Fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas co-processing system and method

Abstract

The application discloses a fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas cooperative treatment system and method, belonging to the field of chemical engineering environment. The treatment system comprises a fly ash separation unit for separating potassium chloride and sodium chloride from waste incineration fly ash; an ammonium salt water unit for forming saturated ammonium salt water from water, sodium chloride and ammonia; a carbonization unit for carbonizing saturated ammonium salt water and non-ferrous smelting flue gas to generate carbonized material containing sodium bicarbonate and ammonium chloride; a first separation unit for separating sodium bicarbonate and ammonium chloride from the carbonized material; a pyrolysis unit for pyrolyzing sodium bicarbonate into sodium carbonate; and a reaction unit for reacting sodium sulfate waste salt and potassium chloride and separating potassium sulfate. The system realizes the recycling of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas waste resources, and the obtained products, sodium carbonate, ammonium chloride and potassium sulfate, all meet the national standard requirements, have high use value, and also reduce the harm of hazardous waste to the environment.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of chemical industry environment, in particular to a fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas co-processing system and method. BACKGROUND

[0002] The main disposal methods of municipal solid waste are landfill, incineration and composting. Among them, incineration has become the main disposal method of municipal solid waste because it can effectively realize waste reduction. In the process of waste incineration, organic matter is oxidized into water and carbon dioxide and discharged into the atmosphere, and inorganic matter is mainly changed into solid particles with small particle size. Among these solid particles, the larger particles settle at the bottom of the incinerator and on the grate, and the fine particles enter the flue gas purification device. These fine particles account for about 50% of the total mass of 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 precipitator, bag filter, etc.). The smaller particles settle at the bottom of the flue or chimney and are called 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 non-ferrous metallurgical wastewater zero discharge, salts in wastewater are discharged in the form of miscellaneous salt.

[0004] The flue gas generated in the non-ferrous metallurgical process is treated to meet the emission standard before being discharged into the atmosphere, and contains a large amount of carbon dioxide which can cause greenhouse effect.

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

[0006] The main purpose of the present application is to provide a fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas co-processing system and method to solve the problem of waste of resources and pollution of the environment caused by the poor utilization of various waste resources in the prior art.

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

[0008] The fly ash separation unit has a fly ash inlet, a fly ash water inlet, a potassium chloride outlet and a sodium chloride outlet, and is used to separate potassium chloride and sodium chloride from the fly ash, respectively.

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

[0010] A carbonization unit having 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 make the saturated ammonium salt water and the non-ferrous smelting flue gas to carry out a carbonization reaction to generate a carbonized material containing sodium bicarbonate and ammonium chloride;

[0011] A first separation unit having 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] A pyrolysis unit having 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 sodium bicarbonate into sodium carbonate;

[0013] A reaction unit having a potassium chloride inlet, a sodium sulfate inlet, a water for reaction inlet, and a potassium sulfate outlet; the potassium chloride outlet is connected to the potassium chloride inlet; the reaction unit is used to make the metallurgical by-product sodium sulfate waste salt and potassium chloride to carry out a double decomposition reaction and separate potassium sulfate from the decomposition material.

[0014] Further, the processing system further comprises 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 salt for salt water inlet of the ammonium salt water 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 water for reaction 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 having a fly ash inlet, a fly ash water inlet, and a solid-liquid mixture outlet; the fly ash washing unit is configured to wash the fly ash to form a solid-liquid mixture;

[0021] a second separation unit having 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 configured to separate a liquid material containing potassium chloride and sodium chloride from the solid-liquid mixture;

[0022] a first evaporative crystallization unit having a separated liquid material inlet, a cooling crystallization mother liquor inlet, a sodium chloride outlet, a first evaporated 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 evaporative crystallization unit is configured to evaporative crystallize sodium chloride from the liquid material containing potassium chloride and sodium chloride and separate a potassium chloride containing mother liquor;

[0023] a cooling crystallization unit having 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; the cooling crystallization unit is configured to cooling crystallize potassium chloride from the potassium chloride containing mother liquor.

[0024] Further, the processing system further comprises a distilled water storage unit, the first evaporated water outlet is connected to an inlet of the distilled water storage unit.

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

[0026] Further, the ammonium salt water unit comprises:

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

[0028] a saturated ammonium salt water unit having a saturated salt water inlet, an ammonia gas inlet, and a saturated ammonium salt water outlet; the saturated salt water outlet is connected to the saturated salt water inlet; the saturated ammonium salt water unit is configured to mix ammonia gas and the saturated salt water to form a saturated ammonium salt water.

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

[0030] Further, the carbonization unit employs a carbonization tower device.

[0031] Further, the pyrolysis unit employs a rotary kiln device.

[0032] Further, the ammonium salt water unit employs an ammonia absorption tower device.

[0033] Further, the second separation unit comprises:

[0034] A first solid-liquid separation unit having a solid-liquid mixture inlet, a fly ash solid material outlet, and a fly ash liquid material outlet; the first solid-liquid separation unit is configured to separate the fly ash liquid material from the solid-liquid mixture;

[0035] A hardness removal unit having a fly ash liquid material inlet, a hardness removal agent inlet, and a post-hardness removal material outlet; the fly ash liquid material outlet is connected to the fly ash liquid material inlet; the hardness removal unit is configured to remove calcium ions and magnesium ions in the fly ash liquid material to form the post-hardness removal material;

[0036] A heavy metal removal unit having a post-hardness removal material inlet, a heavy metal removal agent inlet, and a post-heavy metal removal material outlet; the post-hardness removal material inlet is connected to the post-hardness removal material outlet; the heavy metal removal unit is configured to remove heavy metals in the post-hardness removal material to form the post-heavy metal removal material;

[0037] A second solid-liquid separation unit having a post-heavy metal removal material inlet, a post-separation solid material outlet, and a post-separation liquid material outlet; the post-heavy metal removal material outlet is connected to the post-heavy metal removal material inlet; the second solid-liquid separation unit is configured to separate the post-heavy metal removal material into the post-separation liquid material containing potassium chloride and sodium chloride;

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

[0039] The treatment system further includes a solid waste storage unit; the fly ash solid material outlet and the post-separation solid material outlet are respectively connected to an inlet of the solid waste storage unit.

