CN217535720U - Waste incineration fly ash washing wastewater treatment system - Google Patents
Waste incineration fly ash washing wastewater treatment system Download PDFInfo
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- CN217535720U CN217535720U CN202221220251.7U CN202221220251U CN217535720U CN 217535720 U CN217535720 U CN 217535720U CN 202221220251 U CN202221220251 U CN 202221220251U CN 217535720 U CN217535720 U CN 217535720U
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Abstract
The utility model relates to a waste incineration flying dust washing effluent disposal system, including the raw water equalizing basin, remove heavy metal subsystem, first solid-liquid separation subsystem, first softening subsystem, second solid-liquid separation subsystem, second softening subsystem, third solid-liquid separation subsystem, milipore filter subsystem, first recovery pipeline, membrane separation subsystem, second recovery pipeline, pH adjusting barrel and evaporation crystallization divide the salt subsystem. The utility model thoroughly removes the residual calcium ions by two-stage softening, and the comprehensive energy consumption is lower; COD and SS are removed by the ultrafiltration membrane system, the generated ultrafiltration concentrated solution is recycled to the raw water regulating reservoir, the generated ultrafiltration permeating solution enters the membrane separation subsystem to realize effective separation of sulfate and chloride, the concentration of the sulfate in the effluent is lower, and the separation membrane concentrated solution enters the first softening subsystem for cyclic utilization, so that the purposes of removing the sulfate in the fly ash washing wastewater and reducing the treatment cost of calcium ions are achieved.
Description
Technical Field
The utility model belongs to the technical field of high salt waste water treatment, concretely relates to waste incineration flying dust washing effluent disposal system.
Background
The fly ash (fly ash for short) from domestic garbage incineration is prepared from fly ash obtained from flue gas collection system of garbage incineration power plant, and comprises fluidized bed fly ash and grate furnace fly ash, wherein the fly ash contains CaO and SiO as main components 2 、Na 2 O、K 2 O、Fe 2 O 3 、Al 2 O 3 And MgO, wherein the mass fraction of CaO is the highest and is 20.4-37.9%; the main hazardous substances are heavy metals (Zn, pb, cu, cr, cd, ni, hg and the like) and dioxin organic compounds, the mass fraction of chlorine in the incineration fly ash is the highest and can exceed 25%, wherein the soluble chlorine accounts for 40.6-83.9% of the total chlorine.
The fly ash washing wastewater is derived from the fly ash washing wastewater generated by the washing process in the fly ash resource utilization process, is high-salinity wastewater, and mainly comprises Cl - 、Na + 、K + 、Ca 2+ 、SO 4 2- And Pb 2+ 、Zn 2+ 、Cu 2+ 、Cd 2+ 、Cr 6+ Of an equiheavy metal, wherein Cl - 、Na + 、K + Can be prepared into sodium chloride and chlorine by evaporative crystallization salt separation technologyPotassium chloride product, in order to ensure the quality of sodium chloride and potassium chloride product and the stability of evaporative crystallization system, ca in the fly ash washing wastewater needs to be removed 2+ 、SO 4 2- And Pb 2+ 、Zn 2+ 、Cu 2+ 、Cd 2+ 、Cr 6+ And (3) the heavy metal elements are equal.
At present, the method for removing heavy metals in high-salinity wastewater mainly adds sodium sulfide or heavy metal chelating agent, and can effectively remove heavy metals such as lead and the like.
At present, the method for removing calcium ions in high-salinity wastewater mainly comprises a sodium carbonate calcium removal method, a carbon dioxide calcium removal method and a sodium sulfate calcium removal method. The calcium removal method of sodium carbonate has the best effect, the removal rate of calcium ions can be more than 99%, but the sodium carbonate medicament is expensive and the treatment cost is high; the carbon dioxide calcium removal method has low removal efficiency, needs to be combined with a sodium carbonate calcium removal method for use, and has higher treatment cost. The sodium sulfate calcium removal method is difficult to remove calcium ions in high-salinity wastewater completely, needs to be combined with a sodium carbonate calcium removal method for use, is relatively low in treatment cost, but introduces a large amount of sulfate into the wastewater, and seriously influences the quality of sodium chloride and potassium chloride products in an evaporative crystallization system. Under the condition that the sulfate in the fly ash washing wastewater is not removed, the sulfate can be continuously enriched in an evaporative crystallization system, and the quality of sodium chloride and potassium chloride products can also be influenced.
