CN216837507U - Incineration fly ash washing water recycling treatment device - Google Patents
Incineration fly ash washing water recycling treatment device Download PDFInfo
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- CN216837507U CN216837507U CN202122852769.4U CN202122852769U CN216837507U CN 216837507 U CN216837507 U CN 216837507U CN 202122852769 U CN202122852769 U CN 202122852769U CN 216837507 U CN216837507 U CN 216837507U
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Abstract
The utility model relates to a recycling treatment device for incineration fly ash washing water, which utilizes an incineration fly ash washing system to wash out soluble salt in incineration fly ash, controls chloride ions of the washing fly ash to be less than or equal to 0.04 percent and is used for cement production; aiming at the fly ash washing water, firstly, a washing water pretreatment system is utilized to remove heavy metal ions, calcium ions, organic pollutants and suspended matters in the fly ash washing water, and the concentration of the suspended matters in the effluent of the washing water pretreatment system is controlled to be less than or equal to 0.1 mg/L; separating high-valence ions in the effluent of the washing water pretreatment system by using a membrane separation concentration system, concentrating the TDS of the effluent of the membrane separation concentration system to 150-250 g/L of concentrated solution, and purifying to obtain recycled water; finally, respectively producing sodium chloride with the purity higher than 98.5% and potassium chloride with the purity higher than 90.0% by using an evaporative crystallization salt separation system; thereby realizing the purpose of recycling the incineration fly ash washing water.
Description
Technical Field
The utility model relates to a recycling treatment device for incineration fly ash washing water, belonging to the technical field of industrial wastewater treatment.
Background
The municipal solid waste incineration plants in China can greatly reduce the land occupation of the municipal solid waste landfill, but the incineration fly ash with the grain diameter less than or equal to 100 mu m is generated in the waste incineration process, and the chemical composition of the incineration fly ash is mainly SiO 2、Al2O3、Fe2O3、CaO、MgO、K2O、Na2O, Cl, S, F, partial Hg, As, Pb, Cd, Cr, Cu, Ni, Zn, Mn and other heavy metal elements; the incineration fly ash is characterized by containing heavy metals, soluble salts, particularly chloride, dioxin, furan and other harmful substances, and having high pollution degree to underground water and surrounding environment; the best mode for harmless and resource treatment of the incineration fly ash is to use the incineration fly ash as a comprehensive silicon, aluminum and calcium substitute raw material for cement production, calcine the incineration fly ash and limestone, clay and other substances in a cement rotary kiln to form cement clinker of which the main components are tricalcium silicate, tricalcium aluminate and dicalcium silicate, but the quality of cement is affected by more heavy metals and chlorides contained in the incineration fly ash, and the cement rotary kiln is corroded in the high-temperature firing process, so when the cement clinker is produced by utilizing the incineration fly ash, the incineration fly ash is washed by water firstly, and the contents of the heavy metals and chlorides in the incineration fly ash are reduced, so that the requirements of the cement production are met.
In the incineration fly ash washing process, on one hand, a large amount of washing water is consumed, on the other hand, 25-35% of water-soluble components are dissolved out from the incineration fly ash to generate a large amount of fly ash washing water containing NaCl, KCl and heavy metal ions, the fly ash washing water needs to be subjected to resource treatment, heavy metal pollutants in the fly ash washing water are removed, and water, potassium chloride and sodium chloride are effectively recovered; the utility model provides a recycling treatment device for incineration fly ash washing water from the viewpoints of simple and practical process and good water and salt resource recovery.
Disclosure of Invention
The utility model provides a device for recycling incineration fly ash washing water, aiming at the characteristics that the incineration fly ash contains heavy metals, soluble salts, particularly chlorine salts, dioxin, furan and other harmful substances, and the element proportion of the typical incineration fly ash is as follows: 50-200 g/kg of Si, 90-130 g/kg of Ca, 80-190 g/kg of Cl, 50-80 g/kg of Al, 15-44 g/kg of Fe, 30-90 g/kg of K, 15-80 g/kg of Na, 15-30 g/kg of Mg, 10-25 g/kg of S, 2-18 g/kg of Zn, 2-10 g/kg of Pb, 0.5-3 g/kg of Cu, 1-3 g/kg of Mn, 0.15-0.7 g/kg of Cd, 0.1-0.6 g/kg of Cr, 0.1-0.3 g/kg of Ni and 0.05-0.3 g/kg of As; HJ 662-2013 'environmental protection technical specification for treating solid waste by cooperating with cement kiln'. Regard that incineration fly ash is pretreated to meet the requirement of entering the kiln and then is put into a high-temperature section at the rear end of the cement kiln, so that dioxin in the fly ash is degraded at high temperature while cement clinker is produced, and harmless treatment of the incineration fly ash is realized; the limit value of the content of the main heavy metals in the washed fly ash after the washing treatment is as follows: (Tl + Cd + Pb +15As) is less than or equal to 230mg/kg, and (Be + Cr +10Sn +50Sb + Cu + Mn + Ni + V) is less than or equal to 1150mg/kg, wherein the limit on chlorine elements is very strict, and Cl is required to Be less than or equal to 0.04% (400 mg/kg); the limit value of GB 30760-2014 technical Specification for cement kiln co-processing solid waste on the content of heavy metals in raw materials entering a kiln is as follows: as is less than or equal to 28mg/kg, Pb is less than or equal to 67mg/kg, Cd is less than or equal to 1.0mg/kg, Cr is less than or equal to 98mg/kg, Cu is less than or equal to 65mg/kg, Ni is less than or equal to 65mg/kg, Zn is less than or equal to 361mg/kg, and Mn is less than or equal to 384 mg/kg; according to the incineration fly ash washing system, the incineration fly ash is subjected to three times of countercurrent washing and membrane filtration dehydration by using 5-15 times of large washing water quantity, so that chloride and heavy metals in the incineration fly ash are well washed away, and the washing fly ash is sent to a cement rotary kiln to produce cement clinker.
The incineration fly ash washing water contains Ca2+、Mg2+、Na+、K+、Cl-、SO4 2-High ion concentration, and contains partial heavy metal ions and SiO2And COD, when the incineration fly ash water contains 25-35% of soluble components and the washing water amount is 5-15 times of that of the incineration fly ash, the typical incineration fly ash washing water comprises the following components: ca2+(calcium ion) 0.4-2.4 g/L, Mg2+(magnesium ion) 0.24-1.4 g/L, Na+(sodium ion) 3-10 g/L, K+(Potassium ion) 3-12 g/L, Cl-(chloride ion) 9-30 g/L, SO4 2-2-5 g/L, Cu (sulfate radical) (copper) 0.03-0.2 g/L, Cr (chromium) 0.006-0.04 g/L, Zn (zinc) 0.1-0.7 g/L, Pb (lead) 0.08-0.5 g/L, Cd (cadmium) 0.01-0.04 g/L, SiO2(silica) 0.03-0.2 g/L, TDS (total dissolved solids)) 17.9-62.5 g/L, COD (chemical oxygen demand) 0.1-0.6 g/L, pH 10-12; aiming at the incineration fly ash washing water, firstly, a washing water pretreatment system is utilized, calcium ions, magnesium ions, heavy metal ions, silicon dioxide and suspended matters in the incineration fly ash washing water are removed by sequentially adding sulfuric acid, organic sulfur, sodium carbonate, a flocculating agent and a coagulant aid for reaction, precipitation and sludge-water separation, and the concentration of the suspended matters in the pretreated effluent water is controlled to be less than or equal to 0.1 mg/L; separating high-valence ions in the effluent of the washing water pretreatment system by using a membrane separation concentration system, concentrating the TDS of the effluent of the membrane separation concentration system to 150-250 g/L concentrated solution, and purifying the effluent for reuse in an incineration fly ash washing system; finally, crystallizing and separating out sodium chloride with the purity higher than 98.5 percent which meets the first-level standard requirement of refined industrial dry salt specified by GB/T5462-; effectively recovering water and salt resources in the incineration fly ash washing water.