[0040] Further, the first separation unit includes:

[0041] A third solid-liquid separation unit having a carbonized material inlet, a sodium bicarbonate outlet, and an ammonium chloride-containing material outlet; the third solid-liquid separation unit is configured to separate the carbonized material into the sodium bicarbonate and the ammonium chloride-containing material;

[0042] A salting-out unit having an ammonium chloride-containing material inlet, a salting-out salt inlet, and a post-salting-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 is configured to separate the ammonium chloride from the ammonium chloride-containing material using the sodium chloride to form an ammonium chloride solid-liquid mixture;

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

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

[0045] Further, the processing system further comprises a sodium chloride storage unit, an outlet of the sodium chloride storage unit being connected with 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 water inlet for reaction, and a first decomposed material outlet; the first double decomposition reaction unit is used for performing a first double decomposition reaction on the potassium chloride and the metallurgical by-product sodium sulfate to generate double decomposition material containing potassium mirabilite and sodium chloride;

[0048] The fifth solid-liquid separation unit has a first decomposed material inlet, a potassium mirabilite outlet, and a liquid phase material containing sodium chloride outlet; the first decomposed material outlet is connected with the first decomposed material inlet; the fifth solid-liquid separation unit is used for separating the potassium mirabilite and the liquid phase material containing sodium chloride from the double decomposition material containing potassium mirabilite and sodium chloride;

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

[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 with the potassium sulfate-containing material inlet; the sixth solid-liquid separation unit is used for separating the potassium sulfate from the potassium sulfate-containing material.

[0051] Further, the reaction unit further comprises a second evaporation and crystallization unit having a liquid phase material containing sodium chloride inlet, a second evaporation water outlet, a second evaporation mother liquor outlet, and a second evaporation and crystallization sodium chloride outlet; the liquid phase material containing sodium chloride outlet is connected with the liquid phase material containing sodium chloride inlet; the second evaporation and crystallization unit is used for evaporating and crystallizing the sodium chloride from the liquid phase material containing sodium chloride;

[0052] The first double decomposition reaction unit further has a second evaporation mother liquor inlet and a sixth separation clear liquid inlet; the sixth solid-liquid separation unit further has a sixth separation clear liquid outlet; the second evaporation mother liquor outlet is connected with the second evaporation mother liquor inlet; the sixth separation clear liquid outlet is connected with the sixth separation clear liquid inlet;

[0053] The processing system further comprises a distilled water storage unit; the outlet of the distilled water storage unit is connected with the reaction water inlet of the first metathesis reaction unit and the second metathesis reaction water inlet of the second metathesis reaction unit respectively; the second evaporation water outlet of the second evaporation crystallization unit is connected with the inlet of the distilled water storage unit.

[0054] Further, the processing system further comprises a sodium chloride storage unit, and the second evaporation crystallization sodium chloride outlet of the second evaporation crystallization unit is connected with the inlet of the sodium chloride storage unit.

[0055] Further, the first metathesis reaction unit and the second metathesis reaction unit adopt a reaction kettle device.

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

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

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

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

[0060] Step 2: forming saturated ammonium salt water by using sodium chloride, water and ammonia;

[0061] Step 3: performing carbonization reaction by using the saturated ammonium salt water and the non-ferrous smelting flue gas to obtain 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 respectively;

[0063] Step 5: performing pyrolysis reaction on the sodium bicarbonate to obtain sodium carbonate;

[0064] Step 6: mixing potassium chloride, sodium sulfate and water, and performing reaction to separate potassium sulfate from the reaction product.

[0065] Further, the specific process of Step 1 comprises:

[0066] Step 1-1: first washing the fly ash to form a solid-liquid mixture, and then separating the solid-liquid mixture to obtain liquid phase material containing potassium chloride and sodium chloride;

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

[0068] Step 1-3: cooling crystallization is performed on the potassium chloride containing mother liquor to separate potassium chloride.

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

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

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

[0072] Step 6-3: potassium mirabilite, potassium chloride and water are mixed to perform a second double decomposition reaction to obtain a material containing potassium sulfate;

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

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

[0075] Further, the operation pressure of carbon dioxide in the carbonization reaction is 0.3-0.6 MPa.

[0076] Further, the operation temperature of the carbonization reaction is 30-60°C.

[0077] Further, the operation temperature of the carbonization reaction in step 3 is 30-40°C. Further, 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 a fly ash liquid phase material; the fly ash liquid phase material is sequentially subjected to hard removal and heavy metal removal treatment, and then subjected to a second solid-liquid separation to obtain a liquid phase material containing potassium chloride and sodium chloride; wherein the hard removal agent is sodium hydroxide and sodium carbonate, and a double alkali method is used for hard removal; the heavy metal removal agent is sodium sulfide.

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

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

[0080] Further, the temperature of the cooling crystallization is 10-35°C.

