Cooperative treatment system and method for fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas

Abstract

The invention discloses a cooperative treatment system and method for fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas, and belongs to the field of chemical engineering environments. The treatment system comprises a fly ash separation unit used for separating potassium chloride and sodium chloride from the waste incineration fly ash; the ammonium salt water unit is used for forming saturated ammonium salt water from water, sodium chloride and ammonia gas; the carbonization unit is used for carrying out carbonization reaction on the saturated ammonium salt water and the nonferrous smelting flue gas to generate a carbide material containing sodium bicarbonate and ammonium chloride; the first separation unit is used for separating sodium bicarbonate and ammonium chloride from the carbide material; the pyrolysis unit is used for pyrolyzing sodium bicarbonate into sodium carbonate; and the reaction unit is used for reacting the sodium sulfate waste salt with potassium chloride and separating potassium sulfate. According to the system, recycling of fly ash, sodium sulfate waste salt and nonferrous smelting flue gas waste resources is achieved, obtained products sodium carbonate, ammonium chloride and potassium sulfate all meet national standard requirements, the system has high use value, and meanwhile harm of hazardous waste to the environment is reduced.

Description

Technical Field

[0001] The present application relates to the field of chemical environmental technology, and in particular to a system and method for the coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas. Background Art

[0002] The main methods of treating municipal solid waste are landfill, incineration and composting. Among them, incineration has become the main method of treating municipal solid waste because it can effectively reduce the amount of waste. During the burning of waste, organic matter is oxidized into water and carbon dioxide and discharged into the atmosphere, while inorganic matter mainly turns into solid particles with smaller particle sizes. Among these solid particles, larger particles are deposited at the bottom of the incinerator and on the grate, and fine particles enter the flue gas purification device. These fine particles account for about 50% of the total mass of the incineration residues, and the other 50% is limestone or activated carbon added in the process. The larger particles of these residues are captured in the dust collector (electrostatic dust collector, bag filter, etc.). The smaller particles settle at the bottom of the flue or chimney, which is called waste incineration fly ash, which contains heavy metals and elements such as calcium, sodium, potassium, and chlorine. Fly ash is a hazardous waste, and the current disposal method is mainly landfill, which will occupy arable land and produce leachate to pollute soil and groundwater.

[0003] In the process of zero discharge of nonferrous metallurgical wastewater, the salts in the wastewater will be discharged in the form of miscellaneous salts.

[0004] The flue gas generated by the non-ferrous metallurgical process is discharged into the atmosphere after being treated to meet the standards. It contains a large amount of carbon dioxide that can cause a greenhouse effect.

[0005] In response to the above problems, if a process or system can be developed to process the above hazardous waste as raw materials to produce high value-added products (such as potassium sulfate, sodium carbonate, etc.), it will not only save resources and turn waste into treasure, but also reduce environmental pollution. Summary of the invention

[0006] The main purpose of the present application is to provide a system and method for the coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas, so as to solve the problem in the prior art that various waste resources cannot be well utilized, resulting in resource waste or environmental pollution.

[0007] In order to achieve the above-mentioned purpose, according to one aspect of the present application, a fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system is provided, and the treatment system comprises:

[0008] A fly ash separation unit has a fly ash inlet, a fly ash water inlet, a potassium chloride outlet and a sodium chloride outlet, and the fly ash separation unit is used to separate potassium chloride and sodium chloride from waste incineration fly ash;

[0009] The ammonium brine unit has an ammonia gas inlet, a salt water inlet, a salt water inlet and a saturated ammonium brine outlet; the sodium chloride outlet is connected to the salt water inlet; the ammonium brine unit is used to mix water, sodium chloride and ammonia gas to form a saturated ammonium brine;

[0010] The carbonization unit has a saturated ammonium salt water inlet, a smelting flue gas inlet and a carbonized material outlet; the saturated ammonium salt water outlet is connected to the saturated ammonium salt water inlet; the carbonization unit is used to carbonize the saturated ammonium salt water and the non-ferrous smelting flue gas to generate a carbonized material containing sodium bicarbonate and ammonium chloride;

[0011] The first separation unit has a carbonized material inlet, a sodium bicarbonate outlet and an ammonium chloride outlet; the carbonized material outlet is connected to the carbonized material inlet; the first separation unit is used to separate sodium bicarbonate and ammonium chloride from the carbonized material;

[0012] The pyrolysis unit has a sodium bicarbonate inlet, a pyrolysis flue gas outlet and a sodium carbonate outlet; the sodium bicarbonate outlet is connected to the sodium bicarbonate inlet; the pyrolysis unit is used to pyrolyze the sodium bicarbonate into sodium carbonate;

[0013] The reaction unit has a potassium chloride inlet, a sodium sulfate inlet, a reaction water inlet and a potassium sulfate outlet; the potassium chloride outlet is connected to the potassium chloride inlet; the reaction unit is used to perform a double decomposition reaction on the metallurgical by-product sodium sulfate waste salt and potassium chloride and separate potassium sulfate from the decomposed materials.

[0014] Further, the treatment system also includes a sodium carbonate storage unit, an ammonium chloride storage unit, a potassium sulfate storage unit, a distilled water storage unit, a sodium chloride storage unit, and a potassium chloride storage unit;

[0015] The sodium chloride outlet is connected to the inlet of the sodium chloride storage unit, and the outlet of the sodium chloride storage unit is connected to the brine inlet of the ammonium brine unit;

[0016] The potassium chloride outlet is connected to the inlet of the potassium chloride storage unit, and the outlet of the potassium chloride storage unit is connected to the potassium chloride inlet of the reaction unit;

[0017] The outlet of the distilled water storage unit is respectively connected to the fly ash water inlet of the fly ash separation unit, the salt water inlet of the ammonium salt water unit, and the reaction water inlet of the reaction unit;

[0018] The sodium carbonate outlet of the pyrolysis unit is connected to the inlet of the sodium carbonate storage unit; the ammonium chloride outlet of the first separation unit is connected to the inlet of the ammonium chloride storage unit; and the potassium sulfate outlet of the reaction unit is connected to the inlet of the potassium sulfate storage unit.

[0019] Further, the fly ash separation unit comprises:

[0020] A fly ash washing unit has a fly ash inlet, a fly ash water inlet and a solid-liquid mixture outlet; the fly ash washing unit is used to wash the fly ash to form a solid-liquid mixture;

[0021] The second separation unit has a solid-liquid mixture inlet and a separated liquid material outlet; the solid-liquid mixture outlet is connected to the solid-liquid mixture inlet; the second separation unit is used to separate the liquid material containing potassium chloride and sodium chloride from the solid-liquid mixture;

[0022] The first evaporation crystallization unit has a separated liquid material inlet, a cooling crystallization mother liquor inlet, a sodium chloride outlet, a first evaporation water outlet, and a potassium chloride-containing mother liquor outlet; the separated liquid material outlet is connected to the separated liquid material inlet; the first evaporation crystallization unit is used to evaporate and crystallize sodium chloride from the liquid material containing potassium chloride and sodium chloride and separate the potassium chloride-containing mother liquor;

[0023] The cooling crystallization unit comprises a potassium chloride-containing mother liquor inlet, a cooling crystallization mother liquor outlet and a potassium chloride outlet; the potassium chloride-containing mother liquor outlet is connected to the potassium chloride-containing mother liquor inlet; the cooling crystallization mother liquor outlet is connected to the cooling crystallization mother liquor inlet; and the cooling crystallization unit is used for cooling and crystallizing potassium chloride from the potassium chloride-containing mother liquor.

[0024] Furthermore, the treatment system also includes a distilled water storage unit, and the first evaporated water outlet is connected to the inlet of the distilled water storage unit.

[0025] Furthermore, the first evaporation crystallization unit adopts a multiple-effect evaporation device and / or a mechanical vapor recompression device.

[0026] Further, the ammonium brine unit comprises:

[0027] A saturated brine unit having a brine inlet, a brine water inlet and a saturated brine outlet; the saturated brine unit is used to mix sodium chloride and water to form saturated brine;

[0028] The saturated ammonium brine unit has a saturated brine inlet, an ammonia gas inlet and a saturated ammonium brine outlet; the saturated brine outlet is connected to the saturated brine inlet; the saturated ammonium brine unit is used to form saturated ammonium brine from ammonia gas and saturated brine.

[0029] Furthermore, the pyrolysis flue gas outlet of the pyrolysis unit is connected to the smelting flue gas inlet of the carbonization unit.

[0030] Furthermore, the carbonization unit adopts a carbonization tower device.

[0031] Furthermore, the pyrolysis unit adopts a rotary kiln device.

[0032] Furthermore, the ammonium brine unit adopts an ammonia absorption tower device.

[0033] Further, the second separation unit comprises:

[0034] The first solid-liquid separation unit has a solid-liquid mixture inlet, a fly ash solid phase material outlet, and a fly ash liquid phase material outlet; the first solid-liquid separation unit is used to separate the fly ash liquid phase material from the solid-liquid mixture;

[0035] The hardness removal unit has a fly ash liquid phase material inlet, a hardness removal agent inlet and a hardness removed material outlet; the fly ash liquid phase material outlet is connected to the fly ash liquid phase material inlet; the hardness removal unit is used to remove calcium ions and magnesium ions in the fly ash liquid phase material to form a hardness removed material;

[0036] The heavy metal removal unit has a hardened material inlet, a heavy metal removal agent inlet and a heavy metal removal material outlet; the hardened material inlet and the hardened material outlet are connected; the heavy metal removal unit is used to remove heavy metals in the hardened material to form a heavy metal-removed material;

[0037] The second solid-liquid separation unit has an inlet for the material after heavy metal removal, an outlet for the solid phase material after separation, and an outlet for the liquid phase material after separation; the outlet for the material after heavy metal removal is connected to the inlet for the material after heavy metal removal; the second solid-liquid separation unit is used to separate the liquid phase material containing potassium chloride and sodium chloride from the material after heavy metal removal;

[0038] The first solid-liquid separation unit uses a belt filter and / or a plate-frame filter press; the second solid-liquid separation unit uses a belt filter and / or a plate-frame filter press;

[0039] The processing system also includes a solid waste storage unit; the fly ash solid phase material outlet and the separated solid phase material outlet are respectively connected to the inlet of the solid waste storage unit.

