A method for treating fly ash by carbon black modification and coordination

Abstract

The invention discloses a carbon black modified and coordinated fly ash treatment method, comprising: providing a carbon black modification system consisting of a carbon black pickling unit, a carbon black water washing unit, and a carbon black filter cake drying and granulation unit, a fly ash treatment system consisting of a fly ash washing and decalcification unit and a fly ash water washing unit, a water treatment system, and a garbage incinerator or a cement kiln; the invention achieves a significant reduction in the consumption of sodium carbonate in the fly ash washing process, resource utilization of baking soda desulfurization ash, improvement of the quality of waste tire pyrolysis carbon black, and harmless treatment of carbon black pickling waste liquid by adjusting the operating conditions of each unit of the fly ash treatment system and combining the carbon black modification system.

Description

Technical Field

[0001] The invention relates to the technical field of environmental engineering, and in particular to a method for treating fly ash by synergistic carbon black modification. Background Art

[0002] With the rapid development of the transportation industry, the demand for transportation tools in various countries around the world has increased year by year, especially the number of motor vehicles. The growing number of cars has led to the accumulation of tires, which not only wastes resources but also pollutes the environment. Some scientific research institutions and enterprises use pyrolysis to recycle waste tires, but the ash content of carbon black obtained by pyrolysis is 12% to 20%, which greatly affects the quality and application range of pyrolytic carbon black. Therefore, there is an urgent need for economical and practical waste tire pyrolytic carbon black deashing and modification technology.

[0003] In recent years, with the construction and commissioning of waste incineration power generation projects in various places, the disposal of waste incineration fly ash has become a focus of attention. At present, the fly ash washing + cement kiln coordinated disposal technology has been industrialized, but the high cost of chemicals seriously affects its economic efficiency, restricting the promotion and application of this technology.

[0004] With the improvement of environmental protection standards, baking soda dry desulfurization technology has gradually been popularized and applied in industries such as smelting, coking, ceramics, and hazardous waste incineration. Baking soda dry desulfurization technology occupies a small area, has high desulfurization efficiency, and does not discharge wastewater, but the baking soda desulfurization ash produced faces the dilemma of resource utilization.

[0005] Patent CN102504619A proposes a waste tire pyrolysis carbon black purification process, including acid washing and alkali washing, which reduces the ash content of carbon black from 18.7% to 2.6%, basically reaching the reinforcement level of N330. This method is not only complex in process and equipment, but also uses a large amount of acid washing liquid and alkali solution, and produces a large amount of high-salt wastewater that needs to be treated, so the economic efficiency and technical reliability are poor.

[0006] Patent CN108179277A discloses a method for treating fly ash with high salt and heavy metal content, and specifically records a scheme for multi-stage acid washing desalination and heavy metal removal of fly ash. After analysis, it is known that the problems of this scheme are: ① The fly ash contains a large amount of unreacted slaked lime, so the acid consumption is extremely large and the cost of the reagent is high; ② The acid used is hydrochloric acid, which reacts to produce calcium chloride, and a large amount of sodium carbonate is still needed to remove the calcium ions.

[0007] Patent CN209940485U discloses a baking soda desulfurization ash resource utilization device, which proposes to use carbon dioxide in flue gas to convert baking soda desulfurization ash into desulfurizing agent baking soda, and at the same time use sulfate in baking soda desulfurization ash to convert low value-added quicklime into high value-added calcium sulfate byproduct or gypsum. The use of this technical solution can achieve full and reasonable utilization of solid waste resources and effectively solve the disposal problem of desulfurization ash, but the system is relatively complex, the economy is poor, and it is not easy to promote and apply. Summary of the invention

[0008] The purpose of the present invention is to provide a carbon black modified synergistic fly ash treatment method, which achieves the following through the synergistic treatment of multiple wastes: a significant reduction in the consumption of sodium carbonate during fly ash washing, resource utilization of baking soda desulfurization ash, improvement of the quality of waste tire pyrolysis carbon black, and harmless treatment of carbon black pickling waste liquid.

