperature of the drying medium is preferably below 300 ℃, most preferably 160-260 ℃; the water content of the obtained fly ash finished product is lower than 5%.
As a more preferable embodiment of the present invention, the secondary aqueous washing liquid is used as the pulping water in the step (1), and the tertiary aqueous washing liquid is used as the pulping water in the second-stage elution; the circulating water and the fresh water are used as the third-stage eluting pulping water, and the fresh water is used as the third-stage eluting pulping water in the initial work.
As a more preferable specific embodiment of the invention, the step (3) adopts the first-level water washing liquid in the step (2) to carry out purification treatment to obtain clear liquid and sediment slurry, wherein the purification treatment sequentially comprises heavy metal removal, flocculation precipitation treatment and multistage filtration treatment to finally obtain the clear liquid and sediment slurry.
As a more preferable specific embodiment of the invention, the heavy metal removal treatment can be carried out by adding a heavy metal capturing agent (sodium sulfide, sodium thiosulfate and special-purpose agent) into a heavy metal removal device; the flocculation precipitation treatment can be to add a flocculation precipitation reagent to perform flocculation precipitation reaction; the multistage filtration treatment can be carried out by sequentially filtering through filtration membranes with the filtration pore diameters of 10 mu m, 5 mu m and 1 mu m; the pH value is adjusted by using an acid solution to adjust the pH value of the filtrate to 6-8.
As a preferred embodiment of the present invention, the preheating in the step (4) is to preheat the evaporation raw material liquid at a temperature of 90-110 ℃; the evaporation concentration in the step (4) is preferably that the preheated evaporation raw material liquid enters a forced circulation heat exchanger for evaporation concentration treatment, wherein the temperature of the forced circulation heat exchanger is controlled to be 100-120 ℃.
As a preferred embodiment of the present invention, in the step (4), the evaporative crystallization is carried out in an evaporative crystallizer, 5-30g/L gypsum seed crystal is added during the evaporative crystallization, and by utilizing the principle that the affinity of the same substance is greater than that of the different substance, the small solid gypsum particles are uniformly dispersed in the feed liquid in the evaporative crystallizer, and Ca in the feed liquid 2+ And SO 4 2- Will first condense on the solid gypsum nucleus to form gypsum crystal precipitation.
As a preferred embodiment of the present invention, in the step (4), crystal slurry having a gypsum content of 30wt% to 60wt%, concentrated brine and salt slurry having a salt content of 30wt% to 60wt%, respectively, are obtained at the time of performing the evaporative crystallization; separating gypsum and feed liquid in a gypsum separator to obtain feed liquid and crystalline gypsum with water content not more than 60wt%, conveying the separated feed liquid to a forced circulation heat exchanger for further evaporation and concentration treatment, and dechlorinating the crystalline gypsum in a gypsum dehydration device to obtain a gypsum product and a gypsum eluent, wherein the dechlorination is preferably carried out by adopting a gypsum water washing or leaching mode; the gypsum eluent can be used as pulping water in the multi-stage elution process in the step (2); conveying the concentrated salt solution to a forced circulation heat exchanger for evaporation concentration treatment; the salt slurry enters a sodium chloride crystallization separator for crystallization separation to obtain sodium chloride crystal salt, supernatant and sodium chloride mother liquor; cooling the supernatant in a potassium chloride crystallization separator, and separating out crystals when the temperature is reduced to 10-50 ℃ to obtain potassium chloride crystallization salt with water content not more than 6wt%, potassium chloride mother liquor and non-crystallized potassium chloride mother liquor; purifying the non-crystallized potassium chloride mother liquor; and conveying the sodium chloride mother liquor and the potassium chloride mother liquor into a forced circulation heat exchanger for evaporation concentration treatment.
The condensed water generated by the forced circulation heat exchanger is supplied to the multistage preheater for preheating, and the condensed water generated by the multistage preheater can be respectively used as pulping water of the fly ash eluting unit and water of the gypsum dewatering device.
As a preferred embodiment of the present invention, the clear solution described in the step (5) is repeatedly subjected to the treatment steps of (3) to (5).