[0040] Furthermore, the first separation unit comprises:

[0041] The third solid-liquid separation unit has a carbonized material inlet, a sodium bicarbonate outlet, and an ammonium chloride-containing material outlet; the third solid-liquid separation unit is used to separate sodium bicarbonate and ammonium chloride-containing materials from the carbonized material;

[0042] The salting-out unit has an ammonium chloride material inlet, a salting-out salt inlet and a salted-out material outlet; the ammonium chloride material outlet is connected to the ammonium chloride material inlet; the sodium chloride outlet is connected to the salting-out salt inlet; the salting-out unit is used to separate ammonium chloride from the ammonium chloride material using sodium chloride to form an ammonium chloride solid-liquid mixture;

[0043] The fourth solid-liquid separation unit has a post-salting out material inlet, an ammonium chloride outlet, and a fourth solid-liquid separation liquid phase material outlet; the post-salting out material outlet is connected to the post-salting out material inlet; the fourth solid-liquid separation liquid phase material outlet is connected to the salt water inlet of the ammonium salt water unit; the fourth solid-liquid separation unit is used to separate ammonium chloride from the ammonium chloride solid-liquid mixture;

[0044] The third solid-liquid separation unit adopts a belt filter and / or a plate-frame filter press device; the fourth solid-liquid separation unit adopts a belt filter and / or a plate-frame filter press device.

[0045] Furthermore, the processing system also includes a sodium chloride storage unit, and the outlet of the sodium chloride storage unit is connected to the salt inlet for salting out.

[0046] Further, the reaction unit comprises:

[0047] The first double decomposition reaction unit has a potassium chloride inlet, a sodium sulfate inlet, a reaction water inlet and a first decomposition material outlet; the first double decomposition reaction unit is used to carry out a first double decomposition reaction of potassium chloride and a metallurgical byproduct sodium sulfate to generate a double decomposition material containing glauberite and sodium chloride;

[0048] The fifth solid-liquid separation unit has a first decomposition material inlet, a glauberite outlet and a sodium chloride-containing liquid phase material outlet; the first decomposition material outlet is connected to the first decomposition material inlet; the fifth solid-liquid separation unit is used to separate glauberite and a liquid phase material containing sodium chloride from the double decomposition material containing glauberite and sodium chloride;

[0049] The second double decomposition reaction unit has a glauberite inlet, a potassium chloride inlet for the second double decomposition reaction, a water inlet for the second double decomposition reaction, and an outlet for a material containing potassium sulfate; the glauberite outlet is connected to the glauberite inlet; the second double decomposition reaction unit is used to react glauberite and potassium chloride to generate a material containing potassium sulfate;

[0050] The sixth solid-liquid separation unit has a potassium sulfate-containing material inlet and a potassium sulfate outlet; the potassium sulfate-containing material outlet is connected to the potassium sulfate-containing material inlet; the sixth solid-liquid separation unit is used to separate potassium sulfate from the potassium sulfate-containing material.

[0051] Furthermore, the reaction unit also includes a second evaporation crystallization unit, which has a sodium chloride-containing liquid phase material inlet, a second evaporation water outlet, a second evaporation mother liquor outlet and a second evaporation crystallization sodium chloride outlet; the sodium chloride-containing liquid phase material outlet is connected to the sodium chloride-containing liquid phase material inlet; the second evaporation crystallization unit is used to evaporate and crystallize sodium chloride from the sodium chloride-containing liquid phase material;

[0052] The first metathesis reaction unit also has a second evaporation mother liquor inlet and a sixth separation clear liquid inlet; the sixth solid-liquid separation unit also has a sixth separation clear liquid outlet; the second evaporation mother liquor outlet is connected to the second evaporation mother liquor inlet; the sixth separation clear liquid outlet is connected to the sixth separation clear liquid inlet;

[0053] The treatment system also includes a distilled water storage unit; the outlet of the distilled water storage unit is respectively connected to the reaction water inlet of the first double decomposition reaction unit and the second double decomposition reaction water inlet of the second double decomposition reaction unit; the second evaporated water outlet of the second evaporation crystallization unit is connected to the inlet of the distilled water storage unit.

[0054] Furthermore, the processing system also includes a sodium chloride storage unit, and the second evaporation and crystallization sodium chloride outlet of the second evaporation and crystallization unit is connected to the inlet of the sodium chloride storage unit.

[0055] Furthermore, the first metathesis reaction unit and the second metathesis reaction unit adopt a reactor device.

[0056] Furthermore, the fifth solid-liquid separation unit adopts a belt filter and / or a plate-frame filter press device; the sixth solid-liquid separation unit adopts a belt filter and / or a plate-frame filter press device.

[0057] Furthermore, the second evaporation crystallization unit adopts a multiple-effect evaporation device and / or a mechanical vapor recompression device.

[0058] According to the second aspect of the present application, a method for the coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas is provided, the method adopts the above-mentioned coordinated treatment system; the method comprises the following steps:

[0059] Step 1: Treat the waste incineration fly ash to separate potassium chloride and sodium chloride;

[0060] Step 2: using sodium chloride, water and ammonia to form a saturated ammonium brine;

[0061] Step 3: using saturated ammonium salt water and non-ferrous smelting flue gas to carry out carbonization reaction to obtain a carbonized material containing sodium bicarbonate and ammonium chloride;

[0062] Step 4: Separating sodium bicarbonate and ammonium chloride from the carbonized material containing sodium bicarbonate and ammonium chloride;

[0063] Step 5: thermally decomposing sodium bicarbonate to obtain sodium carbonate;

[0064] Step 6: Mix potassium chloride, sodium sulfate and water, react them, and separate potassium sulfate from the reaction product.

[0065] Furthermore, the specific process of step 1 includes:

[0066] Step 1-1: firstly wash the fly ash with water to form a solid-liquid mixture, and then separate the solid-liquid mixture to obtain a liquid material containing potassium chloride and sodium chloride;

[0067] Step 1-2: performing a first evaporation crystallization on the liquid phase material containing potassium chloride and sodium chloride to obtain first evaporated water, sodium chloride and a mother liquor containing potassium chloride, respectively;

[0068] Step 1-3: Cooling and crystallizing the potassium chloride-containing mother liquor to separate potassium chloride.

[0069] Furthermore, the specific process of step 6 includes:

[0070] Step 6-1: Mix potassium chloride, sodium sulfate and water to perform a first double decomposition reaction to obtain a double decomposition material containing glauberite and sodium chloride;

[0071] Step 6-2: performing solid-liquid separation on the double decomposition material containing glauberite and sodium chloride to obtain a liquid phase material containing glauberite and sodium chloride;

[0072] Step 6-3: Mixing glauberite, potassium chloride and water, and performing a second double decomposition reaction to obtain a material containing potassium sulfate;

[0073] Step 6-4: performing solid-liquid separation on the material containing potassium sulfate to obtain potassium sulfate.

[0074] Furthermore, the temperature of the pyrolysis reaction is 100-200°C.

[0075] Furthermore, the carbon dioxide operating pressure of the carbonization reaction is 0.3-0.6 MPa.

[0076] Furthermore, the operating temperature of the carbonization reaction is 30°C to 60°C.

[0077] Furthermore, the operating temperature of the carbonization reaction in step 3 is 30°C to 40°C. Furthermore, the specific process of step 1-1 includes: firstly washing the fly ash with water to form a solid-liquid mixture, performing a first solid-liquid separation, and separating the fly ash liquid phase material; the fly ash liquid phase material is successively subjected to hardness removal and heavy metal removal treatments, and then a second solid-liquid separation is performed to obtain a liquid phase material containing potassium chloride and sodium chloride; wherein the hardness removal agent is sodium hydroxide and sodium carbonate, and the hardness removal is performed by a double alkali method; the heavy metal removal agent is sodium sulfide.

[0078] Furthermore, the process of step 6-2 also includes performing a second evaporation crystallization on the liquid phase material containing sodium chloride to obtain second evaporated water, sodium chloride and a second evaporated mother liquor; the second evaporated mother liquor, the clear liquid after solid-liquid separation in step 6-4 and the material in step 6-1 are mixed to perform a first double decomposition reaction; the temperature of the second evaporation crystallization is 90° C. to 120° C.

[0079] Furthermore, the temperature of the first evaporation crystallization is 90°C to 120°C.

[0080] Furthermore, the temperature of cooling crystallization is 10°C to 35°C.

[0081] Furthermore, the molar ratio of potassium chloride to sodium sulfate is (2-3):1.

[0082] Furthermore, the temperature of the first metathesis reaction is 30°C to 60°C.

[0083] Furthermore, the temperature of the second metathesis reaction is 25°C to 60°C.