The mud-water separation membrane in the washing water pretreatment system is made of PVDF (polyvinylidene fluoride), so that the acid and alkali resistance is high, the service life is long, the membrane aperture is less than or equal to 50nm, the filtering precision is high, and the effect is good; the material separation membrane is made of polyamide composite membrane material and is MgSO4The removal rate of the waste incineration fly ash washing water is more than or equal to 98 percent, the removal rate of NaCl is less than or equal to 20 percent, and the separation of high-valence ions in the incineration fly ash washing water can be effectively carried out.
In the evaporative crystallization salt separation system, the thermal method is used for carrying out evaporative crystallization salt separation on sodium chloride and potassium chloride, and the difference of the solubility properties of the sodium chloride and the potassium chloride in water is large, see the following table:
solubility table unit of sodium chloride and potassium chloride in water: g/100g water
| Temperature of | 0 | 10 | 20 | 30 | 40 | 50 | 60 | 70 | 80 | 90 | 100 |
| NaCl | 35.7 | 35.8 | 36.0 | 36.3 | 36.6 | 37.0 | 37.3 | 37.8 | 38.4 | 39.0 | 39.8 |
| KCl | 28.0 | 31.2 | 34.2 | 37.2 | 40.1 | 42.6 | 45.8 | 48.8 | 51.3 | 53.9 | 56.3 |
From the table it can be seen that: the solubility of sodium chloride in water is not changed greatly in a temperature range of 0-100 ℃, only the difference is 4.1g/100g of water, while the solubility of potassium chloride in water is changed greatly in a temperature range of 0-100 ℃, the difference is 28.3g/100g of water, sodium chloride is separated out through continuous evaporation concentration of an evaporator through crystallization in a high-temperature region of 80-90 ℃, and when potassium chloride is saturated, potassium chloride is separated out through crystallization in a low-temperature region of 30-40 ℃.
The technical solution of the utility model is as follows: the incineration fly ash washing water recycling treatment device structurally comprises an incineration fly ash washing system, a washing water pretreatment system, a membrane separation concentration system and an evaporative crystallization salt separation system; wherein, the incineration fly ash is pneumatically conveyed to an ash inlet of an incineration fly ash washing system, and the incineration fly ash is discharged from an ash outlet of the incineration fly ash washing system; the water outlet of the incineration fly ash washing system sends out fly ash washing water to a No. 1 water inlet of the washing pretreatment system, and a sludge outlet of the washing pretreatment system sends out sludge cakes; the water outlet of the washing pretreatment system sends the effluent of the washing pretreatment system to the water inlet of the membrane separation concentration system, the concentrated water outlet of the membrane separation concentration system sends the material separation concentrated water to the No. 2 water inlet of the washing pretreatment system, the water outlet of the membrane separation concentration system sends the effluent of the membrane separation concentration system to the liquid inlet of the evaporation crystallization salt separation system, the supplementary steam is connected to the steam inlet of the evaporation crystallization salt separation system, the reuse water sent from the reuse water outlet of the membrane separation concentration system and the condensed water sent from the condensed water outlet of the evaporation crystallization salt separation system are converged into the raw water to the water inlet of the incineration fly ash washing system; the No. 1 salt outlet of the evaporative crystallization salt separation system sends out sodium chloride, and the No. 2 salt outlet of the evaporative crystallization salt separation system sends out potassium chloride KCl; a resource treatment device for incineration fly ash washing water is used for washing soluble salt in incineration fly ash by using an incineration fly ash washing system, controlling chloride ions of the washing fly ash to be less than or equal to 0.03 percent and is used for cement production; aiming at the fly ash washing water, firstly, a washing water pretreatment system is utilized to remove heavy metal ions, calcium ions, organic pollutants and suspended matters in the fly ash washing water; separating high-valence ions in the effluent of the washing water pretreatment system by using a membrane separation concentration system, concentrating the TDS of the effluent of the membrane separation concentration system to 150-250 g/L of concentrated solution, and purifying to obtain recycled water; finally, respectively producing sodium chloride with the purity higher than 98.5% and potassium chloride with the purity higher than 90.0% by using an evaporative crystallization salt separation system; the purpose of recycling the incineration fly ash washing water is realized.
The utility model has the advantages that the utility model discloses a resource treatment device for incineration fly ash washing water, which utilizes an incineration fly ash washing system to wash out soluble salt in the incineration fly ash, controls chloride ions of the washing fly ash to be less than or equal to 0.04 percent and is used for cement production; aiming at the fly ash washing water, firstly, a washing water pretreatment system is utilized to remove heavy metal ions, calcium ions, organic pollutants and suspended matters in the fly ash washing water, and the concentration of the suspended matters in the effluent of the washing water pretreatment system is controlled to be less than or equal to 0.1 mg/L; separating high-valence ions in the effluent of the washing water pretreatment system by using a membrane separation concentration system, concentrating the TDS of the effluent of the membrane separation concentration system to 150-250 g/L of concentrated solution, and purifying to obtain recycled water; finally, respectively producing sodium chloride with the purity higher than 98.5% and potassium chloride with the purity higher than 90.0% by using an evaporative crystallization salt separation system; thereby realizing the purpose of recycling the incineration fly ash washing water.
Drawings
FIG. 1 is a schematic view of the overall structure of a recycling apparatus for incineration fly ash washing water.
In the drawing, FA represents incineration fly ash, WFA represents water washing fly ash, SC represents mud cake, CW represents material separation concentrate, RW represents raw water, RCW represents reuse water, CCW represents condensed water, NaCl represents sodium chloride, KCl represents potassium chloride, SM represents makeup steam, WW represents incineration fly ash wash water, PTO represents wash pretreatment system effluent, MSCO represents membrane separation concentration system effluent, WWs represents incineration fly ash water washing system, PTS represents wash pretreatment system, MSCS represents membrane separation concentration system, MVRS represents evaporative crystallization salt separation system.
FIG. 2 is a schematic view of an incineration fly ash washing system of a incineration fly ash washing water resource treatment apparatus.
In the drawing, WWS represents an incineration fly ash water washing system, FA represents incineration fly ash, WW represents incineration fly ash washing water, RW represents raw water, and WFA represents washing fly ash; FAT denotes incineration fly ash storage silo, AT denotes pulping tank, MT11Indicating a first-stage tank, WT11Denotes the first-order water wash tank, DMF11Indicating one-stage disc filters, MT12Indicating a secondary water tank, WT12Denotes the two-stage Water washing tank, DMF12Indicating two-stage disc filters, MT13Denotes a three-stage tank, WT13Denotes a three-stage washing tank, DMF13Three-stage disc filter, DE dryer, WFAT washing fly ash silo, MT14Represents the fly ash wash tank, QP11Represents a constant feeder, QP, of the incineration fly ash12Representing fly ash conveyors, QP13Shows the water washing fly ash feeder, P11Showing a primary suction pump, P12Denotes a fly ash wash water delivery pump, P13Denotes a two-stage suction pump, P14A three stage suction pump is shown.
FIG. 3 is a schematic structural view of a washing water pretreatment system of a recycling treatment apparatus for incineration fly ash washing water.