Referring to fig. 2 and 3, the invention provides a special system for realizing a waste incineration fly ash water-washing salt-making recycling treatment method based on a seed crystal method, which comprises a fly ash pulping unit 1, a fly ash eluting unit 2, a water washing liquid purifying unit 3, an evaporation crystallization unit 4 and a drying unit 5; wherein the fly ash pulping unit 1 is provided with a fly ash slurry outlet, and the fly ash elution unit 2 is provided with a fly ash slurry inlet, a solid-phase product outlet, a liquid-phase product outlet and a pulping water inlet; the washing liquid purification unit 3 is provided with a liquid phase inlet, a liquid phase outlet and a solid phase outlet; the evaporation crystallization unit 4 is provided with an evaporation raw material liquid inlet, an non-crystallization mother liquid outlet and a condensed water outlet; the solid-phase product outlet of the fly ash elution unit 2 is connected with the inlet of the drying unit 5, the liquid-phase product outlet of the fly ash elution unit 2 is connected with the liquid-phase inlet of the water washing liquid purification unit 3, the liquid-phase outlet of the water washing liquid purification unit 3 is connected with the evaporation raw material liquid inlet of the evaporation crystallization unit 4, the solid-phase outlet of the water washing liquid purification unit 3 is connected with the inlet of the drying unit 5, the non-crystallization mother liquor outlet of the evaporation crystallization unit 4 is connected with the liquid-phase inlet of the water washing liquid purification unit 3, and the condensed water outlet of the evaporation crystallization unit 4 is connected with the slurry-making water inlet of the water washing unit 2.
As a preferred embodiment of the present invention, the fly ash pulping unit may comprise a fly ash pretreatment device (i.e., a crushing device) 1-1, a fly ash buffer device 1-2, a fly ash metering device 1-3, a pulping apparatus 1-4, and a water metering device 1-5; wherein, the outlet of the fly ash pretreatment device 1-1 is connected with the inlet of the fly ash buffer device 1-2, the outlet of the fly ash buffer device 1-2 is connected with the inlet of the fly ash metering device 1-3, and the outlet of the fly ash metering device 1-3 and the outlet of the water metering device 1-5 are connected with the inlet of the pulping equipment 1-4.
As a preferred embodiment of the present invention, the fly ash eluting unit comprises a primary eluting separator 2-1, a secondary eluting separator 2-2, and a tertiary eluting separator 2-3; wherein the first-stage eluting separator 2-1 is provided with a fly ash slurry inlet, a water washing liquid outlet and a solid phase outlet; the second-stage elution and separation device 2-2 is provided with a slurry inlet, a solid phase outlet and a liquid phase inlet; the three-stage elution and separation device 2-3 is provided with a slurry inlet, a solid phase outlet and a liquid phase outlet; the water washing liquid outlet of the first-stage elution and separation device 2-1 is connected with the water washing liquid inlet of the water washing liquid purification unit 3, the solid-phase outlet of the first-stage elution and separation device 2-1 is connected with the slurry inlet of the second-stage elution and separation device 2-2, the liquid-phase outlet of the second-stage elution and separation device 2-2 is connected with the inlet of the water metering device 1-5 of the fly ash pulping unit 1, the solid-phase outlet of the second-stage elution and separation device 2-1 is connected with the slurry inlet of the third-stage elution and separation device 2-3, the liquid-phase outlet of the third-stage elution and separation device 2-3 is connected with the liquid-phase inlet of the second-stage elution and separation device 2-2, and the solid-phase outlet of the third-stage elution and separation device 2-3 is connected with the inlet of the drying unit 5.
As a preferred embodiment of the invention, the washing liquid purifying unit 3 can comprise a heavy metal removing device 3-1, a concentration and precipitation device 3-2, a multi-stage filtering device 3-3, a pH value adjusting device 3-4 and a desliming device 3-5; the heavy metal removing device 3-1 is provided with a washing liquid inlet, a liquid phase outlet and a sludge outlet; the concentration and precipitation device 3-2 is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the multistage filtering device 3-3 is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the pH value adjusting device 3-4 is provided with a liquid phase inlet and a liquid phase outlet; the desliming device 3-5 is provided with a sludge inlet, a solid phase outlet and a liquid phase outlet; the water washing liquid inlet of the heavy metal removing device 3-1 is connected with the liquid phase outlet of the first-stage elution separating device 2-1 of the fly ash eluting unit 2, the liquid phase outlet of the heavy metal removing device 3-1 is connected with the liquid phase inlet of the concentration and precipitation device 3-2, the liquid phase outlet of the concentration and precipitation device 3-2 is connected with the liquid phase inlet of the multi-stage filtering device 3-3, and the liquid phase outlet of the multi-stage filtering device 3-3 is connected with the liquid phase inlet of the pH value adjusting device 3-4; the sludge outlet of the heavy metal removing device 3-1, the sludge outlet of the concentrating and precipitating device 3-2 and the sludge outlet of the multi-stage filtering device 3-3 are connected with the sludge inlet of the desliming device 3-5; the solid phase outlet of the desliming device 3-5 is connected with the inlet of the drying unit 5, the liquid phase outlet of the desliming device 3-5 is connected with the liquid phase inlet of the heavy metal removing device 3-1, and the liquid phase outlet of the pH value adjusting device 3-4 is connected with the inlet of the evaporative crystallization unit 4.