[0009] To achieve this object, the present invention adopts the following technical solutions:

[0010] A method for treating fly ash by modifying carbon black is provided, comprising the following steps:

[0011] S10. Provide a carbon black modification system consisting of a carbon black acid washing unit, a carbon black water washing unit, and a carbon black filter cake drying and granulation unit, a fly ash treatment system consisting of a fly ash washing and decalcification unit and a fly ash water washing unit, a water treatment system, and a garbage incinerator or cement kiln;

[0012] S20, adding carbon black, acid solution and washing liquid L2 from the carbon black water washing unit into the carbon black pickling unit, performing pickling treatment on the carbon black to produce washing liquid L1 and slurry, transporting the washing liquid L1 to the fly ash washing and decalcification unit or the water treatment system, and transporting the slurry to the carbon black water washing unit;

[0013] S30, adding water supplement B1 to the carbon black washing unit, washing the carbon black in the carbon black washing unit to produce washing liquid L2, washing liquid L3 and carbon black filter cake, conveying part of the washing liquid L2 to the carbon black acid washing unit, conveying the remaining washing liquid L2 to the fly ash washing unit, conveying the washing liquid L3 to the fly ash washing and decalcification unit, and conveying the carbon black filter cake to the carbon black filter cake drying and granulation unit for granulation;

[0014] S40, adding fly ash, baking soda desulfurization ash and sulfite oxidant into the fly ash washing and decalcification unit to generate washing liquid and fly ash filter cake, conveying the washing liquid to the water treatment system, and conveying the fly ash filter cake to the fly ash water washing unit;

[0015] S50, adding acid solution and sulfite oxidant to the fly ash washing unit to generate washing liquid and fly ash filter cake, conveying the washing liquid to the water treatment system or the fly ash washing and decalcification unit, and conveying the fly ash filter cake to the waste incinerator or cement kiln.

[0016] Among them, the main components of baking soda desulfurization ash are Na2SO3, Na2SO4, and Na2CO3;

[0017] The main components of fly ash are Ca(OH)2, CaCl2, CaSO3, CaSO4, NaCl, KCl, solid insoluble matter and trace heavy metals;

[0018] Carbon black comes from the pyrolysis carbon black of waste tires. The main components are carbon black, SiO2, ZnO and ZnS. The purpose of pickling is to remove ZnO and ZnS.

[0019] Fly ash and baking soda desulfurization ash are washed with water to make Ca 2+ It generates CaSO3, CaSO4, CaCO3 precipitates and generates strong alkaline liquid NaOH.

[0020] The present invention synergistically disposes of solid wastes from three different fields (fly ash from the incineration of domestic waste, carbon black from the pyrolysis of waste tires, and baking soda desulfurization ash), achieving waste treatment with waste, greatly reducing the cost of harmless treatment and resource utilization of fly ash, while obtaining high-quality modified carbon black and solving the disposal problem of baking soda desulfurization ash, with significant energy-saving and emission reduction effects.

[0021] Further, the carbon black pickling unit includes a 1# pickling pulping tank, a 2# pickling pulping tank, a 1# pickling liquid storage tank, a 2# pickling liquid storage tank, a 3# pickling liquid storage tank and a 1# carbon black solid-liquid separator;

[0022] Step S20 specifically includes the following steps:

[0023] The carbon black with a particle size of less than 70 μm is transported to the 1# pickling pulping tank; part of the liquid in the 1# pickling liquid storage tank is transported to the 1# pickling pulping tank, and the liquid-to-solid ratio of the slurry in the 1# pickling pulping tank is adjusted to 2:1-10:1 L / kg; the acid solution is added to the 1# pickling pulping tank, and the H of the slurry in the 1# pickling pulping tank is adjusted. + The concentration is 0.5-3 mol / L; the slurry stirring and mixing reaction time is 30-180 min. The slurry produced after the pickling is transported to the 1# carbon black solid-liquid separator for solid-liquid separation. The separated liquid is transported to the 1# pickling liquid storage tank, and the separated solid remains in the 1# carbon black solid-liquid separator; part of the liquid in the 1# pickling liquid storage tank is transported to the fly ash washing and decalcification unit or the water treatment system as the washing liquid L1, and the liquid-solid ratio of the washing liquid L1 to the carbon black added to the 1# pickling pulping tank is 0.5:1-3:1 L / kg;