[0084] By applying the technical solution of the present application, a system and method for the coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas are provided, wherein sodium chloride and potassium chloride are extracted from waste incineration fly ash, saturated ammonium brine is formed by utilizing the sodium chloride and ammonia, and the saturated ammonium brine is utilized to treat non-ferrous metallurgical flue gas to form products of sodium carbonate and ammonium chloride; potassium chloride in the fly ash is reacted with worthless non-ferrous metallurgical by-product industrial sodium sulfate to form product potassium sulfate; the treatment system and method of the present application fully realize the recycling of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas waste resources, and the obtained products of sodium carbonate, ammonium chloride and potassium sulfate all meet the requirements of national standards, have high use value, and effectively reduce the harm of hazardous waste to the environment. BRIEF DESCRIPTION OF THE DRAWINGS

[0085] The drawings constituting part of the present application are used to provide a further understanding of the present application. The exemplary embodiments and descriptions of the present application are used to explain the present application and do not constitute an improper limitation on the present application. In the drawings:

[0086] Figure 1 A schematic diagram of a collaborative processing system according to Embodiment 1 of the present application is shown.

[0087] Reference numerals:

[0088] 10. Fly ash separation unit; 11. Fly ash washing unit; 12. Second separation unit; 121. First solid-liquid separation unit; 122. Hardness removal unit; 123. Heavy metal removal unit; 124. Second solid-liquid separation unit; 13. First evaporation crystallization unit; 14. Cooling crystallization unit;

[0089] 20. Ammonium brine unit; 21. Saturated brine unit; 22. Saturated ammonium brine unit;

[0090] 30. Carbonization unit;

[0091] 40. First separation unit; 41. Third solid-liquid separation unit; 42. Salting-out unit; 43. Fourth solid-liquid separation unit;

[0092] 50. Pyrolysis unit;

[0093] 60. reaction unit; 61. first metathesis reaction unit; 62. fifth solid-liquid separation unit; 63. second metathesis reaction unit; 64. sixth solid-liquid separation unit; 65. second evaporation crystallization unit;

[0094] 70. Sodium carbonate storage unit; 71. Ammonium chloride storage unit; 72. Potassium sulfate storage unit; 73. Distilled water storage unit; 74. Sodium chloride storage unit; 75. Potassium chloride storage unit; 76. Solid waste storage unit. DETAILED DESCRIPTION

[0095] It should be noted that, in the absence of conflict, the embodiments and features in the embodiments of the present application can be combined with each other. The present application will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0096] At present, the main way to deal with fly ash from garbage incineration is landfill, which will occupy arable land and pollute soil and groundwater; the way to dispose of industrial sodium sulfate, a by-product of non-ferrous metallurgical wastewater, is to sell it outside, but the sodium sulfate market is in oversupply, and the by-product sodium sulfate is difficult to sell, and it is likely to end up in landfill; the way to dispose of non-ferrous metallurgical waste gas is to discharge it after treatment meets the standards, but it contains a large amount of carbon dioxide, which will cause a greenhouse effect; therefore, if fly ash, by-product sodium sulfate, and metallurgical flue gas can be fully utilized to form useful resources, it will save a lot of resources, reduce environmental pollution, and produce high value-added products.

[0097] According to one aspect of the present application, a fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system is provided, such as Figure 1 As shown, the processing system includes:

[0098] The fly ash separation unit 10 has a fly ash inlet, a fly ash water inlet, a potassium chloride outlet and a sodium chloride outlet. The fly ash separation unit 10 is used to separate potassium chloride and sodium chloride from waste incineration fly ash respectively;

[0099] The ammonium brine unit 20 has an ammonia gas inlet, a salt water inlet, a salt water inlet and a saturated ammonium brine outlet; the sodium chloride outlet is connected to the salt water inlet; the ammonium brine unit 20 is used to mix water, sodium chloride and ammonia gas to form a saturated ammonium brine;

[0100] The carbonization unit 30 has a saturated ammonium salt water inlet, a smelting flue gas inlet and a carbonized material outlet; the saturated ammonium salt water outlet is connected to the saturated ammonium salt water inlet; the carbonization unit 30 is used to carbonize the saturated ammonium salt water and the non-ferrous smelting flue gas to generate a carbonized material containing sodium bicarbonate and ammonium chloride;

[0101] The first separation unit 40 has a carbonized material inlet, a sodium bicarbonate outlet and an ammonium chloride outlet; the carbonized material outlet is connected to the carbonized material inlet; the first separation unit 40 is used to separate sodium bicarbonate and ammonium chloride from the carbonized material;

[0102] The pyrolysis unit 50 has a sodium bicarbonate inlet, a pyrolysis flue gas outlet and a sodium carbonate outlet; the sodium bicarbonate outlet is connected to the sodium bicarbonate inlet; the pyrolysis unit 50 is used to pyrolyze the sodium bicarbonate into sodium carbonate;

[0103] The reaction unit 60 has a potassium chloride inlet, a sodium sulfate inlet, a reaction water inlet and a potassium sulfate outlet; the potassium chloride outlet is connected to the potassium chloride inlet; the reaction unit is used to perform a double decomposition reaction on the metallurgical by-product sodium sulfate waste salt and potassium chloride and separate potassium sulfate from the decomposed materials.

[0104] In the treatment system of the present application, each unit is connected by pipelines, etc., and a power device can be arranged in the middle to control the logistics conveying speed; the above-mentioned method and equipment for extracting sodium chloride and potassium chloride from fly ash can be selected from the existing technology, as long as the purpose can be achieved; the water and salt of the above-mentioned ammonium salt water unit can be mixed before entering the unit or can enter the unit at the same time, and the equipment used can be selected from the existing technology, as long as water, sodium chloride and ammonia can be mixed to form saturated ammonium salt water; the reaction mode and structural design of the above-mentioned carbonization unit can be selected from the existing technology, as long as carbon dioxide and saturated ammonium salt water can be reacted to generate sodium bicarbonate and ammonium chloride; the separation method and structural design of the above-mentioned first separation unit can be selected from the existing technology, as long as sodium bicarbonate and ammonium chloride can be separated from the carbonized material; the heating mode, reaction mode and structural design of the above-mentioned pyrolysis unit can be selected from the existing technology, as long as sodium bicarbonate can be formed into sodium carbonate; the reaction conditions and structural design of potassium chloride, sodium sulfate and water in the above-mentioned reaction unit can be selected from the existing technology, as long as potassium chloride and sodium sulfate can react to generate potassium sulfate.

[0105] The innovation of this application is how to design a system that can synergistically utilize fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas to form high value-added products. The above-mentioned treatment system designed by this application realizes the recycling of fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas waste resources to the greatest extent, while also effectively reducing the harm of hazardous waste to the environment. The annual operating time of the system of this application is 7,200 hours, and the operation is stable.

[0106] In some embodiments, the above-mentioned treatment system also includes a sodium carbonate storage unit 70, an ammonium chloride storage unit 71, a potassium sulfate storage unit 72, a distilled water storage unit 73, a sodium chloride storage unit 74 and a potassium chloride storage unit 75; the sodium chloride outlet is connected to the inlet of the sodium chloride storage unit 74, and the outlet of the sodium chloride storage unit 74 is connected to the salt inlet of the brine of the ammonium brine unit 20; the potassium chloride outlet is connected to the inlet of the potassium chloride storage unit 75, and the outlet of the potassium chloride storage unit 75 is connected to the potassium chloride inlet of the reaction unit 60; the outlet of the distilled water storage unit 73 is respectively connected to the fly ash water inlet of the fly ash separation unit 10, the salt water inlet of the ammonium brine unit 20, and the reaction water inlet of the reaction unit 60; the sodium carbonate outlet of the pyrolysis unit 50 is connected to the inlet of the sodium carbonate storage unit 70; the ammonium chloride outlet of the first separation unit 40 is connected to the inlet of the ammonium chloride storage unit 71; the potassium sulfate outlet of the reaction unit 60 is connected to the inlet of the potassium sulfate storage unit 72.

[0107] The present application sets up transfer storage units for the intermediate products, final products, water, etc. obtained, which can collect or divert the corresponding products, stabilize the logistics transportation speed, and make the entire processing system run stably.

[0108] In some embodiments, the fly ash separation unit 10 comprises:

[0109] The fly ash washing unit 11 has a fly ash inlet, a fly ash water inlet and a solid-liquid mixture outlet; the fly ash washing unit 11 is used to wash the fly ash to form a solid-liquid mixture;

[0110] The second separation unit 12 has a solid-liquid mixture inlet and a separated liquid material outlet; the solid-liquid mixture outlet is connected to the solid-liquid mixture inlet; the second separation unit 12 is used to separate the liquid material containing potassium chloride and sodium chloride from the solid-liquid mixture;

[0111] The first evaporation crystallization unit 13 has a separated liquid material inlet, a cooling crystallization mother liquor inlet, a sodium chloride outlet, a first evaporation water outlet and a potassium chloride-containing mother liquor outlet; the separated liquid material outlet is connected to the separated liquid material inlet; the first evaporation crystallization unit 13 is used to evaporate and crystallize sodium chloride from the liquid material containing potassium chloride and sodium chloride and separate the potassium chloride-containing mother liquor;

[0112] The cooling crystallization unit 14 has an inlet for a potassium chloride-containing mother liquor, an outlet for cooling and crystallizing the mother liquor, and an outlet for potassium chloride; the outlet for the potassium chloride-containing mother liquor is connected to the inlet for the potassium chloride-containing mother liquor; the outlet for cooling and crystallizing the mother liquor is connected to the inlet for cooling and crystallizing the mother liquor; the cooling crystallization unit 14 is used for cooling and crystallizing potassium chloride from the potassium chloride-containing mother liquor.

