CN216095508U - Resource treatment system for salt production by washing waste incineration fly ash based on seed crystal method - Google Patents

Resource treatment system for salt production by washing waste incineration fly ash based on seed crystal method Download PDF

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CN216095508U
CN216095508U CN202120785000.2U CN202120785000U CN216095508U CN 216095508 U CN216095508 U CN 216095508U CN 202120785000 U CN202120785000 U CN 202120785000U CN 216095508 U CN216095508 U CN 216095508U
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inlet
fly ash
liquid
unit
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李忠锋
孔令然
赵小楠
庞新辉
蔡佳龙
刘璐璐
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Bj Zkgr Technology Co ltd
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Bj Zkgr Technology Co ltd
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Abstract

The utility model discloses a resource treatment system for waste incineration fly ash washing salt making based on a seed crystal method, which comprises a fly ash pulping unit (1), a fly ash elution unit (2), a washing liquid purification unit (3), an evaporation crystallization unit (4) and a drying unit (5). The system adopts multi-stage countercurrent and alkaline water washing technologies in the fly ash elution unit, so that the water consumption is low, no dust is raised, the dechlorination effect is good, and the heavy metal leaching rate is low; through organically combining multi-stage countercurrent elution, water washing liquid purification and gypsum crystal seed method evaporation crystallization, the problems of high consumption of water and calcium and magnesium ion remover, easy scaling in the evaporation crystallization process, poor quality of crystallized salt and the like are solved.

Description

Resource treatment system for salt production by washing waste incineration fly ash based on seed crystal method
Technical Field
The utility model relates to a treatment system of waste incineration fly ash, in particular to a resource treatment system for salt production by washing the waste incineration fly ash based on a seed crystal method, and belongs to the field of retreatment and utilization of the waste incineration fly ash.
Background
The fly ash is a powdery substance which is collected in a flue gas pipeline, a flue gas purification device, a separator, a dust remover device and the like in the waste incineration process and has light volume weight and small particle size. The fly ash is listed as solid hazardous waste (code HW18) by the nation because the fly ash is rich in heavy metal inorganic harmful substances and high-concentration dioxin organic carcinogens.
The current Chinese main waste incineration fly ash disposal technology comprises the following steps: cement curing, melt sintering curing, chemical agent stabilization and cement kiln co-processing. The fly ash is subjected to landfill treatment after solidification or stabilization treatment, a large amount of land resources are occupied by the landfill treatment, underground water and soil are easily polluted by landfill leachate, and dioxin, heavy metals and salts which are not removed have long-term potential threat to the environment. The cement kiln cooperative treatment technology is a new treatment means in the development of the fly ash treatment technology, and can realize harmless, reduced and recycled treatment of the household garbage incineration fly ash.
Before the fly ash enters the kiln, dechlorination pretreatment is carried out, otherwise, a large amount of chloride ions in the fly ash can influence the quality of clinker and cement, and the kiln is easy to crust. The water washing pretreatment is a main method for removing chloride ions in the fly ash, and soluble substances (potassium, sodium and chloride ions) in the fly ash can be transferred into water washing liquid. The fly ash water washing liquid contains about 6 wt% -15 wt% of potassium and sodium salts, and Chinese potassium salt resources are relatively scarce, and potassium salts and sodium salts are prepared from the fly ash water washing liquid by an evaporative crystallization technology, so that the vacancy of the Chinese potassium salts is relieved.
The Chinese invention patent (CN 108607870A) discloses a garbage fly ash treatment system and a treatment process, which comprises a fly ash washing system and a wastewater treatment system, wherein wastewater is subjected to heavy metal removal, activated carbon decontamination treatment and calcium ion removal in sequence, and finally the wastewater is utilized; the waste water storage tank is connected with the evaporator, and the evaporator is connected with the centrifugal machine and the reaction water storage tank, so that the salt production by evaporative crystallization of waste water is realized. The method can remove chloride ions in the fly ash, solves the negative influence of chloride on the cooperative treatment process of the cement kiln, generates certain economic benefit and reduces high cost caused by incomplete fly ash treatment.
Although the pollution problem of fly ash is solved in the prior art, the evaporation crystallization process is simple, salt in feed liquid is separated into crystals in the evaporation process and is precipitated and attached to the surface of an evaporator, so that uneven heat transfer and low heat transfer efficiency are caused, energy waste is caused, regular shutdown and cleaning are required, and the production efficiency is seriously influenced.
SUMMERY OF THE UTILITY MODEL
One of the purposes of the utility model is to provide a treatment system for realizing a resource treatment method for preparing salt by washing waste incineration fly ash based on a seed crystal method;
the above object of the present invention is achieved by the following technical solutions:
a special system for realizing a resource treatment method for producing salt by washing waste incineration fly ash based on a seed crystal method comprises a fly ash pulping unit, a fly ash eluting unit, a washing liquid purifying unit, an evaporative crystallization unit and a drying unit; the fly ash washing unit is provided with a fly ash slurry inlet, a solid-phase product outlet, a liquid-phase product outlet and a pulping water inlet; the washing liquid purification unit is provided with a liquid phase inlet, a liquid phase outlet and a solid phase outlet; the evaporative crystallization unit is provided with an evaporative raw material liquid inlet, a non-crystallization mother liquid outlet and a condensed water outlet;
the device comprises a fly ash pulping unit, a fly ash washing unit, a drying unit, a water washing liquid purifying unit, a fly ash pulp outlet of the fly ash pulping unit, a fly ash pulp inlet of the fly ash washing unit, a solid-phase product outlet of the fly ash washing unit, a liquid-phase inlet of the water washing liquid purifying unit, a liquid-phase outlet of the water washing liquid purifying unit, an evaporation raw material liquid inlet of the evaporation crystallization unit, a solid-phase outlet of the water washing liquid purifying unit, an inlet of the drying unit, an outlet of non-crystallization mother liquid of the evaporation crystallization unit, a liquid-phase inlet of the water washing liquid purifying unit and a condensed water outlet of the evaporation crystallization unit, wherein the fly ash pulp inlet of the fly ash washing unit is connected with the condensed water outlet of the fly ash washing unit.