[0024] The liquid in the 2# pickling liquid storage tank is transported to the 1# carbon black solid-liquid separator for washing the carbon black filter cake. The washing time of the carbon black filter cake is 10 to 60 minutes. The washed liquid is returned to the 2# pickling liquid storage tank. A portion of the liquid in the 2# pickling liquid storage tank is transported to the 1# pickling liquid storage tank. The liquid-to-solid ratio of the liquid to the carbon black added to the 1# pickling pulping tank is 1:1 to 4:1 L / kg.

[0025] The liquid in the 3# pickling liquid storage tank is transported to the 1# carbon black solid-liquid separator for washing the carbon black filter cake. The washing time of the carbon black filter cake is 10 to 60 minutes. The washed liquid is returned to the 3# pickling liquid storage tank. A portion of the liquid in the 3# pickling liquid storage tank is transported to the 2# pickling liquid storage tank. The liquid-solid ratio of the liquid to the carbon black added to the 1# pickling pulping tank is 1:1 to 4:1 L / kg. A portion of the washing liquid L2 from the carbon black water washing unit is added to the 3# pickling liquid storage tank. The liquid-solid ratio of the washing liquid L2 to the carbon black added to the 1# pickling pulping tank is 1:1 to 4:1 L / kg.

[0026] The slurry or filter cake produced in the 1# carbon black solid-liquid separator is transported to the 2# acid washing pulping tank, and the formed slurry is transported to the carbon black water washing unit.

[0027] In the present invention, the water treatment system is a conventional technology in the art, which includes the following steps:

[0028] (1) pH adjustment: CaO or Ca(OH)2 is mainly used to adjust the pH value of the acidic wastewater to less than 12 to achieve the pre-removal of heavy metals;

[0029] (2) Deep removal of heavy metals: Use sulfur-containing organic matter such as Na2S or heavy metal chelating agents to precipitate and remove heavy metals;

[0030] (3) The separation of calcium sulfate and the separation of sodium chloride and potassium chloride can be achieved through the following two schemes:

[0031] Scheme 1: Low temperature seeding method + MVR evaporation crystallization salt separation, the steps are as follows:

[0032] ① The monovalent and divalent ions are separated by nanofiltration membrane; after the wastewater passes through the nanofiltration membrane, it produces Ca 2+ 、SO4 2- Concentrated water, containing Na + , K + , Cl - of high saline water;

[0033] ②Use the seed method to achieve Ca 2+ 、SO4 2- Crystallization removal of calcium sulfate in concentrated water, please refer to patent CN211896370U for details;

[0034] ③Use MVR evaporator to treat Na + , K + , Cl - High brine is used to achieve salt separation and crystallization of NaCl and KCl salts, see patent CN102161490A for details.

[0035] Solution 2: Seed crystal method for calcium sulfate removal + MVR evaporation crystallization for salt separation, see patent CN113245342A for details, which will not be described in detail.

[0036] Furthermore, the 1# carbon black solid-liquid separator is a vacuum filtration device or a washing filter press. When the 1# carbon black solid-liquid separator is a vacuum filtration device, a part of the washing liquid L2 generated by the carbon black washing unit is transported to the 1# carbon black solid-liquid separator and mixed with the carbon black filter cake for slurrying. The mixing slurrying time is 10 to 60 minutes. The liquid-solid ratio of the prepared slurry is 2:1 to 5:1 L / kg. The produced slurry is transported to the 2# pickling slurrying tank; when the 1# carbon black solid-liquid separator is a washing filter press, a part of the washing liquid L2 generated by the carbon black washing unit is transported to the 2# pickling slurrying tank and mixed with the filter cake transported from the 1# carbon black solid-liquid separator to the 2# pickling slurrying tank for slurrying. The mixing slurrying time is 10 to 60 minutes. The liquid-solid ratio of the prepared slurry is 2:1 to 5:1 L / kg.