[0113] The fly ash separation unit designed in the present application can fully extract sodium ions, potassium ions, chloride ions, etc. in the fly ash into the liquid phase material, and crystallize sodium chloride by evaporation crystallization, and crystallize potassium chloride by cooling crystallization; it provides relatively pure reactants sodium chloride and potassium chloride for subsequent reactions, and also ensures that the products potassium sulfate, sodium carbonate and ammonium chloride after the reaction reach the purpose of high purity.

[0114] In some embodiments, the treatment system further includes a distilled water storage unit 73, and the first evaporated water outlet is connected to the inlet of the distilled water storage unit 73. The present application designs a return line to return the water generated in the first evaporation and crystallization process to the water storage unit, so as to facilitate the delivery to other units in the treatment system that need water, thereby realizing the recycling of water production and water supply and saving water.

[0115] In some embodiments, the first evaporation crystallization unit 13 uses a multiple-effect evaporation device and / or a mechanical vapor recompression device. The above evaporation equipment is used in this application to improve the evaporation efficiency and obtain relatively pure sodium chloride and water.

[0116] In some embodiments, the ammonium brine unit 20 includes: a saturated brine unit 21, having a brine salt inlet, a brine water inlet and a saturated brine outlet; the saturated brine unit 21 is used to mix sodium chloride and water to form saturated brine; a saturated ammonium brine unit 22, having a saturated brine inlet, an ammonia gas inlet and a saturated ammonium brine outlet; the saturated brine outlet and the saturated brine inlet are connected; the saturated ammonium brine unit is used to form saturated ammonium brine from ammonia gas and saturated brine.

[0117] The present application first mixes water and sodium chloride to form saturated brine, and then feeds the saturated brine into a saturated ammonium brine unit to react with ammonia. This feeding method can fully mix the saturated brine and ammonia, thereby improving the reaction efficiency.

[0118] In some embodiments, the pyrolysis flue gas outlet of the pyrolysis unit 50 is connected to the smelting flue gas inlet of the carbonization unit 30. In the present application, the carbon dioxide generated by the pyrolysis of sodium bicarbonate is returned to the flue gas inlet of the carbonization unit, and the carbon dioxide is not directly removed, but is fully utilized to participate in the reaction. The design of the return route can realize the reuse of waste gas and improve the waste treatment effect.

[0119] In some embodiments, the carbonization unit 30 uses a carbonization tower device, the pyrolysis unit 50 uses a rotary kiln device, and the ammonium salt water unit 20 uses an ammonia absorption tower device. The present application uses the above devices to perform carbonization reaction, pyrolysis reaction and ammonium salt reaction, which can improve the reaction efficiency.

[0120] In some embodiments, the second separation unit 12 includes:

[0121] The first solid-liquid separation unit 121 has a solid-liquid mixture inlet, a fly ash solid phase material outlet, and a fly ash liquid phase material outlet; the first solid-liquid separation unit 121 is used to separate the fly ash liquid phase material from the solid-liquid mixture;

[0122] The hardness removal unit 122 has a fly ash liquid phase material inlet, a hardness removal agent inlet and a hardness removed material outlet; the fly ash liquid phase material outlet is connected to the fly ash liquid phase material inlet; the hardness removal unit is used to remove calcium ions and magnesium ions in the fly ash liquid phase material to form a hardness removed material;

[0123] The heavy metal removal unit 123 has a hardened material inlet, a heavy metal removal agent inlet and a heavy metal removal material outlet; the hardened material inlet and the hardened material outlet are connected; the heavy metal removal unit 123 is used to remove heavy metals in the hardened material to form a heavy metal-removed material;

[0124] The second solid-liquid separation unit 124 has an inlet for the material after heavy metal removal, an outlet for the solid phase material after separation, and an outlet for the liquid phase material after separation; the outlet for the material after heavy metal removal is connected to the inlet for the material after heavy metal removal; the second solid-liquid separation unit 124 is used to separate the liquid phase material containing potassium chloride and sodium chloride from the material after heavy metal removal;

[0125] The first solid-liquid separation unit 121 uses a belt filter and / or a plate-frame filter press; the second solid-liquid separation unit 124 uses a belt filter and / or a plate-frame filter press.

[0126] Through the above-mentioned design, the present application first separates the solid phase from the fly ash, then removes the useless ions in the liquid phase, and finally removes the solid phase precipitate, retaining the separated liquid phase, thereby retaining as many sodium ions, potassium ions, and chloride ions as possible that are useful for subsequent reactions, thereby making full use of the useful ions, improving the efficiency of subsequent reactions, ensuring product purity, and reducing side reactions.

[0127] The processing system also includes a solid waste storage unit 76; the fly ash solid phase material outlet and the separated solid phase material outlet are respectively connected to the inlet of the solid waste storage unit 76.

[0128] In some embodiments, the first separation unit 40 includes:

[0129] The third solid-liquid separation unit 41 has a carbonized material inlet, a sodium bicarbonate outlet, and an ammonium chloride-containing material outlet; the third solid-liquid separation unit 41 is used to separate sodium bicarbonate and ammonium chloride-containing materials from the carbonized material;

[0130] The salting-out unit 42 has an ammonium chloride-containing material inlet, a salting-out salt inlet, and a salted-out material outlet; the ammonium chloride-containing material outlet is connected to the ammonium chloride-containing material inlet; the sodium chloride outlet is connected to the salting-out salt inlet; the salting-out unit 42 is used to separate ammonium chloride from the ammonium chloride-containing material using sodium chloride to form an ammonium chloride solid-liquid mixture;

[0131] The fourth solid-liquid separation unit 43 has a post-salting out material inlet, an ammonium chloride outlet, and a fourth solid-liquid separation liquid phase material outlet; the post-salting out material outlet is connected to the post-salting out material inlet; the fourth solid-liquid separation liquid phase material outlet is connected to the salt water inlet of the ammonium salt water unit 20; the fourth solid-liquid separation unit 43 is used to separate ammonium chloride from the ammonium chloride solid-liquid mixture;

[0132] The third solid-liquid separation unit 41 adopts a belt filter and / or a plate-frame filter press device; the fourth solid-liquid separation unit 43 adopts a belt filter and / or a plate-frame filter press device.

[0133] The present application can fully extract the ammonium chloride through the above design, thereby ensuring the purity of the ammonium chloride.

[0134] In some embodiments, the treatment system further includes a sodium chloride storage unit 74, and the outlet of the sodium chloride storage unit 74 is connected to the salt inlet for salting out. In order to fully separate the ammonium chloride, the present application adopts the method of salting out, and the sodium chloride used for the salting out also comes from the sodium chloride separated from the fly ash, and can be obtained by connecting to the sodium chloride outlet of the fly ash separation unit, or the sodium chloride separated from the fly ash can be first stored in the transfer unit, and the salt used at each location is then connected to the transfer unit to obtain the sodium chloride.

[0135] In some embodiments, the reaction unit 60 comprises:

[0136] The first double decomposition reaction unit 61 has a potassium chloride inlet, a sodium sulfate inlet, a reaction water inlet and a first decomposition material outlet; the first double decomposition reaction unit 61 is used to perform a first double decomposition reaction on potassium chloride and a metallurgical byproduct sodium sulfate to generate a double decomposition material containing glauberite and sodium chloride;

[0137] The fifth solid-liquid separation unit 62 has a first decomposition material inlet, a glauberite outlet and a sodium chloride-containing liquid phase material outlet; the first decomposition material outlet is connected to the first decomposition material inlet; the fifth solid-liquid separation unit 62 is used to separate glauberite and a liquid phase material containing sodium chloride from the double decomposition material containing glauberite and sodium chloride;

[0138] The second double decomposition reaction unit 63 has a glauberite inlet, a potassium chloride inlet for the second double decomposition reaction, a water inlet for the second double decomposition reaction, and an outlet for a material containing potassium sulfate; the glauberite outlet is connected to the glauberite inlet; the second double decomposition reaction unit 63 is used to react glauberite and potassium chloride to generate a material containing potassium sulfate;

[0139] The sixth solid-liquid separation unit 64 has a potassium sulfate-containing material inlet and a potassium sulfate outlet; the potassium sulfate-containing material outlet is connected to the potassium sulfate-containing material inlet; the sixth solid-liquid separation unit 64 is used to separate potassium sulfate from the potassium sulfate-containing material.

[0140] The present application designs the above reaction route, wherein potassium chloride, sodium sulfate and water first react to generate a glauberite intermediate product and sodium chloride and other products, and then the sodium chloride is separated, and then the glauberite and potassium chloride are further reacted to generate potassium sulfate, so that potassium chloride and sodium sulfate can be fully reacted to achieve the purpose of fully utilizing the waste sodium sulfate and obtaining high-purity potassium sulfate.

[0141] In some embodiments, the reaction unit 60 also includes a second evaporation crystallization unit 65, which has a sodium chloride-containing liquid phase material inlet, a second evaporation water outlet, a second evaporation mother liquor outlet, and a second evaporation crystallization sodium chloride outlet; the sodium chloride-containing liquid phase material outlet is connected to the sodium chloride-containing liquid phase material inlet; the second evaporation crystallization unit 65 is used to evaporate and crystallize sodium chloride from the liquid phase material containing sodium chloride. The above-mentioned return routes designed in this application make full use of the water and sodium chloride generated in the second evaporation crystallization process. The water can be supplied to saturated brine water or reaction water, and the sodium chloride can be supplied to saturated brine salt or salting out salt, and finally the product becomes a reactant, which is recycled, making full use of waste resources and saving resources.