As a preferred embodiment of the present invention, the evaporative crystallization unit 4 comprises a multistage preheater 4-1, a forced circulation heat exchanger 4-2, a gypsum seed tank 4-3, an evaporative crystallizer 4-4, a gypsum separator 4-5, a gypsum dewatering device 4-6, a sodium chloride crystallization separator 4-7 and a potassium chloride crystallization separator 4-8; the multistage preheater 4-1 is provided with an evaporation raw material liquid inlet, a preheated water inlet, a condensed water outlet and a liquid phase outlet; the forced circulation heat exchanger 4-2 is provided with a feed liquid inlet, a condensed water outlet and an evaporated liquid outlet; the gypsum seed tank 4-3 is provided with a gypsum seed inlet and a gypsum seed outlet; the evaporation crystallizer 4-4 is provided with an evaporation liquid inlet, a gypsum seed crystal inlet, a crystal slurry outlet, a salt slurry outlet and a concentrated salt liquid outlet; the gypsum separator 4-5 is provided with a crystal slurry inlet, a solid phase outlet and a mother liquor outlet; the gypsum dewatering equipment 4-6 is provided with a solid phase inlet, a water inlet, a gypsum outlet and a liquid phase outlet; the sodium chloride crystallization separator 4-7 is provided with a salt slurry inlet, a supernatant outlet, a solid phase outlet and a mother liquor outlet; the potassium chloride crystallization separator 4-8 is provided with a supernatant inlet, a solid phase outlet and a non-crystallization mother liquor outlet; wherein, the evaporation raw material liquid inlet of the multistage preheater 4-1 is connected with the liquid phase outlet of the pH value adjusting device 3-4 of the washing liquid purifying unit 3; the liquid phase outlet of the multistage preheater 4-1 is connected with the feed liquid inlet of the forced circulation heat exchanger 4-2; the gypsum seed crystal outlet of the gypsum seed crystal tank 4-3 is connected with the gypsum seed crystal inlet of the evaporation crystallizer 4-4; the evaporation liquid outlet of the forced circulation heat exchanger 4-2 is connected with the evaporation liquid inlet of the evaporation crystallizer 4-4, the condensed water outlet of the forced circulation heat exchanger 4-2 is connected with the preheating water inlet of the multistage preheater 4-1, the crystal slurry outlet of the evaporation crystallizer 4-4 is connected with the crystal slurry inlet of the gypsum separator 4-5, the salt slurry outlet of the evaporation crystallizer 4-4 is connected with the salt slurry inlet of the sodium chloride crystallization separator 4-7, and the concentrated salt liquid outlet of the evaporation crystallizer 4-4 is connected with the feed liquid inlet of the forced circulation heat exchanger 4-2; the mother liquor outlet of the gypsum separator 4-5 and the mother liquor outlet of the sodium chloride crystallization separator 4-7 are connected with the feed liquor inlet of the forced circulation heat exchanger 4-2 through mother liquor return pipelines; the supernatant outlet of the sodium chloride crystallization separator 4-7 is connected with the supernatant inlet of the potassium chloride crystallization separator 4-8; the mother liquor outlet of the potassium chloride crystallization separator 4-8 is connected with the feed liquor inlet of the forced circulation heat exchanger 4-2 through a mother liquor return pipeline, and the non-crystallization mother liquor outlet of the potassium chloride crystallization separator 4-8 is connected with the inlet of the washing liquid purification unit 3; the solid phase outlet of the gypsum separator 4-5 is connected with the solid phase inlet of the gypsum dewatering device 4-6, the liquid phase outlet of the gypsum dewatering device 4-6 is connected with the fly ash slurry inlet of the fly ash eluting unit 2, and the condensed water outlet of the multistage preheater 4-1 is respectively connected with the pulping water inlet of the fly ash eluting unit 2 and the water inlet of the gypsum dewatering device 4-6.
The various devices or apparatuses used in the utility model are conventional devices in solid waste reprocessing or waste fly ash reprocessing technologies, which can be purchased commercially and can be applied to the utility model; in addition, the related literature also discloses new improved devices, and better technical effects can be achieved by adopting the new improved devices, such as: fly ash pulping equipment (CN 204848668U, title: fly ash washing apparatus); a first-stage elution separator (CN 204848668U, title: fly ash washing apparatus), a second-stage elution separator (CN 204848668U, title: fly ash washing apparatus), and a third-stage elution separator (CN 204848668U, title: fly ash washing apparatus); heavy metal removing device and concentration and precipitation device (CN 204973179U, the utility model name is a multifunctional buffer pool for treating fly ash washing wastewater, CN 208660466U, the utility model name is a mud scraper for treating high-viscosity easily-hardened materials), and a multistage filtering device (CN 205627217U, the utility model name is a quick-opening type multi-medium filter).