[0037] Further, the carbon black water washing unit includes a 1# water washing liquid storage tank, a 2# water washing liquid storage tank, a 3# water washing liquid storage tank and a 2# carbon black solid-liquid separator, wherein the 2# carbon black solid-liquid separator is a washing filter press;

[0038] Step S30 specifically includes the following steps:

[0039] The slurry from the carbon black pickling unit is transported to the 2# carbon black solid-liquid separator, and the separated liquid is transported to the 1# water washing liquid storage tank, and the separated solid remains in the 2# carbon black solid-liquid separator; a part of the washing liquid L2 in the 1# water washing liquid storage tank is transported to the carbon black pickling unit, and the other part is transported to the fly ash water washing unit. The liquid-solid ratio of the washing liquid L2 transported to the fly ash water washing unit and the fly ash added to the fly ash washing and decalcification unit is 0.5:1 to 4:1 L / kg;

[0040] The liquid in the 2# water washing liquid storage tank is transported to the 2# carbon black solid-liquid separator for washing the carbon black filter cake, and the washing time is 10 to 60 minutes; the washed liquid is returned to the 2# water washing liquid storage tank, and the washed solid remains in the 2# carbon black solid-liquid separator; a part of the liquid in the 2# water washing liquid storage tank is transported to the 1# water washing liquid storage tank, and the liquid-solid ratio of this part of the liquid to the fly ash added to the fly ash washing and decalcification unit is 1:1 to 7:1 L / kg;

[0041] The liquid in the 3# water washing liquid storage tank is transported to the 2# carbon black solid-liquid separator for washing the carbon black filter cake, and the washing time is 10 to 60 minutes. The washed liquid is returned to the 3# water washing liquid storage tank, and the washed solid is transported to the carbon black filter cake drying and granulation unit; a part of the liquid in the 3# water washing liquid storage tank is transported to the 2# water washing liquid storage tank, and the liquid-solid ratio of this part of the liquid to the fly ash added to the fly ash washing and decalcification unit is 1:1 to 7:1 L / kg; another part of the liquid in the 3# water washing liquid storage tank is transported to the fly ash washing and decalcification unit as washing liquid L3, and the liquid-solid ratio of this washing liquid L3 to the fly ash added to the fly ash washing and decalcification unit is 1:1 to 3:1 L / kg; make-up water B1 is added to the 3# water washing liquid storage tank, and the liquid-solid ratio of this make-up water B1 to the fly ash added to the fly ash washing and decalcification unit is 2:1 to 7:1 L / kg.

[0042] Furthermore, the carbon black filter cake drying and granulation unit includes a carbon black filter cake drying device, a carbon black granulation device, a carbon black particle drying device, a packaging device, an exhaust gas dust removal bag, an exhaust gas washing tower and a chimney;

[0043] The carbon black filter cake from the carbon black washing unit is transported to the carbon black filter cake drying equipment for pre-drying. The water content of the pre-dried carbon black is 5% to 30% lower than that of the carbon black particles at the outlet of the carbon black granulation equipment. The pre-dried carbon black is transported to the carbon black granulation equipment, and the dusty and acidic waste gas generated during the pre-drying process is transported to the waste gas dust removal bag;

[0044] The pre-dried carbon black and granulation water are added into the carbon black granulation equipment and stirred and mixed, and the water content of the prepared carbon black particles is 35% to 55%, and the prepared carbon black particles are transported to the carbon black particle drying equipment;

[0045] In the carbon black pellet drying equipment, the moisture content of the carbon black pellets is reduced to less than 1.5%. After drying and cooling, the carbon black pellets are transported to the packaging equipment, and the dusty and acidic waste gas generated is transported to the waste gas dust removal bag;

[0046] The dusty and acidic waste gas is purified in turn by the waste gas dust removal bag and the waste gas washing tower and then discharged into the chimney.