Therefore, there is a need in the art to provide a waste incineration fly ash washing wastewater treatment system to reduce the treatment cost of calcium ions in the wastewater washing liquid.
SUMMERY OF THE UTILITY MODEL
Based on the above-mentioned shortcomings and deficiencies in the prior art, it is an object of the present invention to at least solve one or more of the above-mentioned problems in the prior art, in other words, to provide a waste incineration fly ash washing wastewater treatment system that satisfies one or more of the above-mentioned needs.
In order to achieve the purpose of the utility model, the utility model adopts the following technical scheme:
a waste incineration fly ash washing wastewater treatment system comprises:
the raw water regulating tank is used for collecting the fly ash washing wastewater;
the heavy metal removal subsystem is used for removing heavy metals from the fly ash washing wastewater output by the raw water regulating tank to obtain a mud-water mixture;
the first solid-liquid separation subsystem is used for carrying out solid-liquid separation on the mud-water mixture output by the heavy metal removal subsystem so as to generate heavy metal removal water and heavy metal sludge;
the first softening subsystem is used for removing calcium from the heavy water output by the first solid-liquid separation subsystem to obtain a mud-water mixture;
the second solid-liquid separation subsystem is used for carrying out solid-liquid separation on the muddy water mixture output by the first softening subsystem so as to generate softened water and calcium sulfate sludge;
the second softening subsystem is used for removing residual calcium ions from the softened water output by the second solid-liquid separation subsystem to obtain a mud-water mixture;
the third solid-liquid separation subsystem is used for carrying out solid-liquid separation on the mud-water mixture output by the second softening subsystem to generate deep softened water and calcium carbonate sludge;
the ultrafiltration membrane subsystem is used for removing COD and SS in the deep softened water output by the third solid-liquid separation subsystem so as to generate an ultrafiltration concentrated solution and an ultrafiltration permeating solution;
the first recovery conveying pipeline is used for conveying the ultrafiltration concentrated solution output by the ultrafiltration membrane subsystem to the raw water regulating reservoir;
the membrane separation subsystem is used for separating sulfate and chloride from the ultrafiltration permeate output by the ultrafiltration membrane subsystem, concentrating the sulfate and then feeding the sulfate into a separation membrane concentrated solution, and feeding the chloride into a separation membrane permeate;
the second recovery conveying pipeline is used for conveying the membrane concentrated solution output by the membrane separation subsystem to the first softening subsystem;
the pH adjusting barrel is used for adjusting the pH of the separation membrane permeation liquid output by the membrane separation subsystem to generate reclaimed water;
and the evaporative crystallization salt separation subsystem is used for carrying out evaporative crystallization salt separation on the reclaimed water output by the pH adjusting barrel to generate sodium chloride and potassium chloride.
Preferably, the calcium sulfate sludge output by the second solid-liquid separation subsystem is connected to a gypsum production line through a first conveyor.
Preferably, the calcium carbonate sludge output by the third solid-liquid separation subsystem is connected to the fly ash washing system through a second conveyor.
As a preferred scheme, the raw water adjusting tank is connected with a fly ash washing wastewater source through a first pumping pipeline, the raw water adjusting tank is connected with a heavy metal removal subsystem through a second pumping pipeline, the heavy metal removal subsystem is connected with a first solid-liquid separation subsystem through a third pumping pipeline, a heavy water removal outlet of the first solid-liquid separation subsystem is connected with a first softening subsystem through a fourth pumping pipeline, the first softening subsystem is connected with a second solid-liquid separation subsystem through a fifth pumping pipeline, a softened water outlet of the second solid-liquid separation subsystem is connected with a second softening subsystem through a sixth pumping pipeline, the second softening subsystem is connected with a third solid-liquid separation subsystem through a seventh pumping pipeline, a softened water outlet of the third solid-liquid separation subsystem is connected with an ultrafiltration membrane subsystem through an eighth pumping pipeline, an ultrafiltration permeate outlet of the ultrafiltration membrane subsystem is connected with a membrane separation subsystem through a ninth pumping pipeline, a separation membrane permeate outlet of the membrane separation subsystem is connected with a pH adjusting barrel through a tenth pumping pipeline, and the pH adjusting barrel is connected with an evaporation crystallization salt separation subsystem through an eleventh pumping pipeline.