[0142] In some embodiments, the first double decomposition reaction unit 61 also has a second evaporation mother liquor inlet and a sixth separation clear liquor inlet; the sixth solid-liquid separation unit 64 also has a sixth separation clear liquor outlet; the second evaporation mother liquor outlet is connected to the second evaporation mother liquor inlet; the sixth separation clear liquor outlet is connected to the sixth separation clear liquor inlet. The above-mentioned return route designed by the present application can recycle the separated substances containing unreacted sodium sulfate, potassium salt, etc., to achieve recycling and save resources.

[0143] In some embodiments, the treatment system further includes a distilled water storage unit 73; the outlet of the distilled water storage unit 73 is respectively connected to the reaction water inlet of the first double decomposition reaction unit 61 and the second double decomposition reaction water inlet of the second double decomposition reaction unit 63; the second evaporated water outlet of the second evaporation crystallization unit 65 is connected to the inlet of the distilled water storage unit 73. The treatment system further includes a sodium chloride storage unit 74, and the second evaporated crystallization sodium chloride outlet of the second evaporation crystallization unit 65 is connected to the inlet of the sodium chloride storage unit 74. The present application realizes the recycling of water and sodium chloride in the second evaporation crystallization process by designing a return route; in the water or sodium chloride circulation process, the produced water outlet can be connected to the water inlet of each place to supply water, or the produced water can be first stored in the transfer unit, and the water used at each place is then connected to the transfer unit to take water, and the production and utilization of sodium chloride can also be designed in the same way.

[0144] In some embodiments, the first metathesis reaction unit 61 and the second metathesis reaction unit 63 use a reactor device; the fifth solid-liquid separation unit 62 uses a belt filter and / or a plate-frame filter press device; the sixth solid-liquid separation unit 64 uses a belt filter and / or a plate-frame filter press device; the second evaporation crystallization unit 65 uses a multiple-effect evaporation device and / or a mechanical vapor recompression device. The above devices are used in this application to improve reaction efficiency, separation efficiency, etc.

[0145] According to the second aspect of the present application, a method for the coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas is provided, wherein the above-mentioned coordinated treatment system is used; the method comprises the following steps:

[0146] Step 1: Treat the waste incineration fly ash to separate potassium chloride and sodium chloride;

[0147] Step 2: using sodium chloride, water and ammonia to form a saturated ammonium brine;

[0148] Step 3: using saturated ammonium salt water and non-ferrous smelting flue gas to carry out carbonization reaction to obtain a carbonized material containing sodium bicarbonate and ammonium chloride;

[0149] Step 4: Separating sodium bicarbonate and ammonium chloride from the carbonized material containing sodium bicarbonate and ammonium chloride;

[0150] Step 5: thermally decomposing sodium bicarbonate to obtain sodium carbonate;

[0151] Step 6: Mix potassium chloride, sodium sulfate and water, react them, and separate potassium sulfate from the reaction product.

[0152] The above-mentioned reaction method designed in the present application, combined with the above-mentioned treatment system of the present application, can fully realize the coordinated utilization of fly ash, metallurgical waste gas, and by-product sodium sulfate, and thus obtain high value-added products such as sodium carbonate, ammonium chloride and potassium sulfate. The reaction method is simple to operate and has high efficiency.

[0153] In some embodiments, the specific process of step 1 includes:

[0154] Step 1-1: firstly wash the fly ash with water to form a solid-liquid mixture, and then separate the solid-liquid mixture to obtain a liquid material containing potassium chloride and sodium chloride;

[0155] Step 1-2: performing a first evaporation crystallization on the liquid phase material containing potassium chloride and sodium chloride to obtain first evaporated water, sodium chloride and a mother liquor containing potassium chloride, respectively;

[0156] Step 1-3: Cooling and crystallizing the potassium chloride-containing mother liquor to separate potassium chloride.

[0157] In some embodiments, the specific process of step 6 includes:

[0158] Step 6-1: Mix potassium chloride, sodium sulfate and water to perform a first double decomposition reaction to obtain a double decomposition material containing glauberite and sodium chloride;

[0159] Step 6-2: performing solid-liquid separation on the double decomposition material containing glauberite and sodium chloride to obtain a liquid phase material containing glauberite and sodium chloride;

[0160] Step 6-3: Mixing glauberite, potassium chloride and water, and performing a second double decomposition reaction to obtain a material containing potassium sulfate;

[0161] Step 6-4: performing solid-liquid separation on the material containing potassium sulfate to obtain potassium sulfate.

[0162] In some embodiments, the temperature of the pyrolysis reaction is 100-200° C. The pyrolysis temperature used in the present application can fully pyrolyze sodium bicarbonate into sodium carbonate without generating any byproducts.

[0163] In some embodiments, the carbon dioxide operating pressure of the carbonization reaction is 0.3-0.6 MPa. The present application uses this carbon dioxide operating pressure to fully precipitate the dissolved sodium ions into sodium bicarbonate solid.

[0164] In some embodiments, the operating temperature of the carbonization reaction is 30° C. to 60° C. The present application adopts this operating temperature to fully precipitate the dissolved sodium ions into sodium bicarbonate solid.

[0165] In some embodiments, the specific process of step 1-1 includes: first washing the fly ash with water to form a solid-liquid mixture, performing a first solid-liquid separation to separate the fly ash liquid phase material; the fly ash liquid phase material is successively subjected to hardness removal and heavy metal removal treatments, and then a second solid-liquid separation is performed to obtain a liquid phase material containing potassium chloride and sodium chloride; wherein the hardness removal agent is sodium hydroxide and sodium carbonate, and the hardness removal is performed using a double alkali method; the heavy metal removal agent is sodium sulfide. The above-mentioned agents are selected in this application to fully remove calcium, magnesium ions and heavy metal ions in the fly ash liquid phase.

[0166] In some embodiments, the process of step 6-2 further includes performing a second evaporation crystallization on the liquid phase material containing sodium chloride to obtain second evaporated water, sodium chloride and a second evaporated mother liquor; the second evaporated mother liquor, the clear liquid after solid-liquid separation in step 6-4 and the material in step 6-1 are mixed to perform a first double decomposition reaction.

[0167] In some embodiments, the temperature of the first evaporation crystallization is 90°C to 120°C; the temperature of the second evaporation crystallization is 90°C to 120°C; the temperature of the cooling crystallization is 10°C to 35°C; in the reaction of potassium chloride, sodium sulfate and water, the molar ratio of potassium chloride to sodium sulfate is 2:1 to 3:1; the temperature of the first double decomposition reaction is 30°C to 60°C; the temperature of the second double decomposition reaction is 25°C to 60°C.

[0168] In the two evaporation crystallization processes of the present invention, a suitable crystallization temperature is used according to the characteristics of the sodium chloride to be crystallized, so that sodium chloride with higher purity can be obtained; the above cooling crystallization temperature can be used to fully crystallize potassium chloride to ensure the purity of potassium chloride; and the two double decomposition reaction temperatures are used to make potassium chloride and sodium sulfate fully react in two-step reactions to obtain a high-purity potassium sulfate product.

[0169] The fly ash, sodium sulfate waste salt and non-ferrous metallurgical flue gas coordinated treatment system and treatment method designed in the present application first extract sodium chloride and potassium chloride from the waste incineration fly ash, then make full use of the sodium chloride and external ammonia to form saturated ammonium brine, and then use the saturated ammonium brine to treat the non-ferrous metallurgical flue gas to form high value-added products sodium carbonate and ammonium chloride, wherein sodium carbonate is formed by carbon dioxide in the non-ferrous metallurgical flue gas and sodium ions in the waste fly ash, and ammonium chloride is formed by chloride ions in the waste fly ash and external ammonia; finally, potassium chloride in the fly ash is reacted with worthless non-ferrous metallurgical by-product industrial sodium sulfate to form high value-added sodium carbonate and ammonium chloride. The value-added product potassium sulfate; the high value-added products obtained are sodium carbonate, ammonium chloride and potassium sulfate. The potassium sulfate product obtained meets the GB / T20406-2017 agricultural potassium sulfate powder crystalline qualified product standard, the ammonium chloride product obtained meets the GB / T2946-2018 industrial ammonium chloride qualified product standard, and the sodium carbonate product obtained meets the GB / T210-2022 industrial sodium carbonate Class II qualified product standard; the above-mentioned treatment system designed in this application realizes the recycling of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas waste resources to the greatest extent, while also effectively reducing the harm of hazardous waste to the environment.

[0170] The present application is further described in detail below in conjunction with specific embodiments. These embodiments should not be construed as limiting the scope of protection claimed in the present application.

[0171] The fly ash used in the embodiments of the present application comes from the fly ash generated by waste incineration, the flue gas comes from the flue gas carbon dioxide generated in the non-ferrous metallurgical process, and the by-product sodium sulfate comes from the sodium sulfate after the non-ferrous metallurgical wastewater is treated.