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

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

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

[0084] The technical scheme of the present application provides a fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas treatment system and method. Sodium chloride and potassium chloride are extracted from fly ash from waste incineration, saturated ammonium salt water is formed by using the sodium chloride and ammonia, the saturated ammonium salt water is used to treat non-ferrous metallurgical flue gas to form products sodium carbonate and ammonium chloride; the potassium chloride in the fly ash and the valueless non-ferrous metallurgical by-product industrial sodium sulfate are reacted to form a product potassium sulfate. The treatment system and method fully realize the recycling of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas waste resources, and the obtained products 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 DRAWINGS

[0085] The drawings accompanying the specification of the present application serve to provide further understanding of the present application, the illustrative embodiments of the present application and the explanations thereof serve 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 the treatment system of the embodiment 1 of the present application is shown.

[0087] Reference signs:

[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 salt water unit; 21, saturated salt water unit; 22, saturated ammonium salt water 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 the embodiments in the present application and the features in the embodiments can be combined with each other without conflict. The present application will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0096] Currently, the main treatment method of waste incineration fly ash is landfill, which will occupy arable land and pollute soil and groundwater; the disposal method of by-product industrial sodium sulfate of non-ferrous metallurgical wastewater is external sales, but the market supply of sodium sulfate is greater than demand, and the by-product sodium sulfate is difficult to sell, and finally may go to landfill disposal; the disposal method of non-ferrous metallurgical waste gas is to discharge after treatment, but it contains a large amount of carbon dioxide, which will cause greenhouse effect; therefore, if the 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 co-processing system is provided, as shown in Figure 1 The processing system comprises:

[0098] A fly ash separation unit 10 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 10 is used to separate potassium chloride and sodium chloride from waste incineration fly ash respectively;

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

[0100] A 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 make saturated ammonium salt water and non-ferrous smelting flue gas to carry out carbonization reaction to generate carbonized material containing sodium bicarbonate and ammonium chloride;

[0101] 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;

[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 make the metallurgical by-product sodium sulfate waste salt and potassium chloride undergo a double decomposition reaction and separate potassium sulfate from the decomposition material.

[0104] The units in the treatment system of the present application are connected by pipelines and the like, and power equipment can also be provided therebetween to control the conveying speed of the material flow; the above-mentioned methods and equipment for extracting sodium chloride and potassium chloride from fly ash can be selected from the prior art, as long as the purpose can be achieved; the water and salt in the above-mentioned ammonium salt water unit can be mixed first and then entered into the unit or entered into the unit at the same time; the equipment used can be selected from the prior art, as long as the water, sodium chloride and ammonia gas can be mixed to form saturated ammonium salt water; the reaction method and structural design of the above-mentioned carbonization unit can be selected from the prior art, as long as carbon dioxide and saturated ammonium salt water can react 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 prior art, as long as sodium bicarbonate and ammonium chloride can be separated from the carbonated material; the heating method, reaction method and structural design of the above-mentioned pyrolysis unit can be selected from the prior art, 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 prior art, as long as potassium chloride and sodium sulfate can react to generate potassium sulfate.

[0105] The innovation of the present application lies in how to design a system that can utilize fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas together and form high value-added products. The above-mentioned treatment system designed by the present application maximizes the recycling of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas waste resources, while effectively reducing the harm of hazardous waste to the environment. The system of the present application has a stable operation of 7200 hours per year.

[0106] In some embodiments, the processing 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 salt water inlet of the ammonium salt water 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.

[0107] The present application provides a transfer storage unit for the obtained intermediate product, final product, water, etc., which can collect or distribute the corresponding products, stabilize the material flow conveying speed, and ensure stable operation of the entire processing system.

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

[0109] a fly ash washing unit 11 having 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] a second separation unit 12 having a solid-liquid mixture inlet and a separated liquid phase 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 phase material containing potassium chloride and sodium chloride from the solid-liquid mixture;

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

[0112] a cooling crystallization unit 14 having a potassium chloride-containing mother liquor inlet, a cooling crystallization mother liquor outlet, and a potassium chloride outlet; the potassium chloride-containing mother liquor inlet is connected to the potassium chloride-containing mother liquor outlet; the cooling crystallization mother liquor inlet is connected to the cooling crystallization mother liquor outlet; the cooling crystallization unit 14 is used to cool and crystallize potassium chloride from the potassium chloride-containing mother liquor.

[0113] The fly ash separation unit designed in the application can sufficiently extract sodium ions, potassium ions, chlorine ions and the like in the fly ash into the liquid phase material, and further crystallize sodium chloride by evaporation and crystallization, and crystallize potassium chloride by cooling crystallization; and can provide relatively pure reactants, sodium chloride and potassium chloride, for subsequent reactions, and can also ensure that the products, potassium sulfate and sodium carbonate and ammonium chloride, after the reactions, reach the purpose of high purity.

[0114] In some embodiments, the processing system further comprises 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 application can return the water generated in the first evaporation and crystallization process to the water storage unit through the return line, so as to be delivered to other units of the processing system which need water, to realize the recycling of water production and water supply, and to save water.

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

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

[0117] The application first mixes water and sodium chloride to form saturated salt water, and then sends the saturated salt water into the saturated ammonium salt water unit to react with ammonia gas. The feeding mode can fully mix the saturated salt water and ammonia gas, and improve 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. The carbon dioxide generated by the pyrolysis of sodium bicarbonate is returned to the flue gas inlet of the carbonization unit, instead of being directly discharged, so as to be fully utilized for participating in the reaction. The design of the return line can realize the recycling of waste gas once, and improve the waste treatment effect.

[0119] In some embodiments, the carbonization unit 30 adopts a carbonization tower device, the pyrolysis unit 50 adopts a rotary kiln device, and the ammonium salt water unit 20 adopts an ammonia absorption tower device. The application selects 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 comprises:

[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 configured 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 configured to remove calcium ions and magnesium ions in the fly ash liquid-phase material to form the hardness-removed material.