As the preferred scheme, all the pumping pipelines for pumping the mud-water mixture adopt screw sludge pumps or sludge diaphragm pumps, and the other pumping pipelines adopt self-priming pumps.
Preferably, the first solid-liquid separation subsystem, the second solid-liquid separation subsystem and the third solid-liquid separation subsystem are plate-and-frame filter presses, belt filter presses or horizontal screw centrifuges.
Preferably, the operating pressure of the ultrafiltration membrane subsystem is less than 2bar.
Preferably, the ultrafiltration membrane of the ultrafiltration membrane subsystem is a tubular membrane or a plate-type membrane.
Preferably, the operating pressure of the membrane separation subsystem is 25-30 bar.
Preferably, the separation membrane of the membrane separation subsystem is a wound organic polyamide membrane.
Compared with the prior art, the utility model, beneficial effect is:
(1) The utility model utilizes the first softening subsystem to remove most calcium ions and then utilizes the second softening subsystem to remove the rest calcium ions, thus reducing the treatment cost by more than 50 percent compared with the treatment cost of calcium removal by pure sodium carbonate and having lower comprehensive energy consumption;
(2) The utility model discloses utilize the milipore filter subsystem to get rid of COD and SS, the hyperfiltration concentrate retrieval and utilization of production is to raw water equalizing basin, the ultrafiltration permeate liquid of production gets into the membrane separation subsystem and realizes the effective separation of sulfate and chlorine salt, makes the sulfate concentration of outlet water lower, more is favorable to evaporating crystallization salt separation system steady operation, and the separation membrane concentrate gets into the first subsystem cyclic utilization that softens to reach the mesh of getting rid of flying dust washing waste water sulfate and reducing calcium ion treatment cost;
(3) The calcium sulfate sludge of the utility model can be used for producing gypsum products, and the calcium ions in the fly ash washing wastewater are recycled; and (4) allowing the calcium carbonate sludge to enter a fly ash washing system to obtain washed finished product ash.
Drawings
FIG. 1 is a schematic view of a waste incineration fly ash washing wastewater treatment system according to embodiment 1 of the present invention.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention, the following description will explain embodiments of the present invention with reference to the accompanying drawings. It is obvious that the drawings in the following description are only examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be obtained from these drawings without inventive effort.
Example 1:
as shown in fig. 1, the waste incineration fly ash washing wastewater treatment system of the embodiment includes: the system comprises a raw water adjusting tank 1, a heavy metal removing subsystem 2, a first solid-liquid separation subsystem 3, a first softening subsystem 4, a second solid-liquid separation subsystem 5, a second softening subsystem 6, a third solid-liquid separation subsystem 7, an ultrafiltration membrane subsystem 8, a first recovery conveying pipeline 9, a membrane separation subsystem 10, a second recovery conveying pipeline 11, a pH adjusting barrel 12 and an evaporation crystallization salt separation subsystem 13.
Specifically, the raw water adjusting tank 1 of the present embodiment is used for collecting the fly ash washing wastewater, and is of an underground type, a semi-underground type or an overground type, and is one of a concrete structure, Q235 or SUS 316L; in addition, the volume of the raw water adjusting tank meets the liquid storage amount of continuous operation for 15 h.
In addition, the raw water adjusting tank 1 is connected with the fly ash washing wastewater source 0 through a first pumping pipeline D1 so as to treat the waste incineration fly ash wastewater.