As a preferred embodiment of the present invention, the fly ash pulping unit may include a fly ash pretreatment device (i.e., a crushing device), a fly ash buffer device, a fly ash metering device, a water metering device, a pulping apparatus; the outlet of the fly ash pre-treatment device (crushing device) is connected with the inlet of the fly ash caching device, the outlet of the fly ash caching device is connected with the inlet of the fly ash metering device, and the outlet of the fly ash metering device and the outlet of the water metering device are both connected with the inlet of the pulping equipment.
As a preferred embodiment of the present invention, the fly ash elution unit comprises a primary elution separation device, a secondary elution separation device and a tertiary elution separation device; wherein the first-stage elution separation device is provided with a fly ash slurry inlet, a water washing liquid outlet and a solid phase outlet; the second-stage elution separation device is provided with a slurry inlet, a solid-phase outlet and a liquid-phase inlet; the three-stage elution separation device is provided with a slurry inlet, a solid phase outlet and a liquid phase outlet; wherein, one-level elution separator's wash solution export with wash solution purification unit's wash solution entry link to each other, one-level elution separator's solid phase export with second grade elution separator's thick liquid entry link to each other, second grade elution separator's liquid phase export with the entry of the process water metering device of slurrying unit link to each other, second grade elution separator's solid phase export with third grade elution separator's thick liquid entry link to each other, third grade elution separator's liquid phase export with second grade elution separator's liquid phase entry link to each other, third grade elution separator's solid phase export the entry of drying unit links to each other.
As a preferred embodiment of the present invention, the washing liquid purification unit may include a heavy metal removal device, a concentration and precipitation device, a multi-stage filtration device, a desliming device, and a pH adjustment device; the heavy metal removal device is provided with a washing liquid inlet, a liquid phase outlet and a sludge outlet; the concentration and precipitation device is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the multistage filtering device is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the pH value adjusting device is provided with a liquid phase inlet and a liquid phase outlet; the desliming device is provided with a sludge inlet, a solid phase outlet and a liquid phase outlet; wherein a washing liquid inlet of the heavy metal removal device is connected with a liquid phase outlet of a first-stage elution separation device of the fly ash elution unit, a liquid phase outlet of the heavy metal removal device is connected with a liquid phase inlet of the concentration and precipitation device, a liquid phase outlet of the concentration and precipitation device is connected with a liquid phase inlet of the multi-stage filtration device, and a liquid phase outlet of the multi-stage filtration device is connected with a liquid phase inlet of the pH value adjustment device; the sludge outlet of the heavy metal removal device, the sludge outlet of the concentration and precipitation device and the sludge outlet of the multistage filtering device are all connected with the sludge inlet of the desliming device; and a solid phase outlet of the desliming device is connected with an inlet of the drying unit, a liquid phase outlet of the desliming device is connected with a liquid phase inlet of the heavy metal removal device, and a liquid phase outlet of the pH value adjusting device is connected with an inlet of the evaporative crystallization unit.
As a preferred embodiment of the utility model, the evaporative crystallization unit comprises a multi-stage preheater, a forced circulation heat exchanger, a gypsum seed tank, an evaporative crystallizer, a gypsum separator, a gypsum dehydration device, a sodium chloride crystallization separator and a potassium chloride crystallization separator; the multi-stage preheater is provided with an evaporation raw material liquid inlet, a preheating water inlet, a condensed water outlet and a liquid phase outlet; the forced circulation heat exchanger is provided with a feed liquid inlet, a condensed water outlet and an evaporated liquid outlet; the gypsum seed crystal tank is provided with a gypsum seed crystal inlet and a gypsum seed crystal outlet; the evaporation crystallizer is provided with an evaporation liquid inlet, a gypsum seed crystal inlet, a crystal slurry outlet, a salt slurry outlet and a strong brine outlet; the gypsum separator is provided with a crystal slurry inlet, a solid phase outlet and a mother liquid outlet; the gypsum dewatering equipment is provided with a solid phase inlet, a water inlet, a gypsum outlet and a liquid phase outlet; the sodium chloride crystallization separator is provided with a salt slurry inlet, a supernatant outlet, a solid phase outlet and a mother liquor outlet; the potassium chloride crystallization separator is provided with a supernatant inlet, a solid phase outlet and a non-crystallization mother liquor outlet;
wherein an evaporation raw material liquid inlet of the multi-stage preheater is connected with a liquid phase outlet of a pH value adjusting device of the washing liquid purifying unit; a liquid phase outlet of the multi-stage preheater is connected with a feed liquid inlet of the forced circulation heat exchanger; a gypsum seed crystal outlet of the gypsum seed crystal tank is connected with a gypsum seed crystal inlet of the evaporative crystallizer; an evaporation liquid outlet of the forced circulation heat exchanger is connected with an evaporation liquid inlet of the evaporation crystallizer, a condensed water outlet of the forced circulation heat exchanger is connected with a preheated water inlet of the multi-stage preheater, a crystal slurry outlet of the evaporation crystallizer is connected with a crystal slurry inlet of the gypsum separator, a salt slurry outlet of the evaporation crystallizer is connected with a salt slurry inlet of the sodium chloride separator, and a strong brine outlet of the evaporation crystallizer is connected with a feed liquid inlet of the forced circulation heat exchanger; the mother liquor outlet of the gypsum separator and the mother liquor outlet of the sodium chloride crystallization separator are connected with the feed liquor inlet of the forced circulation heat exchanger through mother liquor return pipelines; the supernatant outlet of the sodium chloride crystal separator is connected with the supernatant inlet of the potassium chloride crystal separator; a mother liquor outlet of the potassium chloride crystal separator is connected with a feed liquid inlet of the forced circulation heat exchanger through a mother liquor return pipeline, and a non-crystallization mother liquor outlet of the potassium chloride crystal separator is connected with an inlet of the washing liquid purification unit; the solid phase outlet of the gypsum separator is connected with the solid phase inlet of the gypsum dewatering equipment, the liquid phase outlet of the gypsum dewatering equipment is connected with the fly ash slurry inlet of the fly ash elution unit, and the condensed water outlet of the multi-stage preheater is respectively connected with the pulping water inlet of the fly ash elution unit and the water inlet of the gypsum dewatering equipment.