[0123] The heavy metal removal unit 123 has a hardness-removed material inlet, a heavy metal removal agent inlet, and a heavy metal-removed material outlet. The hardness-removed material inlet is connected to the hardness-removed material outlet. The heavy metal removal unit 123 is configured to remove heavy metals in the hardness-removed material to form the heavy metal-removed material.

[0124] The second solid-liquid separation unit 124 has a heavy metal-removed material inlet, a separated solid-phase material outlet, and a separated liquid-phase material outlet. The heavy metal-removed material outlet is connected to the heavy metal-removed material inlet. The second solid-liquid separation unit 124 is configured to separate the liquid-phase material containing potassium chloride and sodium chloride from the heavy metal-removed material.

[0125] The first solid-liquid separation unit 121 is selected from a belt filter and / or a plate-and-frame filter press. The second solid-liquid separation unit 124 is selected from a belt filter and / or a plate-and-frame filter press.

[0126] The application separates the solid phase from the fly ash first, removes the useless ions in the liquid phase, and then removes the solid phase precipitate, leaving the separated liquid phase. As a result, more useful sodium ions, potassium ions, and chlorine ions for subsequent reactions are retained, which fully utilizes the useful ions, improves the efficiency of subsequent reactions, ensures product purity, and reduces side reactions.

[0127] The treatment system further 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 configured to separate sodium bicarbonate and ammonium chloride-containing material from the carbonized material.

[0130] The salt precipitation unit 42 has an ammonium chloride-containing material inlet, a salt precipitation salt inlet, and a post-salt precipitation 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 salt precipitation salt inlet; the salt precipitation unit 42 is used to separate ammonium chloride from the ammonium chloride-containing material by using sodium chloride to form an ammonium chloride solid-liquid mixture;

[0131] The fourth solid-liquid separation unit 43 has a post-salt precipitation material inlet, an ammonium chloride outlet, and a fourth solid-liquid separation liquid phase material outlet; the post-salt precipitation material outlet is connected to the post-salt precipitation 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 filter press and / or plate-and-frame filter press device; the fourth solid-liquid separation unit 43 adopts a filter press and / or plate-and-frame filter press device.

[0133] The application can fully extract ammonium chloride and ensure the purity of ammonium chloride through the above design.

[0134] In some embodiments, the processing system further includes a sodium chloride storage unit 74, and the outlet of the sodium chloride storage unit 74 is connected to the salt precipitation salt inlet. In order to fully separate ammonium chloride, the application adopts a salt precipitation method, and the sodium chloride used for salt precipitation also comes from the separated sodium chloride from the fly ash. The sodium chloride can be obtained by being connected to the sodium chloride outlet of the fly ash separation unit, or the separated sodium chloride from the fly ash can be first stored in a transfer unit, and the sodium chloride is obtained by being connected to the transfer unit for use in various places.

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

[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 make the potassium chloride and the metallurgical by-product sodium sulfate undergo a first double decomposition reaction to generate a double decomposition material containing potassium mirabilite and sodium chloride;

[0137] The fifth solid-liquid separation unit 62 has a first decomposition material inlet, a potassium mirabilite 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 potassium mirabilite and a sodium chloride-containing liquid phase material from the double decomposition material containing potassium mirabilite and sodium chloride;

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

[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 for separating potassium sulfate from the potassium sulfate-containing material.

[0140] The present application designs the above reaction route, potassium chloride, sodium sulfate and water are first reacted to generate potassium mirabilite intermediate product and sodium chloride product, then the sodium chloride is separated out, and then the potassium mirabilite and potassium chloride are continuously reacted to generate potassium sulfate, so that the potassium chloride and sodium sulfate can be fully reacted, so as to fully utilize the waste sodium sulfate and obtain high-purity potassium sulfate.

[0141] In some embodiments, the reaction unit 60 further comprises a second evaporation crystallization unit 65 having 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 for evaporating and crystallizing sodium chloride from the sodium chloride-containing liquid phase material. The present application designs the above return route, which fully utilizes the water and sodium chloride generated in the second evaporation crystallization process, the water can be used as saturated brine water or reaction water, and the sodium chloride can be used as saturated brine salt or salting-out salt, so that the product is finally changed into the reactant, and the waste resources are fully utilized and the resources are saved.

[0142] In some embodiments, the first double decomposition reaction unit 61 further has a second evaporation mother liquor inlet and a sixth separation clear liquid inlet; the sixth solid-liquid separation unit 64 further has a sixth separation clear liquid outlet; the second evaporation mother liquor outlet is connected to the second evaporation mother liquor inlet; and the sixth separation clear liquid outlet is connected to the sixth separation clear liquid inlet. The present application designs the above return route, which can recycle and utilize the separated substances containing unreacted sodium sulfate, potassium mirabilite and the like, so as to realize recycling and save resources.

[0143] In some embodiments, the processing system further comprises a distilled water storage unit 73; the outlet of the distilled water storage unit 73 is connected to the reaction water inlet of the first double decomposition reaction unit 61, the second double decomposition reaction water inlet of the second double decomposition reaction unit 63, respectively; the second evaporation water outlet of the second evaporation crystallization unit 65 is connected to the inlet of the distilled water storage unit 73. The processing system further comprises a sodium chloride storage unit 74, and the second evaporation 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 the return route; in the water or sodium chloride recycling process, the water outlet can be connected to the water inlet of each place to supply water, or the generated water can be first stored in a transfer unit, and then the water inlet of each place is connected to the transfer unit to take water; the generation 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 adopt a reaction kettle device; the fifth solid-liquid separation unit 62 adopts a filter press and / or plate-and-frame filter press device; the sixth solid-liquid separation unit 64 adopts a filter press and / or plate-and-frame filter press device; and the second evaporation crystallization unit 65 adopts a multi-effect evaporation device and / or a mechanical vapor recompression device. The selection of the above devices can improve the reaction efficiency, separation efficiency, etc.