The method and system of the present utility model are further described below in conjunction with specific embodiments.
Example 1
Step 1: pulping of fly ash
Step 1-1: pretreating the massive waste incineration fly ash to be treated in a fly ash pretreatment device (crushing device) 1-1, and crushing the fly ash to a particle size of below 2 mm; and then fed into fly ash buffer 1-2.
Step 1-2: the crushed waste incineration fly ash and pulping water are weighed by a fly ash metering device 1-3 respectively, and are stirred and mixed in a pulping device 1-4 according to the proportion of 1:3, and are subjected to hydration reaction and pulping, and finally the fly ash slurry is obtained.
Step 2: fly ash elution
The fly ash slurry is respectively subjected to primary elution, secondary elution and tertiary elution treatment in the primary elution and separation device 2-1, the secondary elution and separation device 2-2 and the tertiary elution and separation device 2-3 in sequence to obtain water-washed fly ash and water-washed liquid; the water washing ash is sequentially sent to the following steps: the fly ash slurry obtained in the step 1-2 enters a first-stage eluting and separating device 2-1 to obtain first-stage water-washed ash (the water content is less than or equal to 55%) and first-stage water-washed liquid (the slag content is less than or equal to 1%), and the first-stage water-washed ash and water are proportioned into first-stage fly ash slurry; the first-stage fly ash enters a second-stage eluting and separating device 2-2 to obtain second-stage water washing ash (the water content is less than or equal to 55 percent) and second-stage water washing liquid (the slag content is less than or equal to 10 percent), and the second-stage water washing ash is proportioned with water to form second-stage fly ash; the secondary fly ash slurry enters a tertiary eluting and separating device 2-3 to obtain tertiary washing ash (the water content is less than or equal to 40%) and tertiary washing liquid (the slag content is less than or equal to 10%).
The washing liquid is sequentially sent to the following steps: the primary water washing liquid enters a water washing liquid purifying unit 3; the secondary water washing liquid enters the water metering device 1-5 to be used as pulping water; the tertiary washing liquid is sent to a secondary eluting and separating device 2-2 and is used as secondary fly ash slurry proportioning water; the FWD process circulating water and the make-up water are used as three-stage eluting pulping water, and the clean water is used as three-stage eluting pulping water in the initial work.
Step 3: drying of fly ash
And (3) drying the water-washed fly ash in the step (2) by using steam or hot air as a drying medium (the set temperature of the drying medium is 230 ℃), and finally obtaining a fly ash finished product with the water content lower than 5%.
Step 4: water wash purification
Step 4-1: the water washing liquid generated by the primary elution enters a heavy metal removal device 3-1 added with a heavy metal capturing agent (sodium sulfide, sodium thiosulfate and special agents) with certain mass concentration, so that the heavy metal content in water is reduced, and the water washing liquid after heavy metal removal is subjected to solid-liquid separation to obtain clear liquid and wet mud;
step 4-2: the clear liquid in the step 4-1 enters a concentration and precipitation device 3-2 added with a flocculation and precipitation medicament with a certain mass concentration to obtain a supernatant and wet mud;
step 4-3: the supernatant obtained in the step 4-2 is fed into a multistage filtration device (10 μm, 5 μm, 1 μm) 3-3 to obtain filtrate and filter residue (i.e. wet sludge).
Step 4-4: the filtrate in the step 4-3 enters a pH value adjusting device 3-4, an acidic reagent with a certain mass concentration is required to be added into the pH value adjusting device 3-4, and finally evaporation raw material liquid is obtained;
step 4-5: the wet sludge in the steps 4-1, 4-2 and 4-3 enters a desliming device 3-5 for treatment, the generated sludge enters a drying unit 5 along with water washing ash for drying treatment, and the generated liquid phase enters a heavy metal removal device 3-1 for retreatment.
Step 5: evaporative crystallization
Step 5-1: the raw material liquid is preheated in a multistage preheater 4-1 to be heated to the evaporating temperature of 90-100 ℃;
step 5-2: the preheated feed liquid enters a forced circulation heat exchanger 4-2 for evaporation and concentration treatment, the program temperature of the heat exchanger is set to 110 ℃, and when the solid-liquid ratio of the feed liquid is more than or equal to 30%, the next operation is carried out;
step 5-3: the concentrated feed liquid enters an evaporation crystallizer 4-4, and is crystallized and layered in the evaporation crystallizer 4-4 to obtain crystal slurry with gypsum content of 30-60 wt%, concentrated salt solution and salt slurry with salt content of 30-60 wt%. The concentrated salt solution is conveyed to a forced circulation heat exchanger 4-2 to be continuously evaporated and concentrated; the crystal slurry enters a gypsum separator 4-5; the salt slurry enters a sodium chloride crystallization separator 4-7, and the crystallization salt and the feed liquid are separated to obtain sodium chloride crystallization salt with the water content of not more than 6wt%, supernatant and sodium chloride mother liquor.