[0172] Example 1

[0173] A system for coordinating the treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas, such as Figure 1As shown, it includes: a fly ash washing unit 11, a first solid-liquid separation unit 121, a hardness removal unit 122, a heavy metal removal unit 123, a second solid-liquid separation unit 124, a first evaporation crystallization unit 13, a cooling crystallization unit 14, a potassium chloride storage unit 75, a distilled water storage unit 73, a sodium chloride storage unit 74, a saturated brine unit 21, a saturated ammonium brine unit 22, a carbonization unit 30, a third solid-liquid separation unit 41, a pyrolysis unit 50, a salting-out unit 42, a fourth solid-liquid separation unit 43, an ammonium chloride storage unit 71, a sodium carbonate storage unit 70, a first double decomposition reaction unit 61, a fifth solid-liquid separation unit 62, a second evaporation crystallization unit 65, a second double decomposition reaction unit 63, a sixth solid-liquid separation unit 64, a potassium sulfate storage unit 72, and a solid waste storage unit 76;

[0174] The input end of the fly ash washing unit 11 can be connected to the fly ash and distilled water storage unit 73, and the output end of the fly ash washing unit 11 is connected to the input end of the first solid-liquid separation unit 121; the output end of the first solid-liquid separation unit 121 includes a liquid output end and a solid output end, the liquid output end of the first solid-liquid separation unit 121 is connected to the liquid input end of the hardness removal unit 122, and the solid output end is connected to the input end of the solid waste storage unit 76; the input end of the hardness removal unit 122 includes a liquid input end and a reagent input end, the reagent input end of the hardness removal unit 122 is connected to the outside, and the output end of the hardness removal unit 122 is connected to the liquid input end of the heavy metal removal unit; the heavy metal removal unit The input end of 123 includes a liquid input end and a reagent input end, the reagent input end of the heavy metal removal unit 123 is connected to the outside, and the output end of the heavy metal removal unit 123 is connected to the input end of the second solid-liquid separation unit 124; the output end of the second solid-liquid separation unit 124 includes a solid output end and a liquid output end, the solid output end of the second solid-liquid separation unit 124 is connected to the input end of the solid waste storage unit, and the liquid output end of the second solid-liquid separation unit 124 is connected to the raw material input end of the first evaporation crystallization unit 13; the input end of the first evaporation crystallization unit 13 includes a raw material input end and a mother liquor input end, and the mother liquor input end is connected to the liquid output end of the cooling crystallization unit 14, The output end of an evaporation crystallization unit 13 includes a distilled water output end, a mother liquor output end and a sodium chloride output end, the distilled water output end is connected to the distilled water storage unit 73, the mother liquor output end is connected to the input end of the cooling crystallization unit 14, and the sodium chloride output end is connected to the input end of the sodium chloride storage unit 74; the input end of the sodium chloride storage unit 74 includes a first evaporation crystallization unit 13 sodium chloride input end and a second evaporation crystallization unit 65 sodium chloride input end, the second evaporation crystallization unit sodium chloride input end is connected to the sodium chloride output end of the second evaporation crystallization unit, and the output end of the sodium chloride storage unit 74 includes a saturated brine unit direction output end and a salting-out unit direction output end, the saturated brine unit direction output end and the salting-out unit direction output end. The output end is connected to the solid input end of the saturated brine unit, and the direction output end of the salting-out unit is connected to the solid input end of the salting-out unit; the input end of the cooling crystallization unit is connected to the mother liquor output end of the first evaporation crystallization unit, and the output end of the cooling crystallization unit includes a solid output end and a liquid output end, and the solid output end is connected to the solid input end of the potassium chloride storage unit 75; the output end of the potassium chloride storage unit 75 includes a first double decomposition reaction direction output end and a second double decomposition reaction direction output end, the first double decomposition reaction direction output end is connected to the potassium chloride input end of the first double decomposition reaction unit, and the second double decomposition reaction direction output end is connected to the potassium chloride input end of the second double decomposition reaction unit;

[0175] The input end of the saturated brine unit 21 includes a distilled water input end, a solid input end and a mother liquor input end, the mother liquor input end is connected to the liquid output end of the fourth solid-liquid separation unit 43, and the output end of the saturated brine unit 21 is connected to the liquid input end of the saturated ammonium brine unit 22; the input end of the saturated ammonium brine unit 22 includes a liquid input end and a gas input end, the gas input end is communicated with the outside, and the output end of the saturated ammonium brine unit 22 is connected to the liquid input end of the carbonization unit 30; the input end of the carbonization unit 30 includes a liquid input end, a non-ferrous smelting flue gas input end and a pyrolysis flue gas input end, the non-ferrous smelting flue gas input end is connected to the outside, the pyrolysis flue gas input end is connected to the flue gas output end of the pyrolysis unit 50, and the output end of the carbonization unit 30 is connected to the input end of the third solid-liquid separation unit 41; The output end includes a liquid output end and a solid output end, the liquid output end is connected to the liquid feed end of the salting-out unit 42, and the solid output end is connected to the feed end of the pyrolysis unit 50; the output end of the pyrolysis unit includes a flue gas output end and a solid output end, and the solid output end is connected to the feed end of the sodium carbonate storage unit; the output end of the sodium carbonate storage unit 70 is connected to the outside; the input end of the salting-out unit 42 includes a solid feed end and a liquid feed end, and the output end of the salting-out unit 42 is connected to the input end of the fourth solid-liquid separation unit 43; the output end of the fourth solid-liquid separation unit 43 includes a solid output end and a liquid output end, the solid output end is connected to the input end of the ammonium chloride storage unit 71, and the liquid output end is connected to the mother liquor input end of the saturated brine unit 21; the output end of the ammonium chloride storage unit 71 is connected to the outside;

[0176] The input end of the first double decomposition reaction unit 61 includes a potassium chloride input end, a by-product sodium sulfate input end, a distilled water input end, a second evaporation mother liquor input end and a sixth clear liquid input end, the by-product sodium sulfate input end is connected to the outside, the distilled water input end is connected to the output end of the distilled water storage unit, the second evaporation mother liquor input end is connected to the mother liquor output end of the second evaporation crystallization unit 65, the sixth clear liquid input end is connected to the liquid output end of the sixth solid-liquid separation unit 64, the output end of the first double decomposition reaction unit 61 is connected to the feed end of the fifth solid-liquid separation unit 62; the output end of the fifth solid-liquid separation unit 62 includes a solid output end and a liquid output end, the solid output end is connected to the intermediate input end of the second double decomposition reaction unit 63, the liquid The output end of the second evaporation crystallization unit 65 includes a mother liquor output end, a sodium chloride output end and a distilled water output end, and the distilled water output end is connected to the input end of the distilled water storage unit; the input end of the second double decomposition reaction unit 63 includes a potassium chloride input end, an intermediate input end and a distilled water input end, and the distilled water input end is connected to the output end of the distilled water storage unit 73, and the output end of the second double decomposition reaction unit 63 is connected to the input end of the sixth solid-liquid separation unit 64, and the output end of the sixth solid-liquid separation unit 64 includes a solid output end and a liquid output end, and the solid output end is connected to the input end of the potassium sulfate storage unit 72, and the output end of the potassium sulfate storage unit 72 is connected to the outside.

[0177] In the above-mentioned embodiment 1, the first solid-liquid separation unit, the second solid-liquid separation unit, the third solid-liquid separation unit, the fourth solid-liquid separation unit, the fifth solid-liquid separation unit and the sixth solid-liquid separation unit adopt a belt filter or a plate and frame filter press; the first evaporation crystallization unit and the second evaporation crystallization unit adopt multiple-effect evaporation or MVR; the saturated ammonia brine unit adopts an ammonia absorption tower; the carbonization unit adopts a carbonization tower; the pyrolysis unit adopts a rotary kiln pyrolysis system; the first double decomposition reaction unit and the second double decomposition reaction unit adopt a reactor system.

[0178] Example 2

[0179] A method for synergistically treating fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas, using the treatment system of Example 1; the treatment method comprises the following steps:

[0180] Step 1: The collected fly ash is transported to the fly ash washing unit for water washing, and the soluble substances are dissolved in water as much as possible. The distilled water comes from the distilled water storage unit; the solid-liquid mixture after water washing is transported to the first solid-liquid separation unit, and the solid-liquid separation is carried out using a belt filter; the solid obtained by solid-liquid separation is transported to the solid waste storage unit as solid waste, and the obtained liquid is transported to the hardness removal unit; sodium hydroxide and sodium carbonate are added to the hardness removal unit, and the hardness removal is carried out using the double alkali method. The sodium carbonate used is the sodium carbonate produced by the pyrolysis unit; the liquid obtained after hardness removal is transported to the heavy metal removal unit, and sodium sulfide is added to remove the heavy metal ions therein. The material after the weight removal treatment is passed into the second solid-liquid separation unit, and the solid-liquid separation is performed using a belt filter; the solid obtained from the solid-liquid separation is transported to the solid waste storage unit as solid waste, and the obtained liquid is transported to the first evaporation crystallization unit; the material is subjected to MVR operation in the first evaporation crystallization unit, and the operating temperature is 100°C, the obtained sodium chloride crystals are transported to the sodium chloride storage unit, the obtained distilled water is transported to the distilled water storage unit, and the discharged mother liquor enters the cooling crystallization unit; the operating temperature of the cooling crystallization unit is 25°C, the obtained potassium chloride is passed into the potassium chloride storage unit, and the obtained mother liquor returns to the first evaporation crystallization unit;

[0181] Step 2: sodium chloride from the sodium chloride storage unit, distilled water from the distilled water storage unit, and the clear liquid from the fourth solid-liquid separation unit are introduced into the saturated brine unit to prepare saturated brine; the saturated brine and ammonia are introduced into the saturated ammonia brine unit and an ammonia absorption tower is used to prepare saturated ammonia brine; the obtained saturated ammonia brine is introduced into the carbonization unit, and carbonization reaction occurs with non-ferrous smelting flue gas from the outside and carbon dioxide flue gas from the pyrolysis unit in the carbonization tower, and the operating pressure of carbon dioxide is 0.5MPa and the operating temperature is 40°C; the product obtained from the carbonization reaction unit is introduced into the third solid-liquid separation unit, and solid-liquid separation is performed using a belt filter; the solid obtained from the solid-liquid separation is introduced into the pyrolysis unit, and the obtained liquid is introduced into the salt The pyrolysis unit is a rotary kiln with a reaction temperature of 150°C. The sodium carbonate product produced is tested to meet the GB / T210-2022 industrial sodium carbonate Class II qualified product standard and is transported to the sodium carbonate storage unit, and the pyrolysis flue gas is transported to the carbonization unit; the clear liquid obtained from the third solid-liquid separation unit is transported to the salting-out unit to undergo salting-out reaction with the sodium chloride from the sodium chloride storage unit; the solid-liquid mixture obtained from the salting-out unit is transported to the fourth solid-liquid separation unit, and a belt filter is used for solid-liquid separation; the ammonium chloride product obtained from the solid-liquid separation is tested to meet the GB / T2946-2018 industrial ammonium chloride qualified product standard and is transported to the ammonium chloride storage unit, and the resulting liquid returns to the saturated brine unit;