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

[0146] Step 1: treating the waste incineration fly ash to separate out potassium chloride and sodium chloride, respectively;

[0147] Step 2: forming saturated ammonium salt water by using sodium chloride, water and ammonia;

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

[0149] Step 4: separating out sodium bicarbonate and ammonium chloride from the carbonized material containing sodium bicarbonate and ammonium chloride, respectively;

[0150] Step 5: performing pyrolysis reaction on the sodium bicarbonate to obtain sodium carbonate;

[0151] Step 6: mixing and reacting potassium chloride, sodium sulfate and water to separate out potassium sulfate from the reaction product.

[0152] The above reaction method designed in the present application, in combination with the above processing system of the present application, can fully realize the co-utilization of fly ash, metallurgical waste gas and by-product sodium sulfate, and further obtain high-value-added products sodium carbonate, ammonium chloride and potassium sulfate. The reaction method is simple in operation and high in efficiency.

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

[0154] Step 1-1: first washing the fly ash to form a solid-liquid mixture, and then separating the solid-liquid mixture to obtain liquid phase material containing potassium chloride and sodium chloride;

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

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

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

[0158] Step 6-1: mixing potassium chloride, sodium sulfate and water to carry out the first double decomposition reaction to obtain a double decomposition material containing potassium mirabilite and sodium chloride;

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

[0160] Step 6-3: mixing potassium mirabilite, potassium chloride and water to carry out the second double decomposition reaction to obtain a material containing potassium sulfate;

[0161] Step 6-4: solid-liquid separation of 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 producing by-products.

[0163] In some embodiments, the operation pressure of carbon dioxide in the carbonation reaction is 0.3-0.6 MPa. The operation pressure of carbon dioxide used in the present application can fully precipitate the dissolved sodium ions into sodium bicarbonate solids.

[0164] In some embodiments, the operation temperature of the carbonation reaction is 30-60°C. The operation temperature used in the present application can fully precipitate the dissolved sodium ions into sodium bicarbonate solids.

[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, carrying out the first solid-liquid separation to separate out a fly ash liquid phase material; and then carrying out the second solid-liquid separation after the fly ash liquid phase material is sequentially subjected to hard removal and heavy metal removal treatment to obtain a liquid phase material containing potassium chloride and sodium chloride; wherein the hard removal agent is sodium hydroxide and sodium carbonate, and the double alkali method is used for hard removal; and the heavy metal removal agent is sodium sulfide. The above agents selected in the present application can fully remove calcium and magnesium ions and heavy metal ions in the fly ash liquid phase.

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

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

[0168] In the two evaporation crystallization processes, the application uses suitable crystallization temperatures according to the characteristics of the crystallized sodium chloride, so that sodium chloride with high purity can be obtained; the above-mentioned cooling crystallization temperature can be used to fully crystallize potassium chloride, so as to ensure the purity of potassium chloride; and the two times of double decomposition reaction temperatures can be used to fully react potassium chloride and sodium sulfate in two steps, so that high-purity potassium sulfate product can be obtained.

[0169] The above-mentioned fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas co-processing system and method designed by the application first extracts sodium chloride and potassium chloride from the fly ash generated by waste incineration, then fully utilizes the sodium chloride and external ammonia gas to form saturated ammonium salt water, and then utilizes the saturated ammonium salt water to process non-ferrous smelting flue gas, so as to form high-value-added products sodium carbonate and ammonium chloride, wherein the sodium carbonate is formed by the sodium ions in the fly ash and the carbon dioxide in the non-ferrous smelting flue gas, and the ammonium chloride is formed by the chlorine ions in the fly ash and the external ammonia gas; finally, the potassium chloride in the fly ash and the valueless by-product industrial sodium sulfate of non-ferrous metallurgy are reacted to form high-value-added product potassium sulfate; the obtained high-value-added products sodium carbonate, ammonium chloride and potassium sulfate meet the GB / T 20406-2017 agricultural potassium sulfate powder crystalline product standard, the obtained ammonium chloride product meets the GB / T 2946-2018 industrial ammonium chloride product standard, and the obtained sodium carbonate product meets the GB / T 210-2022 industrial sodium carbonate II product standard; the above-mentioned processing system designed by the application maximizes the recycling of fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas waste resources, and effectively reduces the harm of hazardous waste to the environment.

[0170] The application will be further described in detail below in combination with specific embodiments, and these embodiments cannot be understood as limiting the scope of the application.

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

[0172] Embodiment 1

[0173] A fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas co-processing system, such as Figure 1As shown, it comprises: 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 evaporative 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 metathesis reaction unit 61, a fifth solid-liquid separation unit 62, a second evaporative crystallization unit 65, a second metathesis 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 with the fly ash and distilled water storage unit 73, and the output end of the fly ash washing unit 11 is connected with 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 with the liquid input end of the hardness removal unit 122, and the solid output end is connected with 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 with the outside, and the output end of the hardness removal unit 122 is connected with the liquid input end of the heavy metal removal unit; the input end of the heavy metal removal unit 123 includes a liquid input end and a reagent input end, the reagent input end of the heavy metal removal unit 123 is connected with the outside, and the output end of the heavy metal removal unit 123 is connected with 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 with the input end of the solid waste storage unit, and the liquid output end of the second solid-liquid separation unit 124 is connected with 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, the mother liquor input end is connected with the liquid output end of the cooling crystallization unit 14, and the output end of the first 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 with the distilled water storage unit 73, the mother liquor output end is connected with the input end of the cooling crystallization unit 14, and the sodium chloride output end is connected with 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 with 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 is connected with the solid input end of the saturated brine unit, and the salting-out unit direction output end is connected with the solid input end of the salting-out unit; the input end of the cooling crystallization unit is connected with 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 with 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 with the potassium chloride input end of the first double decomposition reaction unit, and the second double decomposition reaction direction output end is connected with the potassium chloride input end of the second double decomposition reaction unit;