Step 5-4: the supernatant fluid in the step 5-3 enters a potassium chloride crystallization separator 4-8 when reaching a potassium chloride saturated solution, cooling treatment is carried out, crystals are separated out when the temperature is reduced to 10-50 ℃, and potassium chloride crystallization salt, potassium chloride mother liquor and non-crystallized potassium chloride mother liquor (the impurity content in the potassium chloride mother liquor reaches 0.5-10 wt%); the non-crystallized potassium chloride mother liquor is discharged to a water washing liquid purifying unit 3 for purifying treatment.
Step 5-5: and (3) conveying the sodium chloride mother liquor in the step 5-3 and the potassium chloride mother liquor in the step 5-4 to a forced circulation heat exchanger 4-2 for continuous evaporation concentration treatment.
Step 5-6: in the step 5-3, the evaporation crystallizer 4-4 needs to add 10-30g/L gypsum seed crystal, and by utilizing the principle that the affinity of the same substance is larger than that of different substances, the small solid gypsum particles are uniformly dispersed in the feed liquid in the evaporation crystallizer, and Ca in the feed liquid 2+ And SO 4 2- Will first condense on the solid gypsum nucleus to form gypsum crystal precipitation.
Step 5-7: the crystal slurry in the step 5-3 enters a gypsum separator 4-5, gypsum and feed liquid are separated to obtain crystal gypsum with the water content not more than 60wt%, and the separated feed liquid is conveyed to a forced circulation heat exchanger 4-2 for continuous evaporation concentration treatment;
Step 5-8: the crystallized gypsum in the step 5-7 is delivered to a gypsum dewatering device 4-6 for treatment, preferably, the gypsum is dechlorinated by water washing or leaching, and the gypsum eluent is delivered to a fly ash eluting unit 2 to be used as pulping water.
Wherein, the condensed water generated by the forced circulation heat exchanger 4-2 is used for preheating water of the multistage preheater 4-1, and the temperature of the preheating water can reach 80-100 ℃;
the condensed water produced by the multistage preheater 4-1 can be used as water for pulping of the fly ash eluting unit 2 and water for the gypsum dewatering device 4-6, respectively.
Claims (12)
1. The recycling treatment method of the waste incineration fly ash water washing salt based on the seed crystal method is characterized by comprising the following steps of: (1) Crushing the waste incineration fly ash, and stirring with pulping water to obtain fly ash slurry; (2) Carrying out multistage elution on the fly ash slurry by using water to obtain water-washed fly ash and water-washing liquid; (3) Purifying the water washing liquid to obtain clear liquid and precipitated slurry; adjusting the pH value of the clear solution by using an acid solution to evaporate the raw material liquid; (4) Sequentially carrying out preheating, evaporation concentration, evaporation crystallization, gypsum separation, sodium chloride separation and potassium chloride crystallization separation treatment on the evaporation raw material liquid to obtain gypsum, potassium chloride and sodium chloride products; wherein, gypsum seed crystal is added during evaporation and crystallization to lead Ca in crystallization feed liquid 2+ And SO 4 2- AgglomerationForming gypsum crystal precipitation on the solid gypsum crystal nucleus; (5) Desliming the precipitated slurry obtained in the step (3) to obtain sludge and clear liquid; drying the sludge and the water-washed fly ash generated in the step (2) to obtain a fly ash finished product;
the multi-stage elution in the step (2) is three-stage elution; the three-stage elution comprises: feeding the fly ash slurry prepared in the step (1) into a first-stage eluting and separating device for first-stage eluting to obtain first-stage water-washed fly ash and first-stage water-washing liquid; mixing the first-stage washing fly ash with pulping water to obtain first-stage fly ash pulp, and enabling the first-stage fly ash pulp to enter a second-stage eluting and separating device for second-stage eluting to obtain second-stage washing fly ash and second-stage washing liquid; mixing the secondary washing fly ash with pulping water to obtain secondary fly ash pulp, and enabling the secondary fly ash pulp to enter a tertiary elution separation device for tertiary elution to obtain tertiary washing fly ash and tertiary washing liquid; wherein the water content of the water washing fly ash obtained in each stage of elution step is not more than 40%, and the solid content of the water washing liquid is lower than 1%; finally, drying the three-stage washing fly ash to obtain a fly ash finished product; taking the secondary water washing liquid as pulping water in the step (1), and taking the tertiary water washing liquid as pulping water in the second-stage elution; circulating water and fresh water are used as pulping water for third-stage elution, and fresh water is used as pulping water for third-stage elution during initial operation;
In the step (4), the evaporation crystallization is carried out in an evaporation crystallizer, and 5-30g/L gypsum seed crystal is added during the evaporation crystallization to carry out the evaporation crystallization.