[0182] Step 3: The by-product sodium sulfate from the outside, the potassium chloride from the potassium chloride storage unit, the distilled water from the distilled water storage unit, the mother liquor from the second evaporation crystallization unit and the clear liquid from the sixth solid-liquid separation unit are transported to the first double decomposition reaction unit, and the double decomposition reaction is carried out in a reactor, the molar feed ratio of potassium chloride to sodium sulfate is 2:1, and the operating temperature is 40°C; the material obtained by the double decomposition reaction is transported to the fifth solid-liquid separation unit, and the solid-liquid separation is carried out using a belt filter; the obtained solid is potassium glauberite, which is input into the second double decomposition reaction unit, and the obtained liquid is transported to the second evaporation crystallization unit; the second evaporation crystallization unit uses MVR, the operating temperature is 100°C, and the obtained mother liquor returns to the first The double decomposition reaction unit, the obtained sodium chloride is returned to the sodium chloride storage unit, and the obtained distilled water is returned to the distilled water storage unit; the potassium chloride from the potassium chloride storage unit, the distilled water from the distilled water storage unit and the solid from the fifth solid-liquid separation unit are transported to the second double decomposition reaction unit, and the double decomposition reaction is carried out in a reactor with an operating temperature of 40°C; the product of the second double decomposition reaction unit is transported to the sixth solid-liquid separation unit, and a belt filter is used for solid-liquid separation; the obtained potassium sulfate solid product is tested to meet the GB / T20406-2017 agricultural potassium sulfate powder crystalline qualified product standard, and is transported to the potassium sulfate storage unit for external sale, and the obtained liquid is returned to the first double decomposition reaction unit.

[0183] The coordinated treatment system and process of this application can treat 50,000 tons of fly ash from domestic waste annually; 20,000 tons of sodium sulfate produced by the zero discharge of non-ferrous metallurgical wastewater annually; and 3.6×107Nm 3 The system operates stably with an annual operation time of 7,200 hours. 30,000 tons of potassium sulfate are obtained annually, and the obtained product meets the GB / T20406-2017 agricultural potassium sulfate powder crystalline qualified product standard and is sold externally; 25,000 tons of ammonium chloride are obtained annually, and the obtained product meets the GB / T2946-2018 industrial ammonium chloride qualified product standard and is sold externally; 20,000 tons of sodium carbonate are obtained annually, and the obtained product meets the GB / T210-2022 industrial sodium carbonate Class II qualified product standard and is sold externally.

[0184] In the collaborative treatment system of the present application, the steam condensate obtained from the first evaporation crystallization unit and the second evaporation crystallization unit can be returned to the distilled water storage unit as fly ash washing unit, saturated brine unit, first double decomposition unit, and second double decomposition unit dissolution water for recycling, which can save a lot of tap water consumption; the carbon dioxide flue gas generated by the pyrolysis unit can be returned to the carbonization unit for recycling; the sodium chloride required by the entire system is the sodium chloride generated by the system itself, the required potassium chloride is the potassium chloride generated by the system itself, and the required raw materials are all hazardous wastes recovered from waste-producing enterprises, the raw material cost is zero, and it has good economic value.

[0185] It should be noted that the terms "first", "second", etc. in the specification and claims of the present application are used to distinguish similar objects, and are not necessarily used to describe a specific order or sequence. It should be understood that the terms used in this way can be interchangeable where appropriate, so that the embodiments of the present application described herein can be implemented in an order other than those described herein, for example.

[0186] The above description is only the preferred embodiment of the present application and is not intended to limit the present application. For those skilled in the art, the present application may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. A fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system, characterized in that: The processing system comprises: A fly ash separation unit (10) having a fly ash inlet, a fly ash water inlet, a potassium chloride outlet and a sodium chloride outlet, wherein the fly ash separation unit (10) is used to separate potassium chloride and sodium chloride from waste incineration fly ash; The ammonium brine unit (20) has an ammonia gas inlet, a salt water inlet, a salt water inlet and a saturated ammonium brine outlet; the sodium chloride outlet is connected to the salt water inlet; the ammonium brine unit (20) is used to mix water, the sodium chloride and ammonia gas to form a saturated ammonium brine; The carbonization unit (30) has a saturated ammonium salt water inlet, a smelting flue gas inlet and a carbonized material outlet; the saturated ammonium salt water outlet is connected to the saturated ammonium salt water inlet; the carbonization unit (30) is used to carbonize the saturated ammonium salt water and the non-ferrous smelting flue gas to generate a carbonized material containing sodium bicarbonate and ammonium chloride; A first separation unit (40) has a carbonized material inlet, a sodium bicarbonate outlet and an ammonium chloride outlet; the carbonized material outlet is connected to the carbonized material inlet; the first separation unit (40) is used to separate sodium bicarbonate and ammonium chloride from the carbonized material; A pyrolysis unit (50) has a sodium bicarbonate inlet, a pyrolysis fume outlet and a sodium carbonate outlet; the sodium bicarbonate outlet is connected to the sodium bicarbonate inlet; the pyrolysis unit (50) is used to pyrolyze the sodium bicarbonate into sodium carbonate; The reaction unit (60) has a potassium chloride inlet, a sodium sulfate inlet, a reaction water inlet and a potassium sulfate outlet; the potassium chloride outlet is connected to the potassium chloride inlet; the reaction unit is used to carry out a double decomposition reaction between the metallurgical by-product sodium sulfate waste salt and the potassium chloride and separate potassium sulfate from the decomposed materials.

2. The fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system according to claim 1 is characterized in that: The treatment system further comprises a sodium carbonate storage unit (70), an ammonium chloride storage unit (71), a potassium sulfate storage unit (72), a distilled water storage unit (73), a sodium chloride storage unit (74) and a potassium chloride storage unit (75); The sodium chloride outlet is connected to the inlet of the sodium chloride storage unit (74), and the outlet of the sodium chloride storage unit (74) is connected to the brine inlet of the ammonium brine unit (20); The potassium chloride outlet is connected to the inlet of the potassium chloride storage unit (75), and the outlet of the potassium chloride storage unit (75) is connected to the potassium chloride inlet of the reaction unit (60); The outlet of the distilled water storage unit (73) is respectively connected to the fly ash water inlet of the fly ash separation unit (10), the salt water inlet of the ammonium salt water unit (20), and the reaction water inlet of the reaction unit (60); The sodium carbonate outlet of the pyrolysis unit (50) is connected to the inlet of the sodium carbonate storage unit (70); the ammonium chloride outlet of the first separation unit (40) is connected to the inlet of the ammonium chloride storage unit (71); and the potassium sulfate outlet of the reaction unit (60) is connected to the inlet of the potassium sulfate storage unit (72).

3. The fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system according to claim 1 is characterized in that: The fly ash separation unit (10) comprises: A fly ash washing unit (11) having the fly ash inlet, the fly ash water inlet and the solid-liquid mixture outlet; the fly ash washing unit (11) is used to wash fly ash to form a solid-liquid mixture; A second separation unit (12) has a solid-liquid mixture inlet and a separated liquid material outlet; the solid-liquid mixture outlet is connected to the solid-liquid mixture inlet; the second separation unit (12) is used to separate the liquid material containing potassium chloride and sodium chloride from the solid-liquid mixture; The first evaporation crystallization unit (13) has an inlet for separated liquid phase material, an inlet for cooling and crystallizing mother liquor, the sodium chloride outlet, a first evaporation water outlet and an outlet for mother liquor containing potassium chloride; the outlet for separated liquid phase material is connected to the inlet for separated liquid phase material; the first evaporation crystallization unit (13) is used to evaporate and crystallize the sodium chloride from the liquid phase material containing potassium chloride and sodium chloride and separate the mother liquor containing potassium chloride; A cooling crystallization unit (14) comprises an inlet for a mother liquor containing potassium chloride, an outlet for cooling and crystallizing the mother liquor and the potassium chloride outlet; the outlet for the mother liquor containing potassium chloride is connected to the inlet for the mother liquor containing potassium chloride; the outlet for cooling and crystallizing the mother liquor is connected to the inlet for cooling and crystallizing the mother liquor; the cooling crystallization unit (14) is used for cooling and crystallizing the potassium chloride from the mother liquor containing potassium chloride; the treatment system further comprises a distilled water storage unit (73), the first evaporated water outlet is connected to the inlet of the distilled water storage unit (73); And / or, the ammonium salt water unit (20) comprises: A saturated brine unit (21) having a brine inlet, a brine water inlet and a saturated brine outlet; the saturated brine unit (21) is used to mix the sodium chloride and water to form saturated brine; The saturated ammonium brine unit (22) comprises a saturated brine inlet, the ammonia gas inlet and the saturated ammonium brine outlet; the saturated brine outlet is connected to the saturated brine inlet; the saturated ammonium brine unit is used to form the saturated ammonium brine from ammonia gas and the saturated brine; and / or the pyrolysis flue gas outlet of the pyrolysis unit (50) is connected to the smelting flue gas inlet of the carbonization unit (30).