[0175] The input end of the saturated brine unit 21 comprises a distilled water feed input end, a solid input end and a mother liquor input end, which 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 comprises a liquid input end and a gas input end, which is connected to 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 comprises 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, and 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 of the third solid-liquid separation unit 41 comprises 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 comprises 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 comprises 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 comprises 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 comprises 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 liquor input end, the by-product sodium sulfate input end is connected with the outside, the distilled water input end is connected with the output end of the distilled water storage unit, the second evaporation mother liquor input end is connected with the mother liquor output end of the second evaporation crystallization unit 65, the sixth clear liquor input end is connected with the liquid output end of the sixth solid-liquid separation unit 64, and the output end of the first double decomposition reaction unit 61 is connected with the feeding end of the fifth solid-liquid separation unit 62; the output end of the fifth solid-liquid separation unit 62 comprises a solid output end and a liquid output end, the solid output end is connected with the intermediate input end of the second double decomposition reaction unit 63, and the liquid output end is connected with the input end of the second evaporation crystallization unit 65; the output end of the second evaporation crystallization unit 65 comprises a mother liquor output end, a sodium chloride output end and a distilled water output end, and the distilled water output end is connected with the input end of the distilled water storage unit; the input end of the second double decomposition reaction unit 63 comprises a potassium chloride input end, an intermediate input end and a distilled water input end, the distilled water input end is connected with the output end of the distilled water storage unit 73, the output end of the second double decomposition reaction unit 63 is connected with the input end of the sixth solid-liquid separation unit 64, and the output end of the sixth solid-liquid separation unit 64 comprises a solid output end and a liquid output end, the solid output end is connected with the input end of the potassium sulfate storage unit 72, and the output end of the potassium sulfate storage unit 72 is connected with the outside.

[0177] In the above 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 multi-effect evaporation or MVR; the saturated ammonia salt water unit adopts an ammonia absorption tower; the carbonization unit adopts a carbonization tower; the pyrolysis unit adopts a rotary kiln pyrolysis system; and the first double decomposition reaction unit and the second double decomposition reaction unit adopt a reaction kettle system.

[0178] Embodiment 2

[0179] A fly ash, sodium sulfate waste salt and non-ferrous smelting flue gas collaborative treatment method adopts the treatment system of embodiment 1; the treatment method comprises the following steps:

[0180] Step 1: The collected fly ash is transported into a fly ash washing unit for water washing to dissolve as much soluble matter as possible in water, and the distilled water is obtained from a distilled water storage unit; the solid-liquid mixture after water washing is transported into a first solid-liquid separation unit for solid-liquid separation using a filter press; the obtained solid is transported into a solid waste storage unit as solid waste, and the obtained liquid is transported into a hardness removal unit; sodium hydroxide and sodium carbonate are added in the hardness removal unit for hardness removal using a double alkali method, and the used sodium carbonate is the sodium carbonate produced by the pyrolysis unit; the obtained liquid after hardness removal is transported into a heavy metal removal unit, and sodium sulfide is added to remove heavy metal ions therein; the treated material is transported into a second solid-liquid separation unit for solid-liquid separation using a filter press; the obtained solid is transported into a solid waste storage unit as solid waste, and the obtained liquid is transported into a first evaporation crystallization unit; the material is subjected to MVR operation in the first evaporation crystallization unit at an operating temperature of 100°C; the obtained sodium chloride crystals are transported into a sodium chloride storage unit, the obtained distilled water is transported into a distilled water storage unit, and the external liquid is transported into a cooling crystallization unit; the cooling crystallization unit is operated at a temperature of 25°C; the obtained potassium chloride is transported into a potassium chloride storage unit, and the obtained mother liquor is returned to the first evaporation crystallization unit;

[0181] Step 2: The sodium chloride from the sodium chloride storage unit, the distilled water from the distilled water storage unit, and the clear liquid from the fourth solid-liquid separation unit are transported into a saturated brine unit to prepare saturated brine; the saturated brine is transported into a saturated ammonia brine unit together with ammonia gas to prepare saturated ammonia brine using an ammonia absorption tower; the obtained saturated ammonia brine is transported into a carbonation unit to undergo a carbonation reaction with non-ferrous smelting flue gas from the outside and carbon dioxide flue gas from the pyrolysis unit in a carbonation tower, and the carbon dioxide is operated at a pressure of 0.5 MPa and a temperature of 40°C; the obtained product from the carbonation reaction unit is transported into a third solid-liquid separation unit for solid-liquid separation using a filter press; the obtained solid from the solid-liquid separation is transported into a pyrolysis unit, and the obtained liquid is transported into a salting-out unit; the pyrolysis unit is a rotary kiln, and the reaction temperature is 150°C; the produced sodium carbonate product meets the GB / T 210-2022 Industrial Sodium Carbonate II Class Qualified Product Standard, is transported into a sodium carbonate storage unit, and the pyrolysis flue gas is transported into a carbonation unit; the clear liquid obtained from the third solid-liquid separation unit is transported into a salting-out unit to undergo a salting-out reaction with sodium chloride from the sodium chloride storage unit; the obtained solid-liquid mixture from the salting-out unit is transported into a fourth solid-liquid separation unit for solid-liquid separation using a filter press; the obtained ammonium chloride product meets the GB / T 2946-2018 Industrial Ammonium Chloride Qualified Product Standard, is transported into an ammonium chloride storage unit, and the obtained liquid is returned to the saturated brine unit;

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

[0183] The synergistic treatment system and process of the present application has a yearly treatment capacity of 50,000 tons of household garbage fly ash; a yearly treatment capacity of 20,000 tons of by-product sodium sulfate generated by non-ferrous metallurgical wastewater zero discharge; and a yearly treatment capacity of 3.6x107Nm3of non-ferrous metallurgical flue gas. 3 The system has a stable operation of 7200 hours per year. 30,000 tons of potassium sulfate are obtained per year, 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 per year, 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 per year, and the obtained product meets the GB / T210-2022 industrial sodium carbonate II qualified product standard and is sold externally.