In the figure, PTS represents a washing water pretreatment system, WW represents incineration fly ash washing water, CW represents material separation concentrated water, PTO represents washing water outlet water of the washing water pretreatment system, SC represents mud cake, BT represents a fly ash washing water adjusting tank, D 21Means for adding sulfuric acid and heavy metal removing agent, RT21Denotes a first-order reaction tank, ST21Denotes a primary sedimentation tank, D22Indicating the adding device of sodium carbonate, flocculant and coagulant aid, RT22Denotes a secondary reaction tank, ST22Representing a secondary sedimentation tank, OCE representing an ozone catalytic oxidation device, O3G represents smellyOxygen generator, SWST represents mud-water separation membrane pool, MT21Indicating the outlet tank, MT, of the pretreatment of the washing water22Denotes sludge thickener, PF denotes Filter Press, MT23Denotes the filter-pressing liquid pool, P21Denotes a lift pump, P22Denotes a suction pump, P23Showing the delivery pump of the effluent of the washing pretreatment system, P24Indicating backwash pump, P25Indicating a sludge pump, P26The filtrate return pump is shown.
FIG. 4 is a schematic diagram showing a membrane separation and concentration system of a recycling apparatus for incineration fly ash washing water.
In the drawing, MSCS represents a membrane separation concentration system, PTO represents effluent of a washing pretreatment system, CW represents material separation concentration water, RCW represents reuse water, MSCO represents effluent of the membrane separation concentration system, D31Denotes a scale inhibitor addition apparatus, SAF31Show material separation membrane safety filter, MSM shows material separation membrane device, MT31Indicating material-separating concentrate tank, MT32Water tank for indicating material separation, SAF32Showing electrodialytic cartridge filters, ED showing electrodialytic apparatus, MT 33Showing the water outlet tank, MT, of the membrane separation concentration system34Indicating an electrodialysis water tank, SAF33Showing a reverse osmosis cartridge filter, RO showing a reverse osmosis unit, MT35Indicating the reuse of the water tank, P31High-pressure pumps indicating separation of material, P32Denotes an electrodialysis feed water pump, P33Denotes an evaporative crystallization feed pump, P34Denotes a reverse osmosis booster pump, P35Denotes a reverse osmosis high-pressure pump, P36Indicating a reuse water transfer pump, P37Showing a material separation concentrated water delivery pump.
FIG. 5 is a schematic diagram of an evaporative crystallization salt separation system of a recycling treatment device for incineration fly ash washing water.
In the attached drawing, VSCS represents an evaporation crystallization salt separation system, MSCO represents effluent of a membrane separation concentration system, CCW represents condensed water, NaCl represents sodium chloride, KCl represents potassium chloride, SM represents supplement steam, and CW41Indicating cooling water intake, CW42Indicating cooling water return, PHE41Denotes a primary preheater, PHE42The secondary pre-heater is shown as a secondary pre-heater,DMV for falling film evaporator, DMS for falling film separator, PCV for forced circulation evaporator, PCS for forced circulation separator, SP for vapor compressor, MT41Denotes the condensate tank, CE denotes the thickener, CSE41Indicating sodium salt centrifuge, DPE41Indicating sodium salt weighing and packaging machine, MT42Sodium salt mother liquor tank, CCT Cooling crystallizer, CSE 42Indicating potassium salt centrifuge, DPE42Indicating potassium salt weighing packer, MT43Indicates the sylvite mother liquor tank, PHE43Denotes a potassium salt mother liquor preheater, P41Showing a falling film circulating pump, P42Showing falling film evaporation transfer pump, P43Denotes a condensate pump, P44Denotes a forced circulation pump, P45Denotes a sodium salt discharge pump, P46Denotes the sodium salt mother liquor pump, P47Indicating potassium salt discharge pump, P48The potassium salt mother liquor pump is shown. FIG. 6 is a water balance diagram of an example of recycling incineration fly ash washing water.
Detailed Description
Referring to the attached figure 1, the incineration fly ash washing water recycling treatment device structurally comprises an incineration fly ash washing system WWS, a washing water pretreatment system PTS, a membrane separation concentration system MSCS and an evaporative crystallization salt separation system MVRS; wherein, the incineration fly ash FA is pneumatically conveyed to an ash inlet of an incineration fly ash washing system WWS, and an ash outlet of the incineration fly ash washing system WWS sends out water washing fly ash WFA; the water outlet of the incineration fly ash washing system WWS sends incineration fly ash washing water WW to a No. 1 water inlet of a washing pretreatment system PTS, and a mud outlet of the washing pretreatment system PTS sends out a mud cake SC; a water outlet of the washing pretreatment system PTS sends out washing pretreatment system effluent PTO to a water inlet of a membrane separation concentration system MSCS, a concentrated water outlet of the membrane separation concentration system MSCS sends out material separation concentrated water CW to a No. 2 water inlet of the washing pretreatment system PTS, a water outlet of the membrane separation concentration system MSCS sends out membrane separation concentration system effluent MSCO to a liquid inlet of an evaporative crystallization salt separation system MVRS, supplementary steam SM is connected to a steam inlet of the evaporative crystallization salt separation system MVRS, and recycle water RCW sent out from a recycle water outlet of the membrane separation concentration system MSCS and condensed water CCW sent out from a condensed water outlet of the evaporative crystallization salt separation system MVRS are converged into raw water RW to a water inlet of an incineration fly ash washing system WWS; sodium chloride NaCl is sent out from a No. 1 salt outlet of the MVRS of the evaporative crystallization salt separation system, and potassium chloride KCl is sent out from a No. 2 salt outlet of the MVRS of the evaporative crystallization salt separation system; a resource treatment device for incineration fly ash washing water is used for washing soluble salt in incineration fly ash by utilizing an incineration fly ash washing system, controlling chloride ions of the washing fly ash to be less than or equal to 0.03 percent and being used for cement production; aiming at the fly ash washing water, firstly, a washing water pretreatment system is utilized to remove heavy metal ions, fluorine ions, calcium ions, organic pollutants and suspended matters in the fly ash washing water; separating high-valence ions in the effluent of the washing water pretreatment system by using a membrane separation concentration system, concentrating the TDS of the effluent of the membrane separation concentration system to 150-250 g/L of concentrated solution, and purifying to obtain recycled water; finally, respectively producing sodium chloride with the purity higher than 98.5% and potassium chloride with the purity higher than 90.0% by using an evaporative crystallization salt separation system; the purpose of recycling the incineration fly ash washing water is realized.