[0047] Furthermore, the fly ash washing and decalcification unit includes a 1# fly ash slurrying tank, a 1# fly ash liquid storage tank and a 1# fly ash solid-liquid separator, wherein the 1# fly ash solid-liquid separator adopts a washing filter press or a horizontal screw dehydration centrifuge.

[0048] Step S40 specifically includes the following steps:

[0049] Add the fly ash to the No. 1 fly ash slurry tank, and send part of the liquid in the No. 1 fly ash liquid storage tank to the No. 1 fly ash slurry tank for slurrying;

[0050] Decalcify the slurry in the No. 1 fly ash slurry tank;

[0051] The decalcified slurry in the No. 1 fly ash slurrying tank is transported to the No. 1 fly ash solid-liquid separator, the separated liquid is transported to the No. 1 fly ash liquid storage tank, and the separated fly ash filter cake is transported to the fly ash water washing unit;

[0052] Part of the liquid in the No. 1 fly ash storage tank is transported to the water treatment system as washing liquid L4, and the liquid-to-solid ratio of the washing liquid L4 to the fly ash added to the fly ash washing and decalcification unit is 1:1 to 6:1 L / kg;

[0053] Among them, the washing liquid in the 1# fly ash storage tank also comes from the carbon black water washing unit or the fly ash water washing unit. The liquid-solid ratio of the washing liquid L3 from the carbon black water washing unit and the fly ash added to the fly ash washing and decalcification unit is 1:1~3:1 L / kg, and the liquid-solid ratio of the washing liquid L5 from the fly ash water washing unit and the fly ash added to the fly ash washing and decalcification unit is 1:1~4:1 L / kg.

[0054] Further, the decalcification treatment performed on the slurry in the No. 1 fly ash slurrying tank is any one of a shallow decalcification treatment, a medium decalcification treatment, and a heavy decalcification treatment;

[0055] The shallow decalcification treatment is as follows: the baking soda desulfurization ash is mixed with part of the liquid in the 1# fly ash storage tank and then transported to the 1# fly ash slurry tank. The amount of baking soda desulfurization ash is adjusted to reduce the free Ca in the slurry. 2+ CO3 generated by hydrolysis of baking soda desulfurization ash 2- 、SO3 2- 、SO4 2- Generate CaCO3, CaSO3, CaSO4 precipitation to control Ca content in slurry 2+ / SO4 2- The molar ratio is 0.95-1.05; the liquid-to-solid ratio of the slurry is adjusted to 2:1-5:1 L / kg, and the slurry mixing reaction time is 10-60 min; there is still a large amount of acid-soluble Ca(OH)2 in the fly ash at this stage, so it is called shallow decalcification of fly ash.

[0056] The specific method of moderate decalcification is as follows: the washing liquid L1 from the carbon black pickling unit, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash are mixed and transported to the 1# fly ash pulping tank, and the H content in the mixed liquid of the washing liquid L1, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash is adjusted. + The concentration is 0.1~3mol / L; the pH value of the slurry in the 1# fly ash slurry tank is controlled to be 10~12, and the Ca content in the slurry is controlled to be 2+ / SO4 2-The molar ratio is 0.95-1.05; the liquid-solid ratio of the slurry is adjusted to 3:1-8:1 L / kg, and the slurry mixing reaction time is 10-60 min; there is a small amount of acid-soluble Ca(OH)2 and CaCO3 in the fly ash at this stage, so it is called moderate decalcification of fly ash.