The gypsum seed crystal method is introduced into the evaporative crystallization process of the water washing liquid, so that the decalcification treatment link of the purification process of the water washing liquid is saved, the purification cost of the water washing liquid is obviously reduced, and the water washing liquid evaporative salt preparation process based on the gypsum seed crystal method can effectively prevent the scaling of a heat exchanger and an evaporative crystallizer, reduce the energy consumption of mass and heat transfer and ensure the stable operation of a system; secondly, sulfate radicals, calcium ions and calcium sulfate in the washing liquid are attached to the gypsum seed crystal to form crystallized gypsum, so that the content of the sulfate radicals and the calcium ions in the crystallized salt is effectively reduced, and the quality of the crystallized salt is improved; thirdly, the crystal gypsum is washed by water to remove soluble impurities in the gypsum, the added value of the gypsum product is improved, and the gypsum eluent returns to the fly ash elution unit to be used as elution process water, so that the water consumption in the fly ash elution process and the energy consumption in the evaporative crystallization process are effectively reduced.
The utility model organically combines multi-stage countercurrent elution, water washing liquid purification and gypsum crystal seed method evaporation crystallization, and solves the problems of high water consumption in the fly ash elution process, high consumption of calcium and magnesium ion remover in the water washing liquid purification process, easy scaling in the evaporation crystallization process and poor quality of crystallized salt.
Compared with the prior art, the utility model has the following advantages and prominent technical effects:
1. the fly ash elution unit adopts multi-stage countercurrent and alkaline water washing technologies, so that the water consumption is low, no dust is raised, the dechlorination effect is good, and the heavy metal leaching rate is low.
2. The gypsum crystal seed method is adopted, calcium and magnesium ions do not need to be removed in the water quality purification stage, and the water quality purification cost is reduced.
3. The evaporation crystallization process of the fly ash water washing liquid based on the gypsum seed crystal method can effectively prevent the evaporator from scaling and ensure the stable operation of the system; the technical problem that sulfate radicals influence the quality of the crystal salt is solved, and the quality of the produced salt can be improved; the condensed water is recycled, and the energy consumption is reduced.
4. The non-crystallization mother liquor generated by the evaporation crystallization unit is discharged to the washing liquid purification unit, so that the consumption of forced circulation evaporation equipment can be reduced to a certain extent, and the yield of salt produced by the system is improved more efficiently.
5. The crystal gypsum is dechlorinated by using a water washing or leaching mode, the gypsum product value is improved, and the economic benefit is good.
Drawings
FIG. 1 is a schematic diagram of the components and connections of the various units of the system of the present invention.
FIG. 2 is a schematic diagram of the components and connections of the devices in the system of the present invention.
Reference numerals: 1 fly ash pulping unit, 2 fly ash eluting unit, 3 water washing liquid purifying unit, 4 evaporating and crystallizing unit, 5 drying unit, 1-1 fly ash pretreatment device, 1-2 fly ash buffer device, 1-3 fly ash metering device, 1-4 pulping equipment, 1-5 water metering device, 2-1 first-level eluting and separating device, 2-2 second-level eluting and separating device, 2-3 third-level eluting and separating device, 3-1 heavy metal removing device, 3-2 concentrating and precipitating device, 3-3 multi-level filtering device, 3-4 pH adjusting device, 3-5 desliming device, 4-1 multi-level preheater, 4-2 forced circulation heat exchanger, 4-3 gypsum seed tank, 4-4 evaporating crystallizer, 4-5 gypsum separator, 4-6 gypsum dewatering device, 4-7 sodium chloride crystal separator and 4-8 potassium chloride crystal separator.
Detailed Description
The utility model will be further described with reference to specific embodiments, and the advantages and features of the utility model will become apparent as the description proceeds. It is to be understood that the described embodiments are exemplary only and are not limiting upon the scope of the utility model. It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the utility model, and that such changes and modifications may be within the scope of the utility model.
In the description of the embodiments of the present application, it should be noted that the indication of orientation or positional relationship is based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship which is usually placed when the product of the application is used, or the orientation or positional relationship which is usually understood by those skilled in the art, or the orientation or positional relationship which is usually placed when the product of the application is used, and is only for the convenience of describing the application and simplifying the description, but does not indicate or imply that the indicated device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the application. In the description of the embodiments of the present application, it should also be noted that, unless otherwise explicitly stated or limited, the terms "disposed," "mounted," and "connected" are to be construed broadly, and may for example be fixedly connected, detachably connected, or integrally connected; may be directly connected or indirectly connected through an intermediate. The specific meaning of the above terms in the present application can be understood in a specific case by those of ordinary skill in the art.
In the description of embodiments of the present application, reference to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
A waste incineration fly ash washing salt making resource treatment method based on a seed crystal method comprises the following steps: (1) crushing the waste incineration fly ash, and stirring the crushed waste incineration fly ash and pulping water to obtain fly ash slurry; (2) performing multi-stage elution on the fly ash slurry by using water to obtain water-washed fly ash and water-washed liquid; (3) purifying the water washing liquid to obtain clear liquid and precipitated slurry; adjusting the pH value of the clear liquid with an acid solution to obtain an evaporation raw material liquid; (4) preheating the evaporation raw material liquid, evaporating and concentrating, evaporating and crystallizing, separating gypsum, separating sodium chloride and separating potassium chloride crystal to obtain gypsum, potassium chloride and sodium chloride products; wherein, gypsum seed crystal is added during evaporation crystallization to ensure that Ca in the crystallization feed liquid2+And SO4 2-The gypsum crystal is condensed on the solid gypsum crystal nucleus to form gypsum crystal precipitation; (5) carrying out desliming treatment on the precipitated slurry obtained in the step (3) to obtain sludge and clear liquid; and (3) drying the sludge and the water-washed fly ash generated in the step (2) to obtain a fly ash finished product.
As a preferred embodiment of the present invention, the crushing in step (1) is to crush the waste incineration fly ash into particles having a particle size of 2mm or less; wherein the mass ratio of the crushed waste incineration fly ash particles to the pulping water is preferably 1:2-1:4, and most preferably 1: 3.