[0184] In the synergistic treatment system of the present application, the steam condensate water obtained by the first evaporation crystallization unit and the second evaporation crystallization unit can be returned to the distilled water storage unit for recycling as the fly ash washing unit, the saturated brine unit, the first double decomposition unit, and the second double decomposition unit dissolving water, which can greatly save the consumption of tap water; the carbon dioxide flue gas generated by the pyrolysis unit can be returned to the carbonization unit for recycling; the required sodium chloride for 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 waste recovered from waste-producing enterprises, which has a cost of zero and has good economic value.

[0185] It should be noted that the terms "first", "second", and the like in the description and in the claims of the present application are used for distinguishing between similar objects and not necessarily for describing a specific sequential or chronological order. It is to be understood that the terms so used are interchangeable under appropriate circumstances such that the embodiments of the present application described herein are, for example, capable of orderly execution or performance.

[0186] The preferred embodiments of the present application have been described herein above with the intent to be illustrative rather than limiting. It will be apparent to those having ordinary skill in the art that changes and modifications can be made to the described embodiments. It is intended that all such modifications and changes be considered as within the spirit and scope of the present application as defined by the appended claims.

Claims

1. A system for the co-treatment of fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas, characterized in that, The processing system includes: 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 the fly ash of waste incineration. The ammonium brine unit (20) has an ammonia inlet, a salt water inlet, a brine salt inlet, and a saturated ammonium brine outlet; the sodium chloride outlet and the brine salt inlet are connected; the ammonium brine unit (20) is used to mix water, sodium chloride, and ammonia to form a saturated ammonium brine. The carbonization unit (30) has a saturated ammonium brine inlet, a smelting flue gas inlet, and a carbonized material outlet; the saturated ammonium brine outlet is connected to the saturated ammonium brine inlet; the carbonization unit (30) is used to perform a carbonization reaction between the saturated ammonium brine and the non-ferrous smelting flue gas to generate carbonized material containing sodium bicarbonate and ammonium chloride; The first separation unit (40) has a carbonized material inlet, a sodium bicarbonate outlet and an ammonium chloride outlet; the carbonized material outlet and the carbonized material inlet are connected; the first separation unit (40) is used to separate sodium bicarbonate and ammonium chloride from the carbonized material; the first separation unit (40) includes a third solid-liquid separation unit (41), a salting-out unit (42) and a fourth solid-liquid separation unit (43). 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; the pyrolysis flue gas outlet of the pyrolysis unit (50) is connected to the smelting flue gas inlet of the carbonization unit (30); 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 and the potassium chloride inlet are connected; the reaction unit is used to perform a metathesis reaction between the metallurgical by-product sodium sulfate waste salt and the potassium chloride and to separate potassium sulfate from the decomposed material; The reaction unit (60) includes: 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 cause the potassium chloride and the metallurgical by-product sodium sulfate to undergo a first metathesis reaction to generate metathesis material containing potassium sulfate and sodium chloride; The fifth solid-liquid separation unit (62) has a first decomposition material inlet, a potassium sulfate outlet and a sodium chloride-containing liquid phase material outlet; the first decomposition material outlet and the first decomposition material inlet are connected; the fifth solid-liquid separation unit (62) is used to separate potassium sulfate and sodium chloride-containing liquid phase material from the metathesis material containing potassium sulfate and sodium chloride. The second metathesis reaction unit (63) has a potassium sulfate inlet, a potassium chloride inlet for the second metathesis reaction, a water inlet for the second metathesis reaction, and a potassium sulfate-containing material outlet; the potassium sulfate outlet is connected to the potassium sulfate inlet; the second metathesis reaction unit (63) is used to react potassium sulfate and potassium chloride to generate a potassium sulfate-containing material; 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 and the potassium sulfate-containing material inlet are connected; the sixth solid-liquid separation unit (64) is used to separate potassium sulfate from the potassium sulfate-containing material.

2. The system for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to claim 1, characterized in that, The processing 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 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 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), respectively. 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 system for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to claim 1, characterized in that, The fly ash separation unit (10) includes: The fly ash washing unit (11) has 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; The second separation unit (12) has a solid-liquid mixture inlet and a separated liquid phase material outlet; the solid-liquid mixture outlet is connected to the solid-liquid mixture inlet; the second separation unit (12) is used to separate liquid phase material containing potassium chloride and sodium chloride from the solid-liquid mixture; The first evaporation crystallization unit (13) has a separated liquid phase material inlet, a cooling crystallization mother liquor inlet, a sodium chloride outlet, a first evaporated water outlet, and a potassium chloride-containing mother liquor outlet; the separated liquid phase material outlet and the separated liquid phase material inlet are connected; 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 potassium chloride-containing mother liquor; The cooling crystallization unit (14) has a potassium chloride mother liquor inlet, a cooling crystallization mother liquor outlet, and a potassium chloride outlet; the potassium chloride mother liquor outlet and the potassium chloride mother liquor inlet are connected; the cooling crystallization mother liquor outlet and the cooling crystallization mother liquor inlet are connected; the cooling crystallization unit (14) is used to cool and crystallize the potassium chloride from the potassium chloride mother liquor; The processing system further includes a distilled water storage unit (73), wherein 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: The saturated brine unit (21) has a brine salt inlet, a salt 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) has a saturated brine inlet, an ammonia 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 the saturated ammonium brine from ammonia and the saturated brine.