2. The recycling method according to claim 1, wherein the crushing in the step (1) is to crush the waste incineration fly ash into particles with a particle size of 2mm or less; wherein the mass ratio of the crushed waste incineration fly ash particles to the pulping water is 1:2-1:4;
in the step (2), steam or hot air is adopted as a drying medium to dry the tertiary washing fly ash to obtain a fly ash finished product; wherein the temperature of the drying medium is 160-260 ℃.
3. The recycling treatment method according to claim 2, wherein the mass ratio of the crushed waste incineration fly ash particles to the pulping water is 1:3.
4. The recycling treatment method according to claim 1, wherein the step (3) is performed with the primary washing liquid of the step (2) to obtain a clear liquid and a precipitated slurry, and the purification treatment sequentially comprises heavy metal removal, flocculation precipitation treatment and multistage filtration treatment to finally obtain the clear liquid and the precipitated slurry.
5. The recycling treatment method according to claim 4, wherein the heavy metal removal treatment is a heavy metal removal treatment by adding a heavy metal capturing agent into a heavy metal removal device; the flocculation precipitation treatment is to add a flocculation precipitation reagent to perform flocculation precipitation reaction; the multistage filtration treatment is carried out by a filtration membrane with a filtration pore diameter of 0.05-10 mu m; the pH value is adjusted by using an acid solution to adjust the pH value of the filtrate to 6-8.
6. The recycling treatment method according to claim 1, wherein the preheating in the step (4) means preheating the evaporation raw material liquid to 80 ℃ to 110 ℃; and (3) evaporating and concentrating in the step (4) to enable the preheated evaporating raw material liquid to enter a forced circulation heat exchanger for evaporating and concentrating treatment, wherein the temperature of the forced circulation heat exchanger is controlled to be 90-120 ℃.
7. The recycling treatment method according to claim 1, wherein in the step (4), crystal slurry, concentrated salt solution and salt slurry are obtained after evaporation and crystallization, respectively; separating gypsum and feed liquid in a gypsum separator to obtain feed liquid and crystalline gypsum, conveying the separated feed liquid to a forced circulation heat exchanger for continuous evaporation and concentration treatment, and treating the crystalline gypsum in a gypsum dehydration device to obtain a gypsum product and gypsum eluent; taking the gypsum eluent as pulping water in the multistage elution process in the step (2); conveying the concentrated salt solution to a forced circulation heat exchanger for evaporation concentration treatment; the salt slurry enters a sodium chloride crystallization separator for crystallization separation to obtain sodium chloride crystal salt, supernatant and sodium chloride mother liquor; introducing the supernatant into a potassium chloride crystallization separator for cooling treatment and separation to obtain potassium chloride crystallization salt, potassium chloride mother liquor and non-crystallized potassium chloride mother liquor, and purifying the non-crystallized potassium chloride mother liquor; conveying the sodium chloride mother liquor and the potassium chloride mother liquor into a forced circulation heat exchanger for evaporation concentration treatment;
The condensed water generated by the forced circulation heat exchanger is supplied to the multistage preheater for preheating, and the condensed water generated by the multistage preheater can be respectively used as pulping water of the fly ash eluting unit and water of the gypsum dewatering device.
8. A system for implementing the recycling process according to any one of claims 1-7, characterized in that the system comprises a fly ash pulping unit (1), a fly ash elution unit (2), a water wash purification unit (3), an evaporative crystallization unit (4) and a drying unit (5); wherein the fly ash pulping unit (1) is provided with a fly ash slurry outlet, and the fly ash elution unit (2) is provided with a fly ash slurry inlet, a solid-phase product outlet, a liquid-phase product outlet and a pulping water inlet; the washing liquid purifying unit (3) is provided with a liquid phase inlet, a liquid phase outlet and a solid phase outlet; the evaporation crystallization unit (4) is provided with an evaporation raw material liquid inlet, a non-crystallization mother liquid outlet and a condensed water outlet; the device is characterized in that a fly ash slurry outlet of the fly ash pulping unit (1) is connected with a fly ash slurry inlet of the fly ash eluting unit (2), a solid phase product outlet of the fly ash eluting unit (2) is connected with an inlet of the drying unit (5), a liquid phase product outlet of the fly ash eluting unit (5) is connected with a liquid phase inlet of the water washing liquid purifying unit (3), a liquid phase outlet of the water washing liquid purifying unit (3) is connected with an evaporation raw material liquid inlet of the evaporation crystallizing unit (4), a solid phase outlet of the water washing liquid purifying unit (3) is connected with an inlet of the drying unit (5), a non-crystallization mother liquid outlet of the evaporation crystallizing unit (4) is connected with a liquid phase inlet of the water washing liquid purifying unit (3), and a condensed water outlet of the evaporation crystallizing unit (4) is connected with a pulping water inlet of the fly ash eluting unit (2).