As a preferred embodiment of the present invention, the multi-stage elution in the step (2) is preferably a three-stage elution; specifically, the fly ash slurry prepared in the step (1) enters a first-stage elution separation device to carry out first-stage elution to obtain first-stage washing fly ash and first-stage washing liquid; mixing the first-stage washing fly ash with pulping water to obtain first-stage fly ash slurry, and allowing the first-stage fly ash slurry to enter a second-stage elution separation device for second-stage elution to obtain second-stage washing fly ash and second-stage washing liquid; mixing the second-stage water-washing fly ash with pulping water to obtain second-stage fly ash slurry, and performing third-stage elution on the second-stage fly ash slurry in a third-stage elution separation device to obtain third-stage water-washing fly ash and third-stage water-washing liquid; wherein, the water content of the water washing fly ash obtained in each stage of elution step is not more than 40 percent, and the solid content of the water washing liquid is lower than 1 percent; finally, drying the three-level washing fly ash to obtain a fly ash finished product, for example, drying the three-level washing fly ash by adopting steam or hot air as a drying medium to obtain a fly ash finished product; wherein the temperature of the drying medium is preferably below 300 ℃, most preferably 160-260 ℃; the water content of the obtained fly ash finished product is lower than 5 percent.
As a more preferable embodiment of the utility model, the secondary water washing solution is used as the water for pulping in the step (1), and the tertiary water washing solution is used as the pulping water in the secondary elution; the circulating water and the makeup water of the process are used as the pulping water for the third-stage elution, and the clear water is used as the pulping water for the third-stage elution during the initial work.
As a more preferable specific embodiment of the present invention, in the step (3), the first-stage water washing liquid in the step (2) is adopted to perform purification treatment to obtain clear liquid and precipitated slurry, wherein the purification treatment sequentially comprises heavy metal removal, flocculation precipitation treatment and multi-stage filtration treatment to finally obtain the clear liquid and the precipitated slurry.
As a more preferable embodiment of the present invention, the heavy metal removal treatment may be a heavy metal removal treatment by adding a heavy metal capturing agent (sodium sulfide, sodium thiosulfate, a special agent) into a heavy metal removal device; the flocculation precipitation treatment can be that a flocculation precipitation medicament is added for flocculation precipitation reaction; the multistage filtration treatment can be filtration sequentially through filtration membranes with filtration pore diameters of 10 μm, 5 μm and 1 μm; the pH value is adjusted to 6-8 by using an acidic solution.
As a preferred embodiment of the present invention, the preheating in the step (4) is to preheat the evaporation raw material liquid at a temperature of 90 ℃ to 110 ℃; the evaporation concentration in the step (4) is preferably to enter preheated evaporation raw material liquid into a forced circulation heat exchanger for evaporation concentration treatment, wherein the temperature of the forced circulation heat exchanger is controlled to be 100-120 ℃.
As a preferred embodiment of the utility model, in the step (4), evaporative crystallization is carried out in an evaporative crystallizer, 5-30g/L gypsum seed crystal is added during evaporative crystallization, and the same substances are utilizedThe affinity of the Ca-containing solid gypsum particles is greater than that of the other substances, and the solid gypsum particles are uniformly dispersed in the feed liquid in the evaporative crystallizer, wherein the Ca content in the feed liquid2+And SO4 2-Will first agglomerate on the solid gypsum nuclei to form gypsum crystals and precipitate out.
As a preferred embodiment of the utility model, in the step (4), when evaporation crystallization is carried out, a crystal slurry liquid containing gypsum in an amount of 30 wt% to 60 wt%, a concentrated salt solution and a salt slurry containing salt in an amount of 30 wt% to 60 wt% are respectively obtained; separating gypsum from feed liquid in a gypsum separator to obtain feed liquid and crystalline gypsum with the water content of not more than 60 wt%, conveying the separated feed liquid to a forced circulation heat exchanger for continuous evaporation and concentration treatment, and dechlorinating the crystalline gypsum in a gypsum dewatering device to obtain a gypsum product and gypsum eluent, wherein the dechlorinating is preferably carried out by adopting a gypsum washing or leaching mode; the gypsum eluent can be used as water for pulping in the multi-stage elution process in the step (2); conveying the concentrated salt solution to a forced circulation heat exchanger for evaporation and concentration treatment; the salt slurry enters a sodium chloride crystallization separator for crystallization separation to obtain sodium chloride crystal salt, supernatant and sodium chloride mother liquor; cooling the supernatant in a potassium chloride crystal separator, separating out crystals when the temperature is reduced to 10-50 ℃, and separating to obtain potassium chloride crystal salt with the water content of not more than 6 wt%, potassium chloride mother liquor and non-crystallized potassium chloride mother liquor; purifying the non-crystallized potassium chloride mother liquor; and conveying the sodium chloride mother liquor and the potassium chloride mother liquor to a forced circulation heat exchanger for evaporation and concentration treatment.
Wherein, the condensed water generated in the forced circulation heat exchanger is supplied to a multi-stage preheater for preheating, and the condensed water generated by the multi-stage preheater can be respectively used as water for pulping of the fly ash elution unit and water for a gypsum dehydration device.
As a preferred embodiment of the present invention, the clear solution described in the step (5) is repeatedly subjected to the treatment steps (3) to (5).
Referring to fig. 1 and fig. 2, the special system for realizing the resource treatment method for producing salt by washing the fly ash from the waste incineration with water based on the seed crystal method provided by the utility model comprises a fly ash pulping unit 1, a fly ash elution unit 2, a washing liquid purification unit 3, an evaporation crystallization unit 4 and a drying unit 5; the fly ash washing unit 2 is provided with a fly ash slurry inlet, a solid-phase product outlet, a liquid-phase product outlet and a pulping water inlet; the washing liquid purification unit 3 is provided with a liquid phase inlet, a liquid phase outlet and a solid phase outlet; the evaporative crystallization unit 4 is provided with an evaporative raw material liquid inlet, a non-crystallization mother liquid outlet and a condensed water outlet; the fly ash slurry outlet of the fly ash slurry preparing unit 1 is connected with the fly ash slurry inlet of the fly ash eluting unit 2, the solid-phase product outlet of the fly ash eluting unit 2 is connected with the inlet of the drying unit 5, the liquid-phase product outlet of the fly ash eluting unit 2 is connected with the liquid-phase inlet of the washing liquid purifying unit 3, the liquid-phase outlet of the washing liquid purifying unit 3 is connected with the evaporation raw material liquid inlet of the evaporation crystallizing unit 4, the solid-phase outlet of the washing liquid purifying unit 3 is connected with the inlet of the drying unit 5, the non-crystallization mother liquid outlet of the evaporation crystallizing unit 4 is connected with the liquid-phase inlet of the washing liquid purifying unit 3, and the condensed water outlet of the evaporation crystallizing unit 4 is connected with the slurry preparing water inlet of the fly ash eluting unit 2.