Referring to FIG. 2, the incineration fly ash washing system WWS comprises an incineration fly ash storage bunker FAT, a pulping tank AT and a primary water tank MT11First-stage water washing tank WT11First-stage disc type filter DMF11Second-level water tank MT12Second stage water washing tank WT12Two-stage disc type filter DMF12Third-level water tank MT13Three-stage washing tank WT13Three-stage disc filter DMF13DE of dryer, water washing fly ash storage silo WFAT and fly ash water washing tank MT14QP quantitative feeder for incineration fly ash11QP fly ash conveyor12QP (constant-temperature) water washing fly ash feeding machine13First-stage suction pump P11Fly ash washing water delivery pump P12Second-stage suction pump P13Three-stage suction pump P14(ii) a Wherein the incineration fly ash FA is pneumatically conveyed to an ash inlet of an incineration fly ash storage bin FAT, and an ash outlet of the incineration fly ash storage bin FAT passes through an incineration fly ash constant feeder QP11Connected with the ash inlet of the pulping tank AT, a three-stage water tank MT13The 2# water outlet is connected with the water inlet of a pulping tank AT, and the pulp outlet of the pulping tank AT is connected with a first-stage water washing tank WT11A slurry inlet of the first-level water tank MT11The water outlet of the water tank is connected to a first-stage water washing tank WT11Water inlet of (1) first stageWater washing tank WT11The slurry outlet is connected to a first-stage disc type filter DMF11The slurry inlet of the first-stage disc type filter is DMF11The water outlet of the water pump passes through a primary suction pump P 11And a fly ash water washing tank MT14Is connected with a water inlet of a fly ash washing water tank MT14The water outlet of the fly ash washing water delivery pump P12Sending out incineration fly ash washing water WW; DMF (dimethyl formamide) of primary disc type filter11Is connected to a second-stage water washing tank WT12Ash inlet, second-level water tank MT12The water outlet of the water tank is connected to a second-stage water washing tank WT12Water inlet of, the second-stage washing tank WT12The slurry outlet is connected to a second-stage disc type filter DMF12Slurry inlet of the two-stage disc filter DMF12The water outlet of the pump passes through a secondary suction pump P13With a first-level water tank MT11Connected with the water inlet of the second-stage disc filter DMF12The ash outlet is connected to a three-stage water washing tank WT13The raw water RW is connected to the third-stage water tank MT13Water inlet of (2), three-stage water tank MT13The 1# water outlet is connected to a three-stage washing tank WT13Water inlet of the three-stage washing tank WT13The slurry outlet is connected to a three-stage disc filter DMF13Slurry inlet of the three-stage disc filter DMF13The water outlet of the water pump passes through a three-stage suction pump P14With a second-stage water tank MT12Connected with the water inlet of the three-stage disc filter DMF13The ash outlet of the fly ash conveyor is connected to an ash inlet of the dryer DE, and the ash outlet of the dryer DE passes through a fly ash conveyor QP12An ash inlet of the washing fly ash storage bin WFAT and an ash outlet of the washing fly ash storage bin WFAT pass through a washing fly ash feeding machine QP 13The water washed fly ash WFA is sent out.
Referring to FIG. 3, the PTS of the pretreatment system structurally comprises a fly ash washing water adjusting tank BT, a sulfuric acid and heavy metal removing agent feeding device D21First-order reaction tank RT21First-stage sedimentation tank ST21Sodium carbonate, flocculating agent and coagulant aid adding device D22Second stage reaction tank RT22Second-stage sedimentation tank ST22Ozone catalytic oxidation device OCE and ozone generator O3G. Water outlet tank MT for pretreatment of SWST (single-wall separation) and washing water in mud-water separation membrane pool21Sludge thickener MT22PF of filter press and MT of filter pressing liquid pool23Lift pump P21A suction pump P22And a water outlet delivery pump P of a washing pretreatment system23And a backwash pump P24And a sludge pump P25Filtrate return pump P26(ii) a Wherein the incineration fly ash washing water WW is connected to the 1# water inlet of the fly ash washing water regulating tank BT, the material separation concentrated water CW is connected to the 2# water inlet of the fly ash washing water regulating tank BT, and the water outlet of the fly ash washing water regulating tank BT is connected with the lift pump P21With a first-stage reaction tank RT21Is connected with the water inlet of the device D for adding the sulfuric acid and the heavy metal removing medicament21The drug outlet is connected to a first-stage reaction tank RT21The first-stage reaction tank RT21The water outlet of the water tank is connected to a first-stage sedimentation tank ST21Water inlet of the first-stage sedimentation tank ST21The water outlet of the reaction tank is connected to a secondary reaction tank RT22Water inlet, sodium carbonate, flocculating agent and coagulant aid adding device D 22The medicine outlet is connected to a secondary reaction tank RT22A medicine inlet of the second-stage reaction tank RT22The water outlet of the water tank is connected to a secondary sedimentation tank ST22Water inlet of (2), secondary sedimentation tank ST22The water outlet of the ozone generator is connected to the water inlet of an ozone catalytic oxidation device OCE3The gas outlet of the G is connected to the gas inlet of an ozone catalytic oxidation device OCE, the water outlet of the ozone catalytic oxidation device OCE is connected to the water inlet of a mud-water separation membrane pool SWST, and a primary sedimentation tank ST21A sludge outlet and a secondary sedimentation tank ST22The sludge outlet and the backwashing water outlet of the sludge-water separation membrane tank SWST are connected to a sludge concentration tank MT22A sludge inlet and a sludge concentration tank MT22The sludge outlet of the sludge pump passes through a sludge pump P25The sludge outlet of the filter press PF is connected with the sludge inlet of the filter press PF and used for delivering a sludge cake SC; the pressure filtrate outlet of the filter press PF is connected to a pressure filtrate tank MT23Water inlet of filter pressing liquid pool MT23The water outlet of the filter is connected with a filter liquor reflux pump P26A 3# water inlet connected to the fly ash washing water regulating tank BT; the water outlet of the mud-water separation membrane pool SWST passes through a suction pump P22MT (water tank) for pretreatment of washing water and water outlet tank21Is connected with the water inlet of the washing water pretreatment water outlet tank MT 211# water outlet of the pump passes through a backwashing pump P24And mud-water separation membrane pool SThe backwash water inlet of the WST is connected, and the water outlet tank MT for the pretreatment of the backwash water 212# water outlet through the outlet water delivery pump P of the washing pretreatment system23And (4) sending out a washing pretreatment system outlet water PTO.
Referring to the attached figure 4, the MSCS of the membrane separation concentration system structurally comprises a scale inhibitor feeding device D31SAFETY FILTER SAF FOR MATERIAL-SEPARATING MEMBRANE31MSM (Material Merge volume) and MT (concentrated Water tank) for material separation of material separation membrane device31Material separating water producing tank MT32SAFE FILTER SAF FOR ELECTRO-ELECTROLYSIS32Electrodialysis device ED, membrane separation concentration system water outlet box MT33Electroosmosis water tank MT34SAFE SAFETY FILTER SAF FOR ANTI-SEVERATION OF RO33RO and MT recycling water tank of reverse osmosis device35Material separating high pressure pump P31Electrodialysis water supply pump P32And a liquid feed pump P for evaporative crystallization33Reverse osmosis booster pump P34Reverse osmosis high pressure pump P35And a reuse water delivery pump P36And a material separation concentrated water delivery pump P37(ii) a Wherein the water outlet PTO of the washing water pretreatment system is connected to a material separation membrane cartridge filter SAF31Water inlet, antisludging agent feeding device D31The medicine outlet is also connected to a SAF filter of a material separation membrane31The material separation membrane cartridge filter SAF31The water outlet of the high-pressure pump P is separated by materials31Connected with the water inlet of the material separation membrane device MSM, and the concentrated water outlet of the material separation membrane device MSM is connected to the material separation concentrated water tank MT 31Water inlet, material separation concentrate tank MT31The water outlet of the pump is provided with a material separation concentrated water delivery pump P37Sending out material separation concentrated water CW; the water-producing outlet of the material separation membrane device MSM is connected to the material separation water-producing tank MT 321# water inlet, material separation water production tank MT32Water outlet of the water supply pump is connected with an electrodialysis water supply pump P32SAF filter SAF with electrodialysis32Connected with the water inlet of the filter, and an electrodialysis cartridge filter SAF32Is connected to the water inlet of the electrodialysis device ED, and the water outlet of the electrodialysis device ED is connected to the electrodialysis water production tank MT34Water inlet of (2), electrodialysis water tank MT34The water outlet of the water pump passes through a reverse osmosis booster pump P34SAFE FILTER SAF WITH ANTI-PERMEATION33Connected with the water inlet of the reverse osmosis cartridge filter SAF33The water outlet of the water pump passes through a reverse osmosis high-pressure pump P35Connected with the water inlet of the reverse osmosis device RO, and the concentrated water outlet of the reverse osmosis device RO is connected to the material separation water production tank MT322# water inlet, the produced water outlet of the reverse osmosis device RO is connected to the recycling water tank MT35Water inlet and reuse water tank MT35The water outlet of the water pump is connected with a reuse water delivery pump P36Sending out recycle water RCW; the concentrated water outlet of the electrodialysis device ED is connected to the water outlet tank MT of the membrane separation concentration system33Water outlet tank MT of membrane separation concentration system 33The water outlet of the pump is evaporated and crystallized by a liquid supply pump P33And sending the effluent MSCO out of the membrane separation concentration system.