9. The system according to claim 8, characterized in that the fly ash pulping unit comprises a fly ash pretreatment device (1-1), a fly ash buffer device (1-2), a fly ash metering device (1-3), a pulping apparatus (1-4), a water metering device (1-5); wherein, the outlet of the fly ash pretreatment device (1-1) is connected with the inlet of the fly ash buffer device (1-2), the outlet of the fly ash buffer device (1-2) is connected with the inlet of the fly ash metering device (1-3), and the outlet of the fly ash metering device (1-3) and the outlet of the water metering device (1-5) are connected with the inlet of the pulping equipment (1-4).
10. The system according to claim 8, characterized in that the fly ash elution unit (2) comprises a primary elution separation device (2-1), a secondary elution separation device (2-2) and a tertiary elution separation device (2-3); the first-stage elution and separation device (2-1) is provided with a fly ash slurry inlet, a water washing liquid outlet and a solid phase outlet; the second-stage elution and separation device (2-2) is provided with a slurry inlet, a solid phase outlet and a liquid phase inlet; the three-stage elution and separation device (2-3) is provided with a slurry inlet, a solid phase outlet and a liquid phase outlet; the solid-phase outlet of the first-stage elution separation device (2-1) is connected with the slurry inlet of the third-stage elution separation device (2-3), the solid-phase outlet of the first-stage elution separation device (2-1) is connected with the slurry inlet of the second-stage elution separation device (2-2), the liquid-phase outlet of the second-stage elution separation device (2-2) is connected with the inlet of the water metering device (1-5) of the fly ash pulping unit (1), the solid-phase outlet of the second-stage elution separation device (2-1) is connected with the slurry inlet of the third-stage elution separation device (2-3), the liquid-phase outlet of the third-stage elution separation device (2-3) is connected with the liquid-phase inlet of the second-stage elution separation device (2-3), and the solid-phase outlet of the third-stage elution separation device (2-3) is connected with the inlet of the drying unit (5).
11. The system according to claim 8, wherein the water wash purification unit (3) may comprise a heavy metal removal device (3-1), a concentration and precipitation device (3-2), a multi-stage filtration device (3-3), a pH adjustment device (3-4) and a desliming device (3-5); the heavy metal removing device (3-1) is provided with a washing liquid inlet, a liquid phase outlet and a sludge outlet; the concentration and precipitation device (3-2) is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the multistage filtering device (3-3) is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the pH value adjusting device (3-4) is provided with a liquid phase inlet and a liquid phase outlet; the desliming device (3-5) is provided with a sludge inlet, a solid phase outlet and a liquid phase outlet; the heavy metal removing device comprises a heavy metal removing device (3-1), a first-stage elution separating device (2-1) and a pH value adjusting device (3-4), wherein a water washing liquid inlet of the heavy metal removing device (3-1) is connected with a liquid phase outlet of the first-stage elution separating device (2-1) of the fly ash eluting unit (2), a liquid phase outlet of the heavy metal removing device (3-1) is connected with a liquid phase inlet of the concentration and precipitation device (3-2), a liquid phase outlet of the concentration and precipitation device (3-2) is connected with a liquid phase inlet of the multi-stage filtering device (3-3), and a liquid phase outlet of the multi-stage filtering device (3-3) is connected with a liquid phase inlet of the pH value adjusting device (3-4); the sludge outlet of the heavy metal removing device (3-1), the sludge outlet of the concentrating and precipitating device (3-2) and the sludge outlet of the multi-stage filtering device (3-3) are connected with the sludge inlet of the desliming device (3-5); the solid phase outlet of the desliming device (3-5) is connected with the inlet of the drying unit (5), the liquid phase outlet of the desliming device (3-5) is connected with the liquid phase inlet of the heavy metal removing device (3-1), and the liquid phase outlet of the pH value adjusting device (3-4) is connected with the inlet of the evaporation crystallization unit (4).