4. The fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system according to claim 3 is characterized in that: The second separation unit (12) comprises: A first solid-liquid separation unit (121) has an inlet for the solid-liquid mixture, an outlet for the fly ash solid phase material, and an outlet for the fly ash liquid phase material; the first solid-liquid separation unit (121) is used to separate the fly ash liquid phase material from the solid-liquid mixture; The hardness removal unit (122) has a fly ash liquid phase material inlet, a hardness removal agent inlet and a hardness removed material outlet; The fly ash liquid phase material outlet is connected to the fly ash liquid phase material inlet; the hardness removal unit is used to remove calcium ions and magnesium ions in the fly ash liquid phase material to form a hardness-removed material; The heavy metal removal unit (123) has a hardened material inlet, a heavy metal removal agent inlet and a heavy metal removal material outlet; the hardened material inlet and the hardened material outlet are connected; the heavy metal removal unit (123) is used to remove heavy metals in the hardened material to form a heavy metal-removed material; The second solid-liquid separation unit (124) has an inlet for the material after heavy metal removal, an outlet for the solid phase material after separation and an outlet for the liquid phase material after separation; the outlet for the material after heavy metal removal is connected to the inlet for the material after heavy metal removal; the second solid-liquid separation unit (124) is used to separate the liquid phase material containing potassium chloride and sodium chloride from the material after heavy metal removal; the treatment system also includes a solid waste storage unit (76); the fly ash solid phase material outlet and the outlet for the solid phase material after separation are respectively connected to the inlet of the solid waste storage unit (76).

5. The fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system according to any one of claims 1 to 4, characterized in that: The first separation unit (40) comprises: The third solid-liquid separation unit (41) has the carbonized material inlet, the sodium bicarbonate outlet and the ammonium chloride-containing material outlet; the third solid-liquid separation unit (41) is used to separate the sodium bicarbonate and the ammonium chloride-containing material from the carbonized material respectively; The salting-out unit (42) comprises an ammonium chloride-containing material inlet, a salting-out salt inlet and a salted-out material outlet; the ammonium chloride-containing material outlet is connected to the ammonium chloride-containing material inlet; the sodium chloride outlet is connected to the salting-out salt inlet; the salting-out unit (42) is used to separate ammonium chloride from the ammonium chloride-containing material using the sodium chloride to form an ammonium chloride solid-liquid mixture; The fourth solid-liquid separation unit (43) has a post-salting out material inlet, the ammonium chloride outlet, and a fourth solid-liquid separation liquid phase material outlet; the post-salting out material outlet is connected to the post-salting out material inlet; the fourth solid-liquid separation liquid phase material outlet is connected to the salt water inlet of the ammonium salt water unit (20); the fourth solid-liquid separation unit (43) is used to separate ammonium chloride from the ammonium chloride solid-liquid mixture; The treatment system further comprises a sodium chloride storage unit (74), the outlet of the sodium chloride storage unit (74) being connected to the salting-out salt inlet.

6. The fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system according to any one of claims 1 to 4, characterized in that: The reaction unit (60) comprises: The first metathesis reaction unit (61) has the potassium chloride inlet, the sodium sulfate inlet, the reaction water inlet and the first decomposition material outlet; the first metathesis reaction unit (61) is used to carry out a first metathesis reaction between the potassium chloride and the metallurgical by-product sodium sulfate to generate a metathesis material containing glauberite and sodium chloride; a fifth solid-liquid separation unit (62), comprising a first decomposition material inlet, a glauberite outlet and a sodium chloride-containing liquid phase material outlet; the first decomposition material outlet is connected to the first decomposition material inlet; the fifth solid-liquid separation unit (62) is used to separate glauberite and a sodium chloride-containing liquid phase material from the double decomposition material containing glauberite and sodium chloride; The second double decomposition reaction unit (63) has a glauberite inlet, a second double decomposition reaction potassium chloride inlet, a second double decomposition reaction water inlet and a potassium sulfate-containing material outlet; the glauberite outlet is connected to the glauberite inlet; the second double decomposition reaction unit (63) is used to react glauberite and the potassium chloride to generate a potassium sulfate-containing material; The sixth solid-liquid separation unit (64) has a potassium sulfate-containing material inlet and the potassium sulfate outlet; the potassium sulfate-containing material outlet is connected to the potassium sulfate-containing material inlet; the sixth solid-liquid separation unit (64) is used to separate potassium sulfate from the potassium sulfate-containing material.

7. The fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas coordinated treatment system according to claim 6 is characterized in that: The reaction unit (60) further comprises a second evaporation crystallization unit (65), which has an inlet for a liquid phase material containing sodium chloride, a second evaporation water outlet, a second evaporation mother liquor outlet and a second evaporation crystallization sodium chloride outlet; the outlet for the liquid phase material containing sodium chloride is connected to the inlet for the liquid phase material containing sodium chloride; the second evaporation crystallization unit (65) is used for evaporating and crystallizing sodium chloride from the liquid phase material containing sodium chloride; The first metathesis reaction unit (61) further comprises a second evaporation mother liquor inlet and a sixth separation clear liquor inlet; the sixth solid-liquid separation unit (64) further comprises a sixth separation clear liquor outlet; the second evaporation mother liquor outlet is connected to the second evaporation mother liquor inlet; the sixth separation clear liquor outlet is connected to the sixth separation clear liquor inlet; The treatment system further comprises a distilled water storage unit (73); the outlet of the distilled water storage unit (73) is respectively connected to the reaction water inlet of the first metathesis reaction unit (61) and the second metathesis reaction water inlet of the second metathesis reaction unit (63); the second evaporated water outlet of the second evaporation crystallization unit (65) is connected to the inlet of the distilled water storage unit (73); The treatment system further comprises a sodium chloride storage unit (74), and the second evaporation and crystallization sodium chloride outlet of the second evaporation and crystallization unit (65) is connected to the inlet of the sodium chloride storage unit (74).

8. A method for the coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas, characterized in that: The processing method adopts the collaborative processing system according to any one of claims 1 to 7; the method comprises the following steps: Step 1: Treat the waste incineration fly ash to separate potassium chloride and sodium chloride; Step 2: using the sodium chloride, water and ammonia to form a saturated ammonium salt solution; Step 3: using the saturated ammonium salt water and the non-ferrous smelting flue gas to carry out a carbonization reaction to obtain a carbonized material containing sodium bicarbonate and ammonium chloride; Step 4: Separating sodium bicarbonate and ammonium chloride from the carbonized material containing sodium bicarbonate and ammonium chloride; Step 5: performing a pyrolysis reaction on the sodium bicarbonate to obtain sodium carbonate; Step 6: Mix and react the potassium chloride, sodium sulfate and water, and separate potassium sulfate from the reaction product.

9. The method for coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas according to claim 8, characterized in that: The specific process of step 1 includes: Step 1-1: firstly wash the fly ash with water to form a solid-liquid mixture, and then separate the solid-liquid mixture to obtain a liquid material containing potassium chloride and sodium chloride; Step 1-2: performing a first evaporation crystallization on the liquid phase material containing potassium chloride and sodium chloride to obtain first evaporated water, sodium chloride and a mother liquor containing potassium chloride, respectively; Step 1-3: cooling and crystallizing the potassium chloride-containing mother liquor to separate potassium chloride; and / or, the specific process of step 6 includes: Step 6-1: mixing the potassium chloride, sodium sulfate and water to perform a first double decomposition reaction to obtain a double decomposition material containing glauberite and sodium chloride; Step 6-2: performing solid-liquid separation on the double decomposition material containing glauberite and sodium chloride to obtain a liquid phase material containing glauberite and sodium chloride; Step 6-3: mixing the glauber's salt, the potassium chloride and water, and performing a second double decomposition reaction to obtain a material containing potassium sulfate; Step 6-4: performing solid-liquid separation on the material containing potassium sulfate to obtain potassium sulfate; And / or, the carbon dioxide operating pressure of the carbonization reaction in step 3 is 0.3MPa to 0.6MPa; And / or, the operating temperature of the carbonization reaction in step 3 is 30° C. to 60° C.; And / or, the molar ratio of the potassium chloride to the sodium sulfate in step 6 is (2-3):1; And / or, the temperature of the pyrolysis reaction is 100-200°C.

10. The method for coordinated treatment of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas according to claim 9, characterized in that: The specific process of step 1-1 includes: first washing the fly ash with water to form a solid-liquid mixture, performing a first solid-liquid separation to separate the fly ash liquid phase material; the fly ash liquid phase material is sequentially subjected to hardness removal and heavy metal removal treatments, and then performing a second solid-liquid separation to obtain the liquid phase material containing potassium chloride and sodium chloride; wherein the hardness removal agent is sodium hydroxide and sodium carbonate, and the hardness removal is performed by a double alkali method; the heavy metal removal agent is sodium sulfide; And / or, the process of step 6-2 further includes performing a second evaporation crystallization on the liquid phase material containing sodium chloride to obtain a second evaporated water, sodium chloride and a second evaporated mother liquor; the second evaporated mother liquor, the clear liquid after the solid-liquid separation in step 6-4 and the material in step 6-1 are mixed to perform the first double decomposition reaction; the temperature of the second evaporation crystallization is 90° C. to 120° C.; And / or, the temperature of the first evaporation crystallization is 90°C to 120°C; And / or, the cooling crystallization temperature is 10°C to 35°C; And / or, the temperature of the first metathesis reaction is 30° C. to 60° C.; And / or, the temperature of the second metathesis reaction is 25°C to 60°C.

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