As a preferred embodiment of the present invention, the fly ash pulping unit may include a fly ash pre-treatment device (i.e., a crushing device) 1-1, a fly ash buffer device 1-2, a fly ash metering device 1-3, a pulping apparatus 1-4, a water metering device 1-5; wherein, the outlet of the fly ash pretreatment device 1-1 is connected with the inlet of the fly ash caching device 1-2, the outlet of the fly ash caching device 1-2 is connected with the inlet of the fly ash metering device 1-3, and the outlet of the fly ash metering device 1-3 and the outlet of the water metering device 1-5 are both connected with the inlet of the pulping equipment 1-4.
As a preferred embodiment of the utility model, the fly ash elution unit comprises a first-stage elution separation device 2-1, a second-stage elution separation device 2-2 and a third-stage elution separation device 2-3; wherein the first-stage elution separation device 2-1 is provided with a fly ash slurry inlet, a water washing liquid outlet and a solid phase outlet; the second-stage elution separation device 2-2 is provided with a slurry inlet, a solid phase outlet and a liquid phase inlet; the third-stage elution separation device 2-3 is provided with a slurry inlet, a solid-phase outlet and a liquid-phase outlet; wherein the water washing liquid outlet of the first-stage elution separation device 2-1 is connected with the water washing liquid inlet of the water washing liquid purification unit 3, the solid phase outlet of the first-stage elution separation device 2-1 is connected with the slurry inlet of the second-stage elution separation device 2-2, the liquid phase outlet of the secondary elution separation device 2-2 is connected with the inlet of the water metering device 1-5 of the fly ash pulping unit 1, the solid phase outlet of the second-stage elution separation device 2-1 is connected with the slurry inlet of the third-stage elution separation device 2-3, a liquid phase outlet of the third-stage elution separation device 2-3 is connected with a liquid phase inlet of the second-stage elution separation device 2-2, the solid phase outlet of the three-stage elution separation device 2-3 is connected with the inlet of the drying unit 5.
As a preferred embodiment of the utility model, the washing liquid purification unit 3 can comprise a heavy metal removal device 3-1, a concentration and precipitation device 3-2, a multi-stage filtration device 3-3, a pH value adjusting device 3-4 and a desliming device 3-5; the heavy metal removal device 3-1 is provided with a washing liquid inlet, a liquid phase outlet and a sludge outlet; the concentration and precipitation device 3-2 is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the multistage filtering device 3-3 is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the pH value adjusting device 3-4 is provided with a liquid phase inlet and a liquid phase outlet; the desliming device 3-5 is provided with a sludge inlet, a solid phase outlet and a liquid phase outlet; wherein a water washing liquid inlet of the heavy metal removal device 3-1 is connected with a liquid phase outlet of a first-stage elution separation device 2-1 of the fly ash elution unit 2, a liquid phase outlet of the heavy metal removal device 3-1 is connected with a liquid phase inlet of the concentration and precipitation device 3-2, a liquid phase outlet of the concentration and precipitation device 3-2 is connected with a liquid phase inlet of the multistage filtration device 3-3, and a liquid phase outlet of the multistage filtration device 3-3 is connected with a liquid phase inlet of the pH value adjustment device 3-4; the sludge outlet of the heavy metal removal device 3-1, the sludge outlet of the concentration and precipitation device 3-2 and the sludge outlet of the multistage filtering device 3-3 are all connected with the sludge inlet of the desliming device 3-5; and a solid phase outlet of the desliming device 3-5 is connected with an inlet of the drying unit 5, a liquid phase outlet of the desliming device 3-5 is connected with a liquid phase inlet of the heavy metal removal device 3-1, and a liquid phase outlet of the pH value adjusting device 3-4 is connected with an inlet of the evaporative crystallization unit 4.
As a preferred embodiment of the utility model, the evaporative crystallization unit 4 comprises a multi-stage preheater 4-1, a forced circulation heat exchanger 4-2, a gypsum seed tank 4-3, an evaporative crystallizer 4-4, a gypsum separator 4-5, a gypsum dewatering device 4-6, a sodium chloride crystallization separator 4-7 and a potassium chloride crystallization separator 4-8; the multi-stage preheater 4-1 is provided with an evaporation raw material liquid inlet, a preheating water inlet, a condensed water outlet and a liquid phase outlet; the forced circulation heat exchanger 4-2 is provided with a feed liquid inlet, a condensed water outlet and an evaporated liquid outlet; the gypsum seed crystal tank 4-3 is provided with a gypsum seed crystal inlet and a gypsum seed crystal outlet; the evaporation crystallizer 4-4 is provided with an evaporation liquid inlet, a gypsum seed crystal inlet, a crystal slurry outlet, a salt slurry outlet and a concentrated salt solution outlet; the gypsum separator 4-5 is provided with a crystal slurry inlet, a solid phase outlet and a mother liquid outlet; the gypsum dewatering equipment 4-6 is provided with a solid phase inlet, a water inlet, a gypsum outlet and a liquid phase outlet; the sodium chloride crystallization separator 4-7 is provided with a salt slurry inlet, a supernatant outlet, a solid phase outlet and a mother liquor outlet; the potassium chloride crystallization separator 4-8 is provided with a supernatant inlet, a solid phase outlet and a non-crystallization mother liquor outlet; wherein, an evaporation raw material liquid inlet of the multistage preheater 4-1 is connected with a liquid phase outlet of a pH value adjusting device 3-4 of the washing liquid purifying unit 3; a liquid phase outlet of the multistage preheater 4-1 is connected with a feed liquid inlet of the forced circulation heat exchanger 4-2; a gypsum seed crystal outlet of the gypsum seed crystal tank 4-3 is connected with a gypsum seed crystal inlet of the evaporative crystallizer 4-4; an evaporated liquid outlet of the forced circulation heat exchanger 4-2 is connected with an evaporated liquid inlet of the evaporative crystallizer 4-4, a condensed water outlet of the forced circulation heat exchanger 4-2 is connected with a preheated water inlet of the multistage preheater 4-1, a crystal slurry outlet of the evaporative crystallizer 4-4 is connected with a crystal slurry inlet of the gypsum separator 4-5, a salt slurry outlet of the evaporative crystallizer 4-4 is connected with a salt slurry inlet of the sodium chloride crystallization separator 4-7, and a concentrated salt solution outlet of the evaporative crystallizer 4-4 is connected with a feed liquid inlet of the forced circulation heat exchanger 4-2; the mother liquor outlet of the gypsum separator 4-5 and the mother liquor outlet of the sodium chloride crystallization separator 4-7 are connected with the feed liquor inlet of the forced circulation heat exchanger 4-2 through mother liquor return pipelines; a supernatant outlet of the sodium chloride crystal separator 4-7 is connected with a supernatant inlet of the potassium chloride crystal separator 4-8; a mother liquor outlet of the potassium chloride crystal separator 4-8 is connected with a feed liquid inlet of the forced circulation heat exchanger 4-2 through a mother liquor return pipeline, and a non-crystallization mother liquor outlet of the potassium chloride crystal separator 4-8 is connected with an inlet of the washing liquid purification unit 3; the solid phase outlet of the gypsum separator 4-5 is connected with the solid phase inlet of the gypsum dewatering equipment 4-6, the liquid phase outlet of the gypsum dewatering equipment 4-6 is connected with the fly ash slurry inlet of the fly ash elution unit 2, and the condensed water outlet of the multi-stage preheater 4-1 is respectively connected with the pulping water inlet of the fly ash elution unit 2 and the water inlet of the gypsum dewatering equipment 4-6.