12. The system according to claim 8, wherein the evaporative crystallization unit (4) comprises a multistage preheater (4-1), a forced circulation heat exchanger (4-2), a gypsum seed tank (4-3), an evaporative crystallizer (4-4), a gypsum separator (4-5), a gypsum dewatering device (4-6), a sodium chloride crystallization separator (4-7) and a potassium chloride crystallization separator (4-8); the multistage preheater (4-1) is provided with an evaporation raw material liquid inlet, a preheated water inlet, a condensed water outlet and a liquid phase outlet; the forced circulation heat exchanger (4-2) is provided with a feed liquid inlet, a condensed water outlet and an evaporated liquid outlet; the gypsum seed tank (4-3) is provided with a gypsum seed inlet and a gypsum seed outlet; the evaporation crystallizer (4-4) is provided with an evaporation liquid inlet, a gypsum seed crystal inlet, a crystal slurry outlet, a salt slurry outlet and a concentrated salt liquid outlet; the gypsum separator (4-5) is provided with a crystal slurry inlet, a solid phase outlet and a mother liquor outlet; the gypsum dehydration equipment (4-6) is provided with a solid phase inlet, a water inlet, a gypsum outlet and a liquid phase outlet; the sodium chloride crystallization separator (4-7) is provided with a salt slurry inlet, a supernatant outlet, a solid phase outlet and a mother liquor outlet; the potassium chloride crystallization separator (4-8) is provided with a supernatant inlet, a solid phase outlet and a non-crystallization mother liquor outlet; wherein, the evaporation raw material liquid inlet of the multistage preheater (4-1) is connected with the liquid phase outlet of the pH value adjusting device (3-4) of the washing liquid purifying unit (3); the liquid phase outlet of the multistage preheater (4-1) is connected with the feed liquid inlet of the forced circulation heat exchanger (4-2); the gypsum seed outlet of the gypsum seed tank (4-3) is connected with the gypsum seed inlet of the evaporation crystallizer (4-4); the evaporation liquid outlet of the forced circulation heat exchanger (4-2) is connected with the evaporation liquid inlet of the evaporation crystallizer (4-4), the condensed water outlet of the forced circulation heat exchanger (4-2) is connected with the preheating water inlet of the multistage preheater (4-1), the crystal slurry outlet of the evaporation crystallizer (4-4) is connected with the crystal slurry inlet of the gypsum separator (4-5), the salt slurry outlet of the evaporation crystallizer (4-4) is connected with the salt slurry inlet of the sodium chloride crystallization separator (4-7), and the concentrated salt liquid outlet of the evaporation crystallizer (4-4) is connected with the feed liquid inlet of the forced circulation heat exchanger (4-2); the mother liquor outlet of the gypsum separator (4-5) and the mother liquor outlet of the sodium chloride crystallization separator (4-7) are connected with the feed liquid inlet of the forced circulation heat exchanger (4-2) through mother liquor return pipelines; the supernatant outlet of the sodium chloride crystallization separator (4-7) is connected with the supernatant inlet of the potassium chloride crystallization separator (4-8); the mother liquor outlet of the potassium chloride crystallization separator (4-8) is connected with the feed liquor inlet of the forced circulation heat exchanger (4-2) through a mother liquor return pipeline, and the non-crystallization mother liquor outlet of the potassium chloride crystallization separator (4-8) is connected with the inlet of the washing liquid purification unit (3); the solid phase outlet of the gypsum separator (4-5) is connected with the solid phase inlet of the gypsum dewatering device (4-6), the liquid phase outlet of the gypsum dewatering device (4-6) is connected with the fly ash slurry inlet of the fly ash elution unit (2), and the condensed water outlet of the multistage preheater (4-1) is respectively connected with the pulping water inlet of the fly ash elution unit (2) and the water inlet of the gypsum dewatering device (4-6).
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| CN113955889A (en) * | 2021-08-31 | 2022-01-21 | 江西盖亚环保科技有限公司 | Resource recovery process of fly ash washing liquid |
| CN113772708A (en) * | 2021-09-23 | 2021-12-10 | 华新绿源环保股份有限公司 | Comprehensive recycling treatment process for complex waste salt system |
| CN114377338B (en) * | 2021-12-28 | 2024-07-30 | 郑州鸿跃环保科技有限公司 | Treatment system and treatment method for detoxification of aluminum electrolysis cell overhaul slag |
| CN114716165B (en) * | 2022-04-29 | 2024-07-05 | 中洁蓝环保科技有限公司 | Multi-stage fly ash washing integrated system and method |
| CN115716078A (en) * | 2022-10-17 | 2023-02-28 | 北京中科国润环保科技有限公司 | Method and system for resource utilization of carbon dioxide |
| CN116197223A (en) * | 2023-03-06 | 2023-06-02 | 句容台泥水泥有限公司 | Centralized treatment system and method for massive fly ash generated by incineration of household garbage in power plant |
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