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

5. The system for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to any one of claims 1 to 4, characterized in that, 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) has an ammonium chloride-containing material inlet, a salt inlet for salting out, and a material outlet after salting out; the ammonium chloride-containing material outlet is connected to the ammonium chloride-containing material inlet; the sodium chloride outlet is connected to the salt inlet for salting out; 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 material inlet, an ammonium chloride outlet, and a fourth solid-liquid separation liquid phase material outlet; the post-salting material outlet is connected to the post-salting material inlet; the fourth solid-liquid separation liquid phase material outlet is connected to the salt water inlet of the ammonium brine unit (20); the fourth solid-liquid separation unit (43) is used to separate ammonium chloride from the ammonium chloride solid-liquid mixture; The processing system also includes a sodium chloride storage unit (74), the outlet of which is connected to the salt inlet for salting out.

6. The system for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to claim 1, characterized in that, The reaction unit (60) further includes a second evaporation and 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 and 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 and crystallization unit (65) is used to evaporate and crystallize sodium chloride from the sodium chloride-containing liquid phase material; The first metathesis reaction unit (61) also has a second evaporation mother liquor inlet and a sixth separation clear liquid inlet; the sixth solid-liquid separation unit (64) 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; The processing system further includes a distilled water storage unit (73); the outlet of the distilled water storage unit (73) is 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 evaporation water outlet of the second evaporation crystallization unit (65) is connected to the inlet of the distilled water storage unit (73); The processing system also includes a sodium chloride storage unit (74), and the second evaporation crystallization sodium chloride outlet of the second evaporation crystallization unit (65) is connected to the inlet of the sodium chloride storage unit (74).

7. A method for the co-treatment of fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas, characterized in that, The processing method employs the collaborative processing system described in any one of claims 1 to 6; the method includes the following steps: Step 1: Process the fly ash from waste incineration to separate potassium chloride and sodium chloride; Step 2: Use the sodium chloride, water, and ammonia to form a saturated ammonium salt solution; Step 3: Use the saturated ammonium brine and non-ferrous smelting flue gas to carry out a carbonization reaction to obtain carbonized material containing sodium bicarbonate and ammonium chloride; Step 4: Separate sodium bicarbonate and ammonium chloride from the carbonized material containing sodium bicarbonate and ammonium chloride respectively; Step 5: Perform a pyrolysis reaction on the sodium bicarbonate to obtain sodium carbonate; Step 6: Mix the potassium chloride, sodium sulfate and water, react them, and separate potassium sulfate from the reaction product.

8. The method for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to claim 7, characterized in that, The specific process of step 1 includes: Step 1-1: First, wash the fly ash with water to form a solid-liquid mixture, then separate the solid-liquid mixture to obtain a liquid material containing potassium chloride and sodium chloride; Steps 1-2: The liquid phase material containing potassium chloride and sodium chloride is subjected to a first evaporation crystallization to obtain first evaporation water, sodium chloride and potassium chloride-containing mother liquor, respectively; Steps 1-3: Cool and crystallize the potassium chloride-containing mother liquor to separate the potassium chloride; And / or, the specific process of step 6 includes: Step 6-1: Mix the potassium chloride, sodium sulfate and water to carry out the first metathesis reaction to obtain a metathesis material containing potassium sulfate and sodium chloride; Step 6-2: Perform solid-liquid separation on the metathesis material containing potassium sulfate and sodium chloride to obtain a liquid phase material containing potassium sulfate and sodium chloride. Step 6-3: Mix the potassium sulfate, potassium chloride and water to carry out a second metathesis reaction to obtain a material containing potassium sulfate; Step 6-4: Perform solid-liquid separation on the potassium sulfate-containing material to obtain potassium sulfate.

9. The method for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to claim 7, characterized in that, The carbon dioxide operating pressure for the carbonization reaction in step 3 is 0.3 MPa to 0.6 MPa. And / or, the operating temperature of the carbonization reaction in step 3 is 30℃~60℃; And / or, the molar ratio of potassium chloride to sodium sulfate in step 6 is (2~3):1; And / or, the temperature of the pyrolysis reaction is 100~200℃.

10. The method for co-treating fly ash, sodium sulfate waste salt, and non-ferrous smelting flue gas according to claim 8, characterized in that, The specific process of step 1-1 includes: firstly, 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 then subjected to hardening removal and heavy metal removal treatments, followed by a second solid-liquid separation to obtain the liquid phase material containing potassium chloride and sodium chloride; wherein, the hardening removal agent is sodium hydroxide and sodium carbonate, and the hardening removal is performed using a double alkali method; the heavy metal removal agent is sodium sulfide; And / or, the process of step 6-2 further includes a second evaporation crystallization of the liquid material containing sodium chloride to obtain second evaporated water, sodium chloride, and second evaporation mother liquor; the second evaporation mother liquor, the clear liquid after solid-liquid separation in step 6-4, and the material in step 6-1 are mixed to carry out the first metathesis reaction; the temperature of the second evaporation crystallization is 90℃~120℃; And / or, the temperature of the first evaporation crystallization is 90℃~120℃; And / or, the cooling crystallization temperature is 10℃~35℃; And / or, the temperature of the first metathesis reaction is 30℃~60℃; And / or, the temperature of the second metathesis reaction is 25℃~60℃.

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