The heavy metal removal subsystem 2 of this embodiment is used for removing heavy metals from the fly ash washing wastewater output from the raw water regulating reservoir 1 to obtain a sludge-water mixture. Specifically, the heavy metal removal subsystem 2 is connected with the raw water regulating reservoir 1 through a second pumping pipeline D2. The specific architecture of the heavy metal removal subsystem can refer to the prior art, and is not described herein.
The first solid-liquid separation subsystem 3 of the embodiment is used for performing solid-liquid separation on the mud-water mixture output by the heavy metal removal subsystem 2 to generate heavy metal removal water and heavy metal sludge. Specifically, the first solid-liquid separation subsystem 3 is connected with the heavy metal removal subsystem 2 through a third pumping pipeline D3.
The first softening subsystem 4 of this embodiment is used for removing calcium from the heavy water output by the first solid-liquid separation subsystem 3 to obtain a mud-water mixture. Specifically, the first softening subsystem 4 is connected with the heavy water removal outlet of the first solid-liquid separation subsystem 3 through a fourth pumping pipeline D4.
The specific architecture of the first softening subsystem can refer to the prior art, and is not described herein.
The second solid-liquid separation subsystem 5 of this embodiment is used for performing solid-liquid separation on the sludge-water mixture output by the first softening subsystem 4 to generate softened water and calcium sulfate sludge. Specifically, the second solid-liquid separation subsystem 5 is connected with the first softening subsystem 4 through a fifth pumping conduit D5.
The second softening subsystem 6 of this embodiment is configured to remove residual calcium ions from the softened water output by the second solid-liquid separation subsystem 5, so as to obtain a mud-water mixture. Specifically, the second softening subsystem 6 is connected with the softened water outlet of the second solid-liquid separation subsystem 5 through a sixth pumping pipeline D6.
The specific structure of the second softening subsystem can refer to the prior art, and is not described herein.
The third solid-liquid separation subsystem 7 of the embodiment is used for carrying out solid-liquid separation on the sludge-water mixture output by the second softening subsystem 6 to generate deeply softened water and calcium carbonate sludge. In particular, the third solid-liquid separation subsystem 7 is connected to the second softening subsystem 6 by a seventh pumping conduit D7.
The ultrafiltration membrane subsystem 8 of the present embodiment is used for removing COD and SS from the deeply softened water output from the third solid-liquid separation subsystem 7 to produce an ultrafiltration concentrate and an ultrafiltration permeate. Specifically, the ultrafiltration membrane subsystem 8 is connected with the softened water outlet of the third solid-liquid separation subsystem 7 through an eighth pumping pipeline D8.
The operation pressure of the ultrafiltration membrane subsystem is less than 2bar, the ultrafiltration membrane of the ultrafiltration membrane subsystem is a tubular membrane or a plate-type membrane, and the specific framework of the ultrafiltration membrane subsystem can refer to the prior art and is not described herein.
The first recovery conveying pipeline 9 of this embodiment is used for conveying the ultrafiltration concentrated solution output by the ultrafiltration membrane subsystem 8 to the raw water regulation tank.
The membrane separation subsystem 10 of this embodiment is used to separate sulfate from chloride in the ultrafiltration permeate outputted from the ultrafiltration membrane subsystem 8, concentrate the sulfate into the separation membrane concentrate, and introduce the chloride into the separation membrane permeate. Specifically, the membrane separation subsystem 10 is connected to the ultrafiltration permeate outlet of the ultrafiltration membrane subsystem 8 through a ninth pumping conduit D9.
Wherein the operating pressure of the membrane separation subsystem is 25-30 bar, and the separation membrane of the membrane separation subsystem is a spiral organic polyamide membrane; the specific structure of the membrane separation subsystem can be referred to the prior art and will not be described herein.
The second recycle transfer line 11 of the present embodiment is used for transferring the membrane concentrate outputted from the membrane separation subsystem 10 to the first softening subsystem 4.
The pH adjusting tank 12 of the present embodiment is used to adjust the pH of the separation membrane permeate outputted from the membrane separation subsystem 10 to generate recycled water. Specifically, the pH adjusting barrel 12 is connected to the separation membrane permeate outlet of the membrane separation subsystem 10 through a tenth pumping conduit D10.