Referring to FIG. 5, the evaporative crystallization salt separation system VSCS comprises a primary preheater PHE41PHE of secondary preheater42DMV of falling film evaporator, DMS of falling film separator, PCV of forced circulation evaporator, PCS of forced circulation separator, SP of vapor compressor, MT of condensate water tank41CE and sodium salt centrifuge CSE of thickener41Sodium salt weighing and packaging machine DPE41Sodium salt mother liquor tank MT42Cooling crystallizing tank CCT, sylvite centrifuge CSE42DPE (double layer polyethylene) of potassium salt weighing and packaging machine42Potassium salt mother liquor tank MT43Potassium salt mother liquor preheater PHE43Falling film circulating pump P41Falling film evaporation material transfer pump P42Condensate pump P43Forced circulation pump P44Sodium salt discharging pump P45Sodium salt mother liquor pump P46Potassium salt discharging pump P47Sylvite mother liquor pump P48(ii) a Wherein the MSCO of the effluent of the membrane separation concentration system is connected to a primary preheater PHE41The feed liquid inlet of the first-stage preheater PHE41The feed liquid outlet is connected to a secondary preheater PHE42Feed liquid inlet of the second-stage preheater PHE42The feed liquid outlet of the falling film evaporator DMV is connected to the feed liquid inlet of the No. 1 feed liquid inlet of the falling film evaporator DMV, the feed liquid outlet of the falling film evaporator DMV is connected to the feed liquid inlet of the falling film separator DMS, and the No. 1 feed liquid outlet of the falling film separator DMS passes through the falling film circulating pump P 41Connected with the 2# feed liquid inlet of the DMV of the falling film evaporator to dropThe No. 2 material liquid outlet of the membrane separator DMS passes through a falling film evaporation material transfer pump P42Connected to the 1# feed liquid inlet of a forced circulation evaporator PCV, and a secondary preheater PHE42The condensed water outlet of the condenser, the condensed water outlet of the falling film evaporator DMV and the condensed water outlet of the forced circulation evaporator PCV are all connected to a condensed water tank MT41Water inlet of (2), condensate tank MT41The water outlet of the water pump passes through a condensate pump P43Is connected to a primary preheater PHE41Water inlet of (1), primary preheater PHE41The water outlet of the water tank is used for sending out condensed water CCW; the feed liquid outlet of the forced circulation evaporator PCV is connected to the feed liquid inlet No. 1 of the forced circulation separator PCS, and the feed liquid outlet of the forced circulation separator PCS passes through a forced circulation pump P44Connected to the 2# feed liquid inlet of the PCV, the vapor outlet of the DMS and the vapor outlet of the PCS are connected to the vapor inlet of the vapor compressor SP, and the vapor outlet of the vapor compressor SP and the supplementary vapor SM are connected to the PHE42The vapor inlet of the falling film evaporator DMV and the vapor inlet of the forced circulation evaporator PCV; the discharge port 1# of the forced circulation separator PCS passes through a sodium salt discharge pump P45Connected to the inlet of thickener CE, and the outlet of thickener CE is connected to sodium salt centrifuge CSE 41Sodium salt centrifuge CSE41The filtrate outlet is connected to a sodium salt mother liquor tank MT42Liquid inlet of (2), sodium salt mother liquor tank MT42The liquid outlet of the sodium salt mother liquor pump P462# feed liquid inlet connected to forced circulation separator PCS, sodium salt centrifuge CSE41The salt outlet is connected to a sodium salt weighing and packaging machine DPE41Sodium salt inlet, sodium salt weighing and packaging machine DPE41The salt outlet of the device sends sodium chloride NaCl; the 2# discharge port of the forced circulation separator PCS passes through a sylvite discharge pump P47Is connected to a feed inlet of a cooling crystallization tank CCT and cooling water is fed with CW41A cooling water inlet connected to the CCT of the cooling crystallization tank, and a cooling water outlet for cooling the CCT of the crystallization tank sends cooling water backwater CW42(ii) a A discharge port of the cooling crystallization tank CCT is connected to a potassium salt centrifuge CSE42The feed inlet of the sylvite centrifuge CSE42The filtrate outlet is connected to a potassium salt mother liquor tank MT43The liquid inlet of the potassium salt mother liquor tank MT43The liquid outlet of the reactor is connected with a potassium salt mother liquor pump P48Preheater PHE for potassium salt mother liquor43The liquid inlet of the potassium salt mother liquor preheater PHE is connected with43The liquid outlet of the potassium salt centrifugal separator is connected to a 3# feed liquid inlet of the forced circulation separator PCS and a potassium salt centrifugal machine CSE42The salt outlet of the salt-removing device is connected to a potassium salt weighing and packaging machine DPE42Salt inlet, potassium salt weighing and packaging machine DPE42The salt outlet of the device sends out potassium chloride KCl.
The method for recycling incineration fly ash washing water comprises the following steps:
1) The soluble salt in the incineration fly ash is washed out by an incineration fly ash washing system, the content of chloride ions in the washing fly ash is controlled to be less than or equal to 0.04 percent, and the incineration fly ash is reused for cement production.
2) Through the washing pretreatment system, the fly ash washing water is subjected to reaction, precipitation, catalytic oxidation and sludge-water separation, heavy metal ions, calcium ions, organic pollutants and suspended matters in the fly ash washing water are removed, and the concentration of the suspended matters in the effluent of the washing pretreatment system is controlled to be less than or equal to 0.1 mg/L.
3) Separating high-valence ions in the effluent of the washing water pretreatment system through a membrane separation concentration system, and returning the material separation concentrated water to washing water pretreatment; the TDS of the effluent of the membrane separation concentration system is concentrated to 150-250 g/L of concentrated solution, and meanwhile, the recycled water is purified.
4) And (3) evaporating and crystallizing the concentrated solution of the membrane separation and concentration system to obtain sodium chloride with the purity higher than 98.5% and potassium chloride with the purity higher than 90.0% through an evaporation and crystallization salt separation system, and finally realizing the purpose of recycling the incineration fly ash washing water.
Washing out soluble salt in the incineration fly ash through an incineration fly ash washing system in the step 1), controlling the content of chloride ions in the washing fly ash to be less than or equal to 0.04%, and reusing the washing fly ash for cement production; specifically, aiming at the characteristics that incineration fly ash contains heavy metals, soluble salts, especially chlorine salt, dioxin, furan and other harmful substances, the typical incineration fly ash comprises the following elements in percentage by weight: 50-200 g/kg of Si, 90-130 g/kg of Ca, 80-190 g/kg of Cl, 50-80 g/kg of Al, 15-44 g/kg of Fe, 30-90 g/kg of K, 15-80 g/kg of Na, 15-30 g/kg of Mg, 10-25 g/kg of S, 2-18 g/kg of Zn, 2-10 g/kg of Pb, 0.5-3 g/kg of Cu, 1-3 g/kg of Mn, 0.15-0.7 g/kg of Cd, 0.1-0.6 g/kg of Cr, 0.1-0.3 g/kg of Ni and 0.05-0.3 g/kg of As; and (3) carrying out three times of countercurrent washing and membrane filtration dehydration on the incineration fly ash by using 5-15 times of larger washing water amount, well washing off chlorides and heavy metals in the incineration fly ash, controlling Cl in the washing fly ash to be less than or equal to 0.4g/kg, and delivering the washing fly ash to a cement rotary kiln to produce cement clinker.