Various devices or apparatuses used in the utility model are conventional devices in the technology of solid waste reprocessing or garbage fly ash reprocessing, and the devices can be purchased commercially and are all suitable for the utility model; in addition, the related literature also discloses new devices with improved devices, and better technical effects can be achieved by using the new devices with improved devices, such as: fly ash pulping equipment (CN 204848668U, the name of the utility model is a fly ash washing device); a first-stage elution and separation device (CN 204848668U, the name of the utility model is a fly ash washing device), a second-stage elution and separation device (CN 204848668U, the name of the utility model is a fly ash washing device), and a third-stage elution and separation device (CN 204848668U, the name of the utility model is a fly ash washing device); heavy metal removing device and concentrated precipitation device (CN 204973179U, utility model name: a multifunctional buffer pool for treating fly ash washing wastewater; CN 208660466U, utility model name: a mud scraper for treating materials with high viscosity and easy hardening), multistage filtering device (CN 205627217U, utility model name: quick-open type multi-medium filter).
The system of the present invention is further described below with reference to specific embodiments.
Example 1
Step 1: fly ash pulping
Step 1-1: the block waste incineration fly ash to be treated is pretreated in a fly ash pretreatment device (crushing device) 1-1, and the particle size of the fly ash is crushed to be below 2 mm; and then sent to the fly ash buffer device 1-2.
Step 1-2: the crushed waste incineration fly ash and pulping water are respectively weighed by a fly ash metering device 1-3, stirred and mixed in a pulping device 1-4 according to the proportion of 1:3, subjected to hydration reaction and pulping, and finally fly ash slurry is obtained.
Step 2: fly ash elution
The fly ash slurry is sequentially subjected to primary elution, secondary elution and tertiary elution in a primary elution separation device 2-1, a secondary elution separation device 2-2 and a tertiary elution separation device 2-3 to obtain washing fly ash and washing liquid; wherein, the water washing ash sequentially comprises the following steps: the fly ash slurry obtained in the step 1-2 enters a first-stage elution separation device 2-1 to obtain first-stage washing ash (the water content is less than or equal to 55%) and first-stage washing liquid (the slag content is less than or equal to 1%), and the first-stage washing ash is mixed with water to form first-stage fly ash slurry; the first-stage fly ash slurry enters a second-stage elution separation device 2-2 to obtain second-stage water washing ash (the water content is less than or equal to 55%) and second-stage water washing liquid (the slag content is less than or equal to 10%), and the second-stage water washing ash is mixed with water to form second-stage fly ash slurry; and (3) feeding the second-stage fly ash slurry into a third-stage elution separation device 2-3 to obtain third-stage washing ash (the water content is less than or equal to 40%) and third-stage washing liquid (the slag content is less than or equal to 10%).
The water washing liquid sequentially comprises the following steps: the first-stage washing liquid enters a washing liquid purification unit 3; the secondary water washing liquid enters the water metering device 1-5 to be used as pulping water; sending the third-stage water washing liquid into a second-stage elution separation device 2-2 to serve as second-stage fly ash slurry proportioning water; and (3) adopting FWD process circulating water and makeup water as pulping water for three-stage elution, and adopting clear water as the pulping water for three-stage elution during initial work.
And step 3: drying of fly ash
And (3) drying the washed fly ash in the step (2) by adopting steam or hot air as a drying medium (the set temperature of the drying medium is 230 ℃), and finally obtaining a fly ash finished product with the water content of less than 5%.
And 4, step 4: purification of water washing liquid
Step 4-1: the water washing liquid generated by the first-stage elution enters a heavy metal removing device 3-1 added with a heavy metal catching agent (sodium sulfide, sodium thiosulfate and a special medicament) with a certain mass concentration, the heavy metal content in the water is reduced, and the water washing liquid after heavy metal removal is subjected to solid-liquid separation to obtain clear liquid and wet mud;
step 4-2: the clear liquid in the step 4-1 enters a concentration and precipitation device 3-2 added with a flocculation and precipitation medicament with certain mass concentration to obtain supernatant liquid and wet mud;
step 4-3: and (3) enabling the supernatant obtained in the step (4-2) to enter a multistage filtering device (10 mu m, 5 mu m and 1 mu m)3-3 to obtain filtrate and filter residues (namely wet mud).
Step 4-4: the filtrate obtained in the step 4-3 enters a pH value adjusting device 3-4, and an acidic reagent with a certain mass concentration is added into the pH value adjusting device 3-4, so that an evaporation raw material liquid is finally obtained;
and 4-5: and (4) allowing the wet sludge obtained in the step (4-1), the step (4-2) and the step (4-3) to enter a desliming device (3-5) for treatment, allowing the generated sludge to enter a drying unit (5) along with washed ash for drying treatment, and allowing the generated liquid phase to enter a heavy metal removal device (3-1) for retreatment.