The evaporative crystallization salt separation subsystem 13 of the embodiment is used for carrying out evaporative crystallization salt separation on the reclaimed water output by the pH adjusting barrel 12 to generate sodium chloride and potassium chloride. Specifically, the evaporative crystallization salt separation subsystem 13 is connected with the pH adjusting barrel 12 through an eleventh pumping pipe D11.
The specific structure of the evaporative crystallization salt separation subsystem can refer to the prior art, and is not described herein.
In addition, the calcium sulfate sludge output from the second solid-liquid separation subsystem 5 of the present embodiment is connected to the gypsum production line S by the first conveyor H1.
The calcium carbonate sludge output from the third solid-liquid separation subsystem 7 of this embodiment is connected to the fly ash washing system X by the second conveyor H2.
The conveyor is one of a belt conveyor and a scraper conveyor, the belt is made of rubber, and the scraper is made of one of SUS316L or 2205 dual-phase steel.
All pumping pipelines for pumping the mud-water mixture adopt screw sludge pumps or sludge diaphragm pumps, and the other pumping pipelines adopt self-sucking pumps; the method can also be realized by adopting self-flowing, and can be specifically determined according to the actual installation environment. In addition, the pipeline is made of Q235, SUS316L or 2205 duplex stainless steel, so that corrosion resistance is realized.
The first solid-liquid separation subsystem 3, the second solid-liquid separation subsystem 5 and the third solid-liquid separation subsystem 7 of the embodiment are plate-and-frame filter presses, belt filter presses or horizontal screw centrifuges, and can be determined specifically according to practical application scenarios.
The processing procedure of the waste incineration fly ash washing wastewater treatment system of the embodiment includes:
(1) The fly ash washing wastewater enters a raw water adjusting tank, and the raw water adjusting tank is used for storing and homogenizing the fly ash washing wastewater;
specifically, the fly ash washing wastewater (washing filtrate for short) in the embodiment contains 8 to 15% of chloride ions, 1 to 3% of sodium ions, 1 to 3% of potassium ions and 2 to 4% of calcium ions;
(2) The fly ash washing wastewater of the raw water regulating tank enters a heavy metal removing subsystem to remove heavy metals such as lead, zinc, copper, cadmium, chromium and the like in the fly ash washing wastewater to generate a first muddy water mixture;
the heavy metal removal subsystem of the embodiment comprises a dosing unit, a coagulation reaction unit, a flocculation reaction unit and a precipitation unit, wherein the treatment process of the fly ash washing wastewater by the heavy metal removal system sequentially comprises dosing, coagulation reaction, flocculation reaction and precipitation;
wherein the step of adding the medicine is adding a weight removing agent, and the weight removing agent is sodium sulfide or a heavy metal chelating agent;
the coagulant for coagulation reaction is PAC or PFS;
the flocculating agent of the flocculation reaction is anionic PAM or nonionic PAM;
the sedimentation tank for sedimentation is semi-underground or overground, a concrete structure, Q235 or SUS316L is adopted, and the volume of the sedimentation tank needs to meet the sedimentation time of more than 15 h.
(3) The first mud-water mixture enters a first solid-liquid separation subsystem to generate heavy water and heavy metal-removed sludge;
the removal rate of heavy metals such as lead, zinc, copper, cadmium, chromium and the like in the heavy metal removal water is more than 90 percent, and the water content of the heavy metal sludge is 50-60 percent.
(4) Heavy metal sludge enters a hazardous waste temporary storage;
wherein, heavy metal mud adopts ton bag packing, and fourth conveying system transports for fork truck.
(5) The heavy water is removed and enters a first softening subsystem, most calcium ions are removed, and a mud-water mixture II is generated;
specifically, the softening agent adopted by the first softening system is sodium sulfate.
(6) The mud-water mixture II enters a second solid-liquid separation subsystem to generate softened water and calcium sulfate sludge;
wherein the removal rate of calcium ions in the softened water is more than 90 percent, and the water content of the calcium sulfate sludge is 30-35 percent.