The step 2) is to perform reaction, precipitation, catalytic oxidation and sludge-water separation on the fly ash washing water through the washing water pretreatment system, remove heavy metal ions, calcium ions, organic pollutants and suspended matters in the fly ash washing water, and control the concentration of the suspended matters in the effluent of the washing water pretreatment system to be less than or equal to 0.1 mg/L; particularly, Ca is contained in the incineration fly ash washing water2+、Mg2+、Na+、K+、Cl-、SO4 2-High ion concentration, and contains partial heavy metal ions and SiO2And COD characteristics, namely water concentration: ca2+0.4 to 2.4g/L, Mg2+0.24 to 1.4g/L, Na+Is 3 to 10g/L, K+Is 3 to 12g/L, Cl-9 to 30g/L, SO4 2-2 to 5g/L, Cu of 0.03 to 0.2g/L, Cr of 0.006 to 0.04g/L, Zn of 0.1 to 0.7g/L, Pb of 0.08 to 0.5g/L, Cd of 0.01 to 0.04g/L, SiO20.03-0.2 g/L, TDS of 17.9-62.5 g/L, COD of 0.1-0.8 g/L, pH of 10-12; firstly, adding sulfuric acid and a heavy metal removing agent into a primary reaction tank, adjusting the pH value of incineration fly ash washing water from 10-12 to 6.5-7.5, and removing Cu, Cr, Zn, Pb, Cd and SiO by using a primary sedimentation tank2With a portion of Mg2+Adding sodium carbonate, PAC and PAM into a secondary reaction tank, and removing Ca by using a secondary sedimentation tank2+The COD in the waste water is reduced by ozone catalytic oxidation, and the waste water is filtered by a mud-water separation membrane with the membrane aperture less than or equal to 50nm to effectively filter the residual fine CaCO in the waste liquid 3With metal hydroxide crystals and suspended matters, controlling the pH of the effluent of the washing pretreatment system to be 6.5-7.5, and controlling the SS to be not less than 0.1mg/L, Cu and not more than 0.1mg/L, Cr and not more than 0.1mg/L, Zn and not more than 0.1mg/L, Pb and not more than 0.1mg/L, Cd and not more than 0.1mg/L, SiO2≤5.0mg/L、COD≤50mg/L、Ca2+≤100mg/L、Mg2+≤200mg/L、SO4 2-≤2000mg/L、K+3000-12000 mg/L, Na+3340-11840 mg/L, Cl-12000-30000 mg/L, TDS is 20645-56145 mg/L; the mud-water separation membrane device automatically performs backwashing for 30-90 seconds every 30-90 minutes so as to maintain long-term stable operation of the mud-water separation membrane; and (5) carrying out outward transportation treatment on the precipitated sludge and the sludge cake obtained by backwashing, draining and press-filtering.
The step 3) separates high-valence ions in the effluent of the washing water pretreatment system through a membrane separation concentration system, and the material separation concentrated water returns to the washing water pretreatment; concentrating TDS of effluent of a membrane separation concentration system to 150-250 g/L of concentrated solution, and simultaneously purifying recycled water; particularly, aiming at the effluent of a washing water pretreatment system, firstly, the MgSO (MgSO) pair is utilized4Separating high-valence ions in the incineration fly ash washing water by using a material separation membrane with the removal rate of more than or equal to 98% and the removal rate of NaCl of less than or equal to 20%, and returning the material separation concentrated water which is concentrated to 1/10-1/5 to a washing water pretreatment system; main ions of water produced by material separation: k+2.85 to 11.4g/L, Na +3.173-11.248 g/L, Cl-11.4-28.5 g/L, TDS is 17.423-51.148 g/L, TDS of effluent of the membrane separation concentration system is concentrated to 150-250 g/L concentrated solution by electrodialysis, mainly sodium chloride and potassium chloride are sent to an evaporation crystallization salt separation system; the TDS of the electrodialysis effluent is 0.5-2 g/L, and the effluent with the TDS less than or equal to 0.05g/L is purified by reverse osmosis and reused in an incineration fly ash washing system.
In the step 4), the concentrated solution of the membrane separation concentration system is evaporated and crystallized to obtain sodium chloride with the purity higher than 98.5% and potassium chloride with the purity higher than 90.0% through an evaporation crystallization salt separation system, and finally the purpose of recycling the incineration fly ash washing water is achieved; specifically, a membrane separation concentration system sends out NaCl and KCl feed liquid with the concentration of 150-250 g/L, falling film evaporation and forced circulation evaporation are adopted, primary standard requirements of refined industrial dry salt specified by GB/T5462-; the recovered steam with the temperature of 85 ℃ is pressurized and heated to 105 ℃ by a steam compressor with the temperature difference of 20 ℃ for recycling; the TDS of the condensed water is less than or equal to 0.05g/L, and the condensed water is used for preheating the feeding material and then is reused in an incineration fly ash washing system after being cooled; finally, the aim of recycling the waste incineration fly ash washing water is fulfilled.
Examples
Two 5000T/D cement production lines exist in a certain cement plant, and the urban domestic garbage incineration fly ash is treated by utilizing the cooperation of the existing cement kilns; the embodiment aims at the characteristics of incineration fly ash and fly ash washing water, and utilizes the incineration fly ash washing water resource treatment technology to construct an incineration fly ash washing dechlorination and fly ash washing water treatment system with the incineration fly ash treatment capacity of 360T/D; the water washing fly ash is used for replacing part of cement raw materials, so that the pollution problem of incineration fly ash is solved, and reverse osmosis produced water, condensed water, sodium chloride and potassium chloride are effectively recovered.
1. Design of incineration fly ash washing water parameters
1.1 design incineration fly ash composition and Ash amount
The main components of the incineration fly ash are as follows: unit: g/kg
| Composition (I) | Si | Ca | Cl | Al | Fe | K |
| Concentration of | 120 | 110 | 170 | 62 | 26 | 75 |
| Composition (I) | Na | Mg | S | Zn | Pb | Mn |
| Concentration of | 58 | 19 | 18 | 5.3 | 3.2 | 1.4 |
| Composition (I) | Cu | Cd | Cr | Ni | As | |
| Concentration of | 0.96 | 0.32 | 0.21 | 0.14 | 0.12 |
The flying ash amount of the waste water is 360T/D (15T/H).
1.2 design of the quality and quantity of the incineration fly ash washing water
The water quality of the incineration fly ash washing water is designed as follows: unit (excluding pH): mg/L
| Item | pH | SS | Cu | Cr | Zn | Pb | Cd | SiO2 |
| Concentration of | 10.7 | 10 | 96 | 21 | 530 | 320 | 32 | 85 |
| Item | COD | Ca | Mg | SO4 | K | Na | Cl | TDS |
| Concentration of | 450 | 1400 | 960 | 3800 | 7500 | 5800 | 17000 | 37544 |
The amount of washing water of the incineration fly ash is 3600m3/D(150m3/H)。
2. Incineration fly ash washing system balance
The water balance of the incineration fly ash washing water recycling treatment system is shown in the water balance diagram of the incineration fly ash washing water recycling treatment embodiment in the attached figure 6.