And 5: evaporative crystallization
Step 5-1: preheating raw material liquid in a multistage preheater 4-1 and raising the temperature to an evaporation temperature of 90-100 ℃;
step 5-2: the preheated feed liquid enters a forced circulation heat exchanger 4-2 for evaporation and concentration treatment, the temperature of the heat exchanger program is set to be 110 ℃, and the next operation is carried out when the solid-liquid ratio of the feed liquid is more than or equal to 30%;
step 5-3: the concentrated feed liquid enters an evaporation crystallizer 4-4, and after crystallization and layering in the evaporation crystallizer 4-4, crystal slurry with gypsum content of 30 wt% -60 wt%, concentrated brine and salt slurry with salt content of 30 wt% -60 wt% are obtained. Conveying the concentrated salt solution to a forced circulation heat exchanger 4-2 for continuous evaporation and concentration treatment; the crystal slurry enters a gypsum separator 4-5; and (3) allowing the salt slurry to enter a sodium chloride crystallization separator 4-7, and separating the crystallized salt from the feed liquid to obtain sodium chloride crystallized salt with the water content of not more than 6 wt%, supernatant and sodium chloride mother liquor.
Step 5-4: when the supernatant in the step 5-3 reaches a potassium chloride saturated solution, the supernatant enters a potassium chloride crystallization separator 4-8, cooling treatment is carried out, crystals are separated out when the temperature is reduced to 10-50 ℃, and potassium chloride crystalline salt with the water content not more than 6 wt%, a potassium chloride mother solution and a potassium chloride mother solution which is not crystallized are obtained after separation (the impurity content in the potassium chloride mother solution reaches 0.5 wt% -10 wt%); discharging the potassium chloride mother liquor which is not crystallized to a washing liquor purification unit 3 for purification treatment.
Step 5-5: and (4) conveying the sodium chloride mother liquor in the step (5-3) and the potassium chloride mother liquor in the step (5-4) to a forced circulation heat exchanger (4-2) to continue evaporation and concentration.
And 5-6: in the step 5-3, 10-30g/L gypsum seed crystal is required to be added into the evaporative crystallizer 4-4, and by utilizing the principle that the affinity of the same substance is greater than that of the different substance, the solid gypsum particles are uniformly dispersed in the feed liquid in the evaporative crystallizer, and Ca in the feed liquid2+And SO4 2-Will first agglomerate on the solid gypsum nuclei to form gypsum crystals and precipitate out.
And 5-7: the crystal slurry in the step 5-3 enters a gypsum separator 4-5, gypsum and feed liquid are separated to obtain crystalline gypsum with the water content of not more than 60 wt%, and the separated feed liquid is conveyed to a forced circulation heat exchanger 4-2 to be continuously subjected to evaporation concentration treatment;
and 5-8: and (3) conveying the crystallized gypsum in the step (5-7) to a gypsum dehydration device (4-6) for treatment, preferably dechlorinating the gypsum in a gypsum water washing or leaching way, and conveying the gypsum eluent to a fly ash elution unit (2) as water for pulping.
Wherein, the condensed water generated by the forced circulation heat exchanger 4-2 is used for preheating water of the multistage preheater 4-1, and the temperature of the preheating water can reach 80-100 ℃;
the condensed water produced by the multi-stage preheater 4-1 can be used as the water for pulping of the fly ash elution unit 2 and the water for the gypsum dewatering device 4-6 respectively.

Claims (6)

1. A resource treatment system for realizing salt production by washing waste incineration fly ash based on a seed crystal method is characterized by comprising a fly ash pulping unit (1), a fly ash elution unit (2), a washing liquid purification unit (3), an evaporation crystallization unit (4) and a drying unit (5); the fly ash pulping unit (1) is provided with a fly ash slurry outlet, and the fly ash eluting unit (2) is provided with a fly ash slurry inlet, a solid-phase product outlet, a liquid-phase product outlet and a pulping water inlet; the washing liquid purification unit (3) is provided with a liquid phase inlet, a liquid phase outlet and a solid phase outlet; the evaporative crystallization unit (4) is provided with an evaporative raw material liquid inlet, a non-crystallization mother liquid outlet and a condensed water outlet; a fly ash slurry outlet of the fly ash pulping unit (1) is connected with a fly ash slurry inlet of the fly ash eluting unit (2), the solid-phase product outlet of the fly ash elution unit (2) is connected with the inlet of the drying unit (5), the liquid-phase product outlet of the fly ash elution unit (2) is connected with the liquid-phase inlet of the washing liquid purification unit (3), the liquid phase outlet of the washing liquid purification unit (3) is connected with the evaporation raw material liquid inlet of the evaporation crystallization unit (4), the solid phase outlet of the washing liquid purifying unit (3) is connected with the inlet of the drying unit (5), the non-crystallization mother liquor outlet of the evaporation crystallization unit (4) is connected with the liquid phase inlet of the washing liquid purification unit (3), a condensed water outlet of the evaporative crystallization unit (4) is connected with a pulping water inlet of the fly ash elution unit (2);
the evaporative crystallization unit (4) comprises a multi-stage preheater (4-1), a forced circulation heat exchanger (4-2), a gypsum seed crystal tank (4-3), an evaporative crystallizer (4-4), a gypsum separator (4-5), a gypsum dewatering device (4-6), a sodium chloride crystallization separator (4-7) and a potassium chloride crystallization separator (4-8); the multi-stage preheater (4-1) is provided with an evaporation raw material liquid inlet, a preheating water inlet, a condensed water outlet and a liquid phase outlet; the forced circulation heat exchanger (4-2) is provided with a feed liquid inlet, a condensed water outlet and an evaporated liquid outlet; the gypsum seed crystal tank (4-3) is provided with a gypsum seed crystal inlet and a gypsum seed crystal outlet; the evaporation crystallizer (4-4) is provided with an evaporation liquid inlet, a gypsum seed crystal inlet, a crystal slurry outlet, a salt slurry outlet and a strong brine outlet; the gypsum separator (4-5) is provided with a crystal slurry inlet, a solid phase outlet and a mother liquid outlet; the gypsum dewatering device (4-6) is provided with a solid phase inlet, a water inlet, a gypsum outlet and a liquid phase outlet; the sodium chloride crystallization separator (4-7) is provided with a salt slurry inlet, a supernatant outlet, a solid phase outlet and a mother liquor outlet; the potassium chloride crystallization separator (4-8) is provided with a supernatant inlet, a solid phase outlet and a non-crystallization mother liquor outlet; wherein an evaporation raw