(7) Calcium sulfate sludge enters a gypsum production line;
(8) The softened water enters a second softening subsystem to remove all residual calcium ions to generate a muddy water mixture III;
specifically, the softener used by the second softening subsystem is sodium carbonate.
(9) The mud-water mixture III enters a third solid-liquid separation subsystem to generate deeply softened water and calcium carbonate sludge;
wherein the removal rate of calcium ions in the deeply softened water is more than 99 percent, and the water content of the calcium carbonate sludge is 30-35 percent.
(10) The calcium carbonate sludge enters a fly ash washing system and finally enters washed finished product ash for being used as a raw material for building materials.
(11) The deeply softened water enters an ultrafiltration membrane subsystem to remove COD and SS in the deeply softened water, and an ultrafiltration concentrated solution and an ultrafiltration permeate are generated;
wherein the operating pressure of the ultrafiltration membrane subsystem is less than 2bar, the ultrafiltration membrane is a tubular membrane or a plate-type membrane, the concentration rate of the ultrafiltration concentrated solution to the inlet water is more than 10 times, the interception efficiency of the ultrafiltration permeate to COD is 30-50%, and the interception efficiency to SS is more than 99%.
(12) Recycling the ultrafiltration concentrated solution to a raw water regulating reservoir;
(13) The ultrafiltration permeate enters a membrane separation subsystem to realize the separation of sulfate and chloride, the sulfate is concentrated and enters a separation membrane concentrated solution, and the chloride enters a separation membrane permeate;
wherein the operating pressure of the membrane separation system is 25-30 bar, the separation membrane is a roll type organic polyamide membrane, the concentration rate of the concentrated solution of the separation membrane to the inlet water is not less than 10 times, the interception efficiency of the permeate of the separation membrane to sulfate is 95-98%, and the interception efficiency to chloride is 20-30%.
(14) Recycling the concentrated solution of the separation membrane to the first softening subsystem, and removing calcium ions by using sulfate;
(15) The separation membrane permeate enters a pH adjusting barrel for adjusting pH to generate reclaimed water;
wherein the pH value of the reclaimed water is 7-8.
(16) The reclaimed water enters an evaporation crystallization salt separation subsystem to realize sodium and potassium salt separation and is used for preparing sodium chloride and potassium chloride products.
The waste incineration fly ash washing wastewater treatment system of this embodiment can realize that the calcium ion gets rid of the cost and saves more than 50%, and the sulfate content that water treatment goes out water (promptly the normal water) and compare in fly ash washing wastewater is lower, is more favorable to the steady operation of evaporation crystallization system, and calcium sulfate mud can be used to the gypsum production line simultaneously, forms the gypsum product, has realized calcium ion resourceization in the fly ash washing liquid.
The foregoing has been a detailed description of the preferred embodiments and principles of the present invention, and it will be apparent to those skilled in the art that variations may be made in the specific embodiments based on the concepts of the present invention, and such variations are considered as within the scope of the present invention.
Claims (10)
1. The utility model provides a waste incineration fly ash washing effluent disposal system which characterized in that includes:
the raw water regulating tank is used for collecting the fly ash washing wastewater;
the heavy metal removal subsystem is used for removing heavy metals from the fly ash washing wastewater output by the raw water regulating tank to obtain a mud-water mixture;
the first solid-liquid separation subsystem is used for carrying out solid-liquid separation on the mud-water mixture output by the heavy metal removal subsystem so as to generate heavy metal removal water and heavy metal sludge;
the first softening subsystem is used for removing calcium from the heavy water output by the first solid-liquid separation subsystem to obtain a mud-water mixture;
the second solid-liquid separation subsystem is used for carrying out solid-liquid separation on the muddy water mixture output by the first softening subsystem so as to generate softened water and calcium sulfate sludge;
the second softening subsystem is used for removing residual calcium ions from the softened water output by the second solid-liquid separation subsystem to obtain a mud-water mixture;
the third solid-liquid separation subsystem is used for carrying out solid-liquid separation on the mud-water mixture output by the second softening subsystem to generate deep softened water and calcium carbonate sludge;
the ultrafiltration membrane subsystem is used for removing COD and SS in the deep softened water output by the third solid-liquid separation subsystem so as to generate an ultrafiltration concentrated solution and an ultrafiltration permeating solution;
the first recovery conveying pipeline is used for conveying the ultrafiltration concentrated solution output by the ultrafiltration membrane subsystem to the raw water regulating reservoir;
the membrane separation subsystem is used for separating sulfate and chloride from the ultrafiltration permeate output by the ultrafiltration membrane subsystem, concentrating the sulfate and feeding the concentrated solution into a separation membrane, and feeding the chloride into the separation membrane permeate;
the second recovery conveying pipeline is used for conveying the membrane concentrated solution output by the membrane separation subsystem to the first softening subsystem;
the pH adjusting barrel is used for adjusting the pH of the separation membrane permeation liquid output by the membrane separation subsystem to generate reclaimed water;
and the evaporative crystallization salt separation subsystem is used for carrying out evaporative crystallization salt separation on the reclaimed water output by the pH adjusting barrel to generate sodium chloride and potassium chloride.