3. Effect of treatment
3.1 incineration fly ash washing Effect
The main heavy metal content of the water-washing fly ash reaches the limit value of GB 30760-2014 technical Specification for cement kiln co-processing solid waste on the content of heavy metal in raw materials entering the kiln: cu is less than or equal to 65mg/kg, Cr is less than or equal to 98mg/kg, Zn is less than or equal to 361mg/kg, Pb is less than or equal to 67mg/kg, Cd is less than or equal to 1.0mg/kg, and Cl is less than or equal to 400 mg/kg.
3.2 incineration fly ash washing pretreatment effect
The incineration fly ash washing pretreatment effluent water quality unit (except pH) is as follows: mg/L
| Item | pH | SS | Cu | Cr | Zn | Pb | Cd | SiO2 |
| Concentration of | 7 | ≤0.1 | ≤0.1 | ≤0.1 | ≤0.1 | ≤0.1 | ≤0.1 | ≤5 |
| Item | COD | Ca | Mg | SO4 | K | Na | Cl | TDS |
| Concentration of | ≤50 | ≤100 | ≤200 | 1400 | 7500 | 5995 | 17000 | 32200 |
3.3 Material separation, electrodialysis concentration, reverse osmosis purification treatment effects
Material separation, electrodialysis concentration, reverse osmosis water purification unit: mg/L
3.4 salt separation effect of evaporative crystallization
Crystallizing and separating sodium chloride with the purity higher than 98.5 percent which meets the first-level standard requirement of refining industrial dry salt specified by GB/T5462-2015 Industrial salt at 85 ℃, and cooling and crystallizing at 40 ℃ to separate potassium chloride with the purity higher than 90.0 percent which meets the chemical index of the first-level product specified by GB/T7118-2008 Industrial Potassium chloride; TDS of the condensed water is less than or equal to 65 mg/L.
4. System main equipment
Claims (7)
1. The incineration fly ash washing water recycling treatment device is characterized by comprising an incineration fly ash washing system, a washing water pretreatment system, a membrane separation concentration system and an evaporative crystallization salt separation system; wherein, the incineration fly ash is pneumatically conveyed to an ash inlet of an incineration fly ash washing system, and the incineration fly ash is discharged from an ash outlet of the incineration fly ash washing system; the water outlet of the incineration fly ash washing system sends incineration fly ash washing water to a No. 1 water inlet of the washing pretreatment system, and a sludge outlet of the washing pretreatment system sends sludge cakes out; the water outlet of the washing pretreatment system sends the effluent of the washing pretreatment system to the water inlet of the membrane separation concentration system, the concentrated water outlet of the membrane separation concentration system sends the material separation concentrated water to the No. 2 water inlet of the washing pretreatment system, the water outlet of the membrane separation concentration system sends the effluent of the membrane separation concentration system to the liquid inlet of the evaporation crystallization salt separation system, the supplementary steam is connected to the steam inlet of the evaporation crystallization salt separation system, the reuse water sent from the reuse water outlet of the membrane separation concentration system and the condensed water sent from the condensed water outlet of the evaporation crystallization salt separation system are converged into the raw water to the water inlet of the incineration fly ash washing system; and a No. 1 salt outlet of the evaporative crystallization salt separation system sends out sodium chloride, and a No. 2 salt outlet of the evaporative crystallization salt separation system sends out potassium chloride (KCl).
2. The incineration fly ash washing resource treatment device as claimed in claim 1, wherein the incineration fly ash washing system structurally comprises an incineration fly ash storage bin, a pulping tank, a primary water washing tank, a primary disc filter, a secondary water tank, a secondary water washing tank, a secondary disc filter, a tertiary water tank, a tertiary water washing tank, a tertiary disc filter, a dryer, a washing fly ash storage bin, a fly ash washing water tank, an incineration fly ash quantitative feeder, a fly ash conveyor, a washing fly ash feeder, a primary suction pump, a fly ash washing water conveying pump, a secondary suction pump and a tertiary suction pump; the system comprises an incineration fly ash storage bin, a fly ash washing water tank, a fly ash conveying pump, a fly ash storage bin, a slurry outlet, a slurry inlet, a slurry tank, a slurry outlet, a slurry washing tank, a slurry outlet, a slurry washing tank and a slurry outlet, wherein the incineration fly ash is conveyed to the ash inlet of the incineration fly ash storage bin through the pneumatic conveying pump; the ash outlet of the first-level disc filter is connected to the ash inlet of the second-level water washing tank, the water outlet of the second-level water tank is connected to the water inlet of the second-level water washing tank, the slurry outlet of the second-level disc filter is connected to the slurry inlet of the second-level disc filter through the second-level suction pump, the ash outlet of the second-level disc filter is connected to the ash inlet of the third-level water washing tank, raw water is connected to the water inlet of the third-level water tank, the 1# water outlet of the third-level water tank is connected to the water inlet of the third-level water washing tank, the slurry outlet of the third-level water washing tank is connected to the slurry inlet of the third-level disc filter, the water outlet of the third-level disc filter is connected to the ash inlet of the dryer, the ash outlet of the dryer is connected to the ash inlet of the fly ash washing storage bin through the fly ash conveyor and the ash inlet of the fly ash washing storage bin, and the ash outlet of the fly ash washing bin delivers the washed fly ash through the fly ash washing feeder.
3. The incineration fly ash washing water resource treatment device as claimed in claim 1, wherein the washing water pretreatment system structurally comprises a fly ash washing water adjusting tank, a sulfuric acid and heavy metal removal agent adding device, a primary reaction tank, a primary sedimentation tank, a sodium carbonate and flocculant and coagulant aid adding device, a secondary reaction tank, a secondary sedimentation tank, an ozone catalytic oxidation device, an ozone generator, a mud-water separation membrane tank, a washing water pretreatment water outlet tank, a sludge concentration tank, a filter press, a filter pressing liquid tank, a lifting pump, a suction pump, a washing water pretreatment system water outlet delivery pump, a backwashing pump, a sludge pump and a filtrate pressure reflux pump; wherein the incineration fly ash washing water is connected to a No. 1 water inlet of a fly ash washing water regulating tank, the material separation concentrated water is connected to a No. 2 water inlet of the fly ash washing water regulating tank, a water outlet of the fly ash washing water regulating tank is connected with a water inlet of a first-stage reaction tank through a lift pump, a medicine outlet of a sulfuric acid and heavy metal removal agent adding device is connected to a medicine inlet of the first-stage reaction tank, a water outlet of the first-stage reaction tank is connected to a water inlet of a first-stage sedimentation tank, a water outlet of the first-stage sedimentation tank is connected to a water inlet of a second-stage reaction tank, a medicine outlet of a sodium carbonate, flocculating agent and coagulant aid adding device is connected to a medicine inlet of the second-stage reaction tank, a water outlet of the second-stage reaction tank is connected to a water inlet of a second-stage sedimentation tank, a water outlet of the second-stage sedimentation tank is connected to a water inlet of an ozone catalytic oxidation device, an air outlet of the ozone catalytic oxidation device is connected to a water inlet of an ozone separation membrane tank, the sludge outlet of the first-stage sedimentation tank, the sludge outlet of the second-stage sedimentation tank and the backwashing water outlet of the sludge-water separation membrane tank are all connected to the sludge inlet of the sludge concentration tank, the sludge outlet of the sludge concentration tank is connected with the sludge inlet of the filter press through a sludge pump, and the sludge outlet of the filter press sends out sludge cakes; a filter pressing liquid outlet of the filter press is connected to a water inlet of a filter pressing liquid pool, and a water outlet of the filter pressing liquid pool is connected to a No. 3 water inlet of a fly ash washing water regulating pool through a filter pressing liquid reflux pump; the water outlet of the mud-water separation membrane pool is connected with the water inlet of the washing pretreatment water outlet tank through a suction pump, the No. 1 water outlet of the washing pretreatment water outlet tank is connected with the backwashing water inlet of the mud-water separation membrane pool through a backwashing pump, and the No. 2 water outlet of the washing pretreatment water outlet tank is pumped out of the washing pretreatment system through the washing pretreatment system water outlet conveying pump.