material liquid inlet of the multistage preheater (4-1) is connected with a liquid phase outlet of a pH value adjusting device (3-4) of the washing liquid purifying unit (3); a liquid phase outlet of the multistage preheater (4-1) is connected with a feed liquid inlet of the forced circulation heat exchanger (4-2); a gypsum seed crystal outlet of the gypsum seed crystal tank (4-3) is connected with a gypsum seed crystal inlet of the evaporative crystallizer (4-4); an evaporated liquor outlet of the forced circulation heat exchanger (4-2) is connected with an evaporated liquor inlet of the evaporation crystallizer (4-4), a condensed water outlet of the forced circulation heat exchanger (4-2) is connected with a preheated water inlet of the multistage preheater (4-1), a crystal slurry outlet of the evaporation crystallizer (4-4) is connected with a crystal slurry inlet of the gypsum separator (4-5), a salt slurry outlet of the evaporation crystallizer (4-4) is connected with a salt slurry inlet of the sodium chloride crystallization separator (4-7), and a concentrated salt solution outlet of the evaporation crystallizer (4-4) is connected with a feed liquid inlet of the forced circulation heat exchanger (4-2); the mother liquor outlet of the gypsum separator (4-5) and the mother liquor outlet of the sodium chloride crystallization separator (4-7) are connected with the feed liquor inlet of the forced circulation heat exchanger (4-2) through mother liquor return pipelines; the supernatant outlet of the sodium chloride crystal separator (4-7) is connected with the supernatant inlet of the potassium chloride crystal separator (4-8); a mother liquor outlet of the potassium chloride crystal separator (4-8) is connected with a feed liquid inlet of the forced circulation heat exchanger (4-2) through a mother liquor return pipeline, and a non-crystallization mother liquor outlet of the potassium chloride crystal separator (4-8) is connected with an inlet of the washing liquid purification unit (3); the solid phase outlet of the gypsum separator (4-5) is connected with the solid phase inlet of the gypsum dewatering device (4-6), the liquid phase outlet of the gypsum dewatering device (4-6) is connected with the fly ash slurry inlet of the fly ash elution unit (2), and the condensed water outlet of the multi-stage preheater (4-1) is respectively connected with the pulping water inlet of the fly ash elution unit (2) and the water inlet of the gypsum dewatering device (4-6).
2. A resource processing system according to claim 1, wherein the fly ash pulping unit comprises a fly ash pretreatment device (1-1), a fly ash buffer device (1-2), a fly ash metering device (1-3), a pulping device (1-4), and a water metering device (1-5); the outlet of the fly ash pretreatment device (1-1) is connected with the inlet of the fly ash caching device (1-2), the outlet of the fly ash caching device (1-2) is connected with the inlet of the fly ash metering device (1-3), and the outlet of the fly ash metering device (1-3) and the outlet of the water metering device (1-5) are connected with the inlet of the pulping equipment (1-4).
3. A resource treatment system according to claim 1, characterized in that the fly ash elution unit (2) comprises a primary elution separation device (2-1), a secondary elution separation device (2-2) and a tertiary elution separation device (2-3); the first-stage elution separation device (2-1) is provided with a fly ash slurry inlet, a water washing liquid outlet and a solid phase outlet; the second-stage elution separation device (2-2) is provided with a slurry inlet, a solid-phase outlet and a liquid-phase inlet; the three-stage elution separation device (2-3) is provided with a slurry inlet, a solid phase outlet and a liquid phase outlet; wherein the water washing liquid outlet of the first-stage elution separation device (2-1) is connected with the water washing liquid inlet of the water washing liquid purification unit (3), the solid phase outlet of the first-stage elution separation device (2-1) is connected with the slurry inlet of the second-stage elution separation device (2-2), the liquid phase outlet of the secondary elution separation device (2-2) is connected with the inlet of the water metering device (1-5) of the fly ash pulping unit (1), the solid phase outlet of the second-stage elution separation device (2-2) is connected with the slurry inlet of the third-stage elution separation device (2-3), the liquid phase outlet of the third-stage elution separation device (2-3) is connected with the liquid phase inlet of the second-stage elution separation device (2-2), and a solid phase outlet of the three-stage elution separation device (2-3) is connected with an inlet of the drying unit (5).
4. A resource treatment system according to claim 1, characterized in that the washing liquid purification unit (3) comprises a heavy metal removal device (3-1), a concentration and precipitation device (3-2), a multi-stage filtration device (3-3), a pH value adjustment device (3-4) and a desliming device (3-5).
5. A resource treatment system according to claim 4, characterized in that the heavy metal removal device (3-1) is provided with a washing liquid inlet, a liquid phase outlet and a sludge outlet; the concentration and precipitation device (3-2) is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the multistage filtering device (3-3) is provided with a liquid phase inlet, a liquid phase outlet and a sludge outlet; the pH value adjusting device (3-4) is provided with a liquid phase inlet and a liquid phase outlet; the desliming device (3-5) is provided with a sludge inlet, a solid phase outlet and a liquid phase outlet; wherein a water washing liquid inlet of the heavy metal removal device (3-1) is connected with a liquid phase outlet of a first-stage elution separation device (2-1) of the fly ash elution unit (2), a liquid phase outlet of the heavy metal removal device (3-1) is connected with a liquid phase inlet of the concentration and precipitation device (3-2), a liquid phase outlet of the concentration and precipitation device (3-2) is connected with a liquid phase inlet of the multistage filtration device (3-3), and a liquid phase outlet of the multistage filtration device (3-3) is connected with a liquid phase inlet of the pH value adjustment device (3-4); the sludge outlet of the heavy metal removal device (3-1), the sludge outlet of the concentration and precipitation device (3-2) and the sludge outlet of the multistage filtering device (3-3) are connected with the sludge inlet of the desliming device (3-5).
6. A resource treatment system according to claim 5, characterized in that the solid phase outlet of the desliming device (3-5) is connected with the inlet of the drying unit (5), the liquid phase outlet of the desliming device (3-5) is connected with the liquid phase inlet of the heavy metal removal device (3-1), and the liquid phase outlet of the pH value adjusting device (3-4) is connected with the inlet of the evaporative crystallization unit (4).
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