2. The waste incineration fly ash washing wastewater treatment system according to claim 1, wherein the calcium sulfate sludge output by the second solid-liquid separation subsystem is connected to a gypsum production line through a first conveyor.
3. The waste incineration fly ash washing wastewater treatment system according to claim 1, wherein the calcium carbonate sludge output by the third solid-liquid separation subsystem is connected to the fly ash washing system through a second conveyor.
4. The waste incineration fly ash washing wastewater treatment system as set forth in claim 1, wherein the raw water conditioning tank is connected to a fly ash washing wastewater source through a first pumping pipeline, the raw water conditioning tank is connected to the heavy metal removal subsystem through a second pumping pipeline, the heavy metal removal subsystem is connected to the first solid-liquid separation subsystem through a third pumping pipeline, the heavy water removal outlet of the first solid-liquid separation subsystem is connected to the first softening subsystem through a fourth pumping pipeline, the first softening subsystem is connected to the second solid-liquid separation subsystem through a fifth pumping pipeline, the softened water outlet of the second solid-liquid separation subsystem is connected to the second softening subsystem through a sixth pumping pipeline, the second softening subsystem is connected to the third solid-liquid separation subsystem through a seventh pumping pipeline, the softened water outlet of the third solid-liquid separation subsystem is connected to the ultrafiltration membrane subsystem through an eighth pumping pipeline, the ultrafiltration permeate outlet of the ultrafiltration membrane subsystem is connected to the membrane separation subsystem through a ninth pumping pipeline, the separation membrane permeate outlet of the membrane separation subsystem is connected to the pH adjustment barrel through a tenth pumping pipeline, and the pH adjustment barrel are connected to the solid-liquid evaporation subsystem through a ninth pumping pipeline.
5. The waste incineration fly ash washing wastewater treatment system according to claim 4, wherein all pumping pipelines for pumping the sludge-water mixture adopt a screw sludge pump or a sludge diaphragm pump, and the other pumping pipelines adopt self-sucking pumps.
6. The waste incineration fly ash washing wastewater treatment system according to claim 1, wherein the first solid-liquid separation subsystem, the second solid-liquid separation subsystem and the third solid-liquid separation subsystem are plate-and-frame filter presses, belt filter presses or horizontal decanter centrifuges.
7. The waste incineration fly ash washing wastewater treatment system of claim 1, wherein the operating pressure of the ultrafiltration membrane subsystem is less than 2bar.
8. The system for treating waste incineration fly ash washing wastewater as claimed in claim 1 or 7, wherein the ultrafiltration membrane of the ultrafiltration membrane subsystem is a tubular membrane or a plate-type membrane.
9. The system for treating waste incineration fly ash washing wastewater as claimed in claim 1, wherein the operating pressure of the membrane separation subsystem is 25-30 bar.
10. The system for treating waste incineration fly ash washing wastewater as claimed in claim 1 or 9, wherein the separation membrane of the membrane separation subsystem is a rolled organic polyamide membrane.
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