4. The recycling device of incineration fly ash washing water according to claim 1, wherein the membrane separation concentration system comprises a scale inhibitor feeding device, a material separation membrane cartridge filter, a material separation membrane device, a material separation concentration water tank, a material separation water tank, an electrodialysis cartridge filter, an electrodialysis device, a membrane separation concentration system water outlet tank, an electrodialysis water tank, a reverse osmosis cartridge filter, a reverse osmosis device, a reuse water tank, a material separation high-pressure pump, an electrodialysis water supply pump, an evaporative crystallization liquid supply pump, a reverse osmosis booster pump, a reverse osmosis high-pressure pump, a reuse water delivery pump and a material separation concentration water delivery pump; wherein the water outlet of the washing pretreatment system is connected to the water inlet of the material separation membrane cartridge filter, the drug outlet of the scale inhibitor feeding device is also connected to the water inlet of the material separation membrane cartridge filter, the water outlet of the material separation membrane cartridge filter is connected with the water inlet of the material separation membrane device through a material separation high-pressure pump, the concentrated water outlet of the material separation membrane device is connected to the water inlet of the material separation concentrated water tank, and the water outlet of the material separation concentrated water tank is used for sending out material separation concentrated water through a material separation concentrated water conveying pump; the water outlet of the material separation membrane device is connected to the water inlet No. 1 of the material separation water production tank, the water outlet of the material separation water production tank is connected with the water inlet of the electrodialysis cartridge filter through an electrodialysis water supply pump, the water outlet of the electrodialysis cartridge filter is connected to the water inlet of the electrodialysis device, the water outlet of the electrodialysis device is connected to the water inlet of the electrodialysis water production tank, the water outlet of the electrodialysis water production tank is connected with the water inlet of the reverse osmosis cartridge filter through a reverse osmosis booster pump, the water outlet of the reverse osmosis cartridge filter is connected with the water inlet of the reverse osmosis device through a reverse osmosis high-pressure pump, the concentrated water outlet of the reverse osmosis device is connected to the water inlet No. 2 of the material separation water production tank, the water outlet of the reverse osmosis device is connected to the water inlet of the reuse water tank, and the water outlet of the reuse water tank is used for pumping out the reuse water through a reuse water conveying pump; and a concentrated water outlet of the electrodialysis device is connected to a water inlet of a water outlet tank of the membrane separation concentration system, and a water outlet of the water outlet tank of the membrane separation concentration system is fed out of the membrane separation concentration system through an evaporative crystallization liquid feed pump to discharge water.
5. The incineration fly ash washing water resource treatment device according to claim 1, characterized in that the evaporation, crystallization and salt separation system structurally comprises a primary preheater, a secondary preheater, a falling film evaporator, a falling film separator, a forced circulation evaporator, a forced circulation separator, a steam compressor, a condensed water tank, a thickener, a sodium salt centrifuge, a sodium salt weighing and packaging machine, a sodium salt mother liquor tank, a cooling and crystallization tank, a potassium salt centrifuge, a potassium salt weighing and packaging machine, a potassium salt mother liquor tank, a potassium salt mother liquor preheater, a falling film circulating pump, a falling film evaporation and material transfer pump, a condensed water pump, a forced circulating pump, a sodium salt discharge pump, a sodium salt mother liquor pump, a potassium salt discharge pump and a potassium salt mother liquor pump; wherein the water outlet of the membrane separation concentration system is connected to the feed liquid inlet of the first-stage preheater, the feed liquid outlet of the first-stage preheater is connected to the feed liquid inlet of the second-stage preheater, the feed liquid outlet of the second-stage preheater is connected to the feed liquid inlet No. 1 of the falling film evaporator, the feed liquid outlet of the falling film evaporator is connected to the feed liquid inlet No. 2 of the falling film separator, the feed liquid outlet No. 2 of the falling film separator is connected to the feed liquid inlet No. 1 of the forced circulation evaporator through the falling film evaporation material transfer pump, and the condensed water outlet of the second-stage preheater, a condensed water outlet of the falling film evaporator and a condensed water outlet of the forced circulation evaporator are both connected to a water inlet of a condensed water tank, a water outlet of the condensed water tank is connected to a water inlet of the primary preheater through a condensed water pump, and condensed water is sent out from a water outlet of the primary preheater; the feed liquid outlet of the forced circulation evaporator is connected to the feed liquid inlet No. 1 of the forced circulation separator, the feed liquid outlet of the forced circulation separator is connected to the feed liquid inlet No. 2 of the forced circulation evaporator through a forced circulation pump, the steam outlet of the falling film separator and the steam outlet of the forced circulation separator are both connected to the steam inlet of a steam compressor, and the steam outlet and the supplementary steam of the steam compressor are respectively connected to the steam inlet of a secondary preheater, the steam inlet of a falling film evaporator and the steam inlet of the forced circulation evaporator; a discharge port No. 1 of the forced circulation separator is connected to a feed port of the thickener through a sodium salt discharge pump, a discharge port of the thickener is connected to a feed port of a sodium salt centrifuge, a filtrate outlet of the sodium salt centrifuge is connected to a liquid inlet of a sodium salt mother liquor tank, a liquid outlet of the sodium salt mother liquor tank is connected to a feed liquid inlet No. 2 of the forced circulation separator through a sodium salt mother liquor pump, a salt outlet of the sodium salt centrifuge is connected to a salt inlet of a sodium salt weighing and packaging machine, and a salt outlet of the sodium salt weighing and packaging machine sends sodium chloride out; a discharge port No. 2 of the forced circulation separator is connected to a feed port of the cooling crystallization tank through a sylvite discharge pump, cooling water is fed into a cooling water inlet of the cooling crystallization tank, and a cooling water outlet of the cooling crystallization tank sends cooling water return water; the discharge port of the cooling crystallization tank is connected to the feed port of a potassium salt centrifuge, the filtrate outlet of the potassium salt centrifuge is connected to the liquid inlet of a potassium salt mother liquor tank, the liquid outlet of the potassium salt mother liquor tank is connected with the liquid inlet of a potassium salt mother liquor preheater through a potassium salt mother liquor pump, the liquid outlet of the potassium salt mother liquor preheater is connected to the feed liquid inlet of a forced circulation separator, the salt outlet of the potassium salt centrifuge is connected to the salt inlet of a potassium salt weighing and packaging machine, and the salt outlet of the potassium salt weighing and packaging machine sends out potassium chloride.
6. The recycling device for incineration fly ash washing water according to claim 1, wherein the sludge-water separation membrane in the washing water pretreatment system is made of PVDF (polyvinylidene fluoride), and the membrane pore diameter is less than or equal to 50 nm.
7. The recycling device of incineration fly ash washing water according to claim 1, wherein the material separation membrane in the membrane separation concentration system is a polyamide composite membrane.
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