[0057] The heavy decalcification treatment is as follows: the washing liquid L1 from the carbon black pickling unit, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash are mixed and transported to the 1# fly ash slurry tank, and the H content in the mixed liquid of the washing liquid L1, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash is adjusted. + The concentration is 0.1~3mol / L, the pH value of the slurry in the 1# fly ash slurry tank is controlled to be 3.5~5, and the Ca content in the slurry is controlled 2+ / SO4 2- The molar ratio is 0.95-1.05, and the liquid-to-solid ratio of the slurry is adjusted to 3:1-8:1 L / kg; a sulfite oxidant is introduced into the No. 1 fly ash slurrying tank, and the mixing reaction time of the slurry and the sulfite oxidant is 30-180 min; there is no acid-soluble Ca(OH)2 and CaCO3 in the fly ash at this stage, so it is called severe decalcification of fly ash.

[0058] Further, the fly ash washing unit includes a fly ash washing unit A and a fly ash washing unit B, wherein the fly ash washing unit A includes a 2A# fly ash slurry tank, a 2A# fly ash liquid storage tank, and a 2A# fly ash solid-liquid separator, wherein the 2A# fly ash solid-liquid separator adopts a washing filter press or a horizontal screw dehydration centrifuge;

[0059] Step S50 specifically includes the following steps:

[0060] The fly ash filter cake from the fly ash washing and decalcification unit is transported to the 2A# fly ash slurry tank, and the liquid-solid ratio of the slurry is adjusted by controlling the amount of liquid transported from the 2A# fly ash storage tank to the 2A# fly ash slurry tank;

[0061] The liquid-solid ratio of the slurry in the 2A# fly ash slurrying tank is controlled to be 2:1-5:1 L / kg, acid is added to the 2A# fly ash slurrying tank to adjust the pH value of the slurry to 1.5-3.5, the slurry is stirred and reacted for 30-180 min, so that the salt and heavy metals in the fly ash filter cake enter the water. This operation is called fly ash acid leaching; alternatively, the liquid-solid ratio of the slurry in the 2A# fly ash slurrying tank is controlled to be 3:1-8:1 L / kg, acid is added to the 2A# fly ash slurrying tank to adjust the pH value of the slurry to 3.5-5, a sulfite oxidant is introduced, and the slurry and the sulfite oxidant are mixed and reacted for 30-180 min. This operation is called fly ash oxidation; alternatively, the liquid-solid ratio of the slurry in the 2A# fly ash slurrying tank is controlled to be 2:1-5:1 L / kg, the slurry is stirred and reacted for 10-60 min, so that the salt in the fly ash filter cake enters the water. This operation is called fly ash washing;

[0062] The slurry after fully mixing and reaction in the 2A# fly ash slurry making tank is transported to the 2A# fly ash solid-liquid separator, the separated liquid is transported to the 2A# fly ash liquid storage tank, and the separated fly ash filter cake is transported to the fly ash water washing unit B;

[0063] Part of the liquid in the 2A# fly ash storage tank leaves the fly ash washing unit A and is transported to the fly ash washing and decalcification unit or the fly ash washing unit B as washing liquid L5. The liquid-to-solid ratio of the washing liquid L5 to the fly ash added to the fly ash washing and decalcification unit is 0.5:1 to 4:1 L / kg.

[0064] The washing liquid L2 from the carbon black water washing unit or the washing liquid L6 from the fly ash water washing unit B is transported to the 2A# fly ash storage tank, the liquid-solid ratio of the washing liquid L2 from the carbon black water washing unit to the fly ash added to the fly ash washing and decalcification unit is 0.5:1~2:1L / kg, and the liquid-solid ratio of the washing liquid L6 from the fly ash water washing unit B to the fly ash added to the fly ash washing and decalcification unit is 1:1~4:1L / kg.

[0065] Further, the fly ash washing unit B includes a 2B# fly ash slurry tank, a 2B# fly ash liquid storage tank, and a 2B# fly ash solid-liquid separator, wherein the 2B# fly ash solid-liquid separator adopts a washing filter press or a horizontal screw dehydration centrifuge;

[0066] Step S50 also includes the following steps:

[0067] The fly ash filter cake from the fly ash washing unit A is transported to the 2B# fly ash slurry tank, and the liquid-to-solid ratio of the slurry in the 2B# fly ash slurry tank is adjusted to 2:1-5:1 L / kg by controlling the amount of liquid transported from the 2B# fly ash storage tank to the 2B# fly ash slurry tank;

[0068] The materials in the 2B# fly ash slurry tank are mixed and stirred to dilute the salt in the fly ash filter cake into the water. The slurry stirring time is 10 to 60 minutes. This operation is called fly ash washing. Alternatively, acid is added to the 2B# fly ash slurry tank to adjust the pH value of the slurry to 1.5 to 3.5, so that the salt and heavy metals in the fly ash filter cake enter the water. The slurry stirring reaction time is 30 to 180 minutes. This operation is called fly ash acid leaching.

[0069] The slurry after fully mixing and reacting in the 2B# fly ash slurry making tank is transported to the 2B# fly ash solid-liquid separator, and the separated liquid is transported to the 2B# fly ash liquid storage tank. The separated fly ash filter cake is mixed with quicklime or slaked lime and then transported to the waste incinerator or cement kiln;

[0070] Part of the liquid in the 2B# fly ash storage tank leaves the fly ash washing unit B and is transported to the 2A# fly ash storage tank or the water treatment system as washing liquid L6. The liquid-to-solid ratio of the washing liquid L6 to the fly ash added to the fly ash washing and decalcification unit is 0.5:1 to 4:1 L / kg.

[0071] The washing liquid L2 from the carbon black water washing unit or the washing liquid L5 from the 2A# fly ash storage tank is transported to the 2B# fly ash storage tank, the liquid-to-solid ratio of the washing liquid L2 from the carbon black water washing unit and the fly ash added to the fly ash washing and decalcification unit is 1:1~4:1 L / kg, and the liquid-to-solid ratio of the washing liquid L5 from the 2A# fly ash storage tank and the fly ash added to the fly ash washing and decalcification unit is 0.5:1~2:1 L / kg.

[0072] In the present invention, the added acid solution is a HCl solution with a mass fraction of 10 to 40% and / or a H2SO4 solution with a mass fraction of 10 to 98.3%.

[0073] Furthermore, the added sulfite oxidant is air or H2O2 solution; if H2O2 solution is added, the molar ratio of H2O2 to sulfite is 1 to 1.2; if air is introduced, the molar ratio of O2 in the air to sulfite is 1.2 to 2.5.

[0074] Furthermore, the present invention can form the following three treatment processes by adjusting the operating conditions of each unit of the fly ash treatment system and combining it with the carbon black modification system: (1) carbon black modification in conjunction with fly ash heavy decalcification, oxidation + acid leaching + washing process; (2) carbon black modification in conjunction with fly ash shallow decalcification + washing + washing process; (3) carbon black modification in conjunction with fly ash moderate decalcification + oxidation + acid leaching process.

[0075] In process (1), the fly ash washing and decalcification unit operation realizes the heavy decalcification and sulfite oxidation of fly ash, the fly ash water washing A unit operation realizes the dilution of salt in fly ash and partial leaching of heavy metals, and the fly ash water washing B unit operation realizes the dilution of salt in fly ash. Specifically, the operation steps of the carbon black modification and fly ash heavy decalcification, oxidation + acid leaching + washing process are as follows: ① Carbon black, HCl and / or H2SO4 and washing liquid L2 enter the carbon black acid washing unit together, the generated slurry enters the carbon black water washing unit, and the generated washing liquid L1 enters the fly ash washing and decalcification unit; ② The slurry leaving the carbon black acid washing unit enters the carbon black water washing unit together with the make-up water B1, and the generated carbon black filter cake enters the carbon black filter cake drying and granulation unit, a part of the generated washing liquid L2 enters the carbon black acid washing unit, and the other part enters the fly ash water washing B unit, and no washing liquid L3 is generated; ③ The carbon black filter cake leaving the carbon black water washing unit enters the carbon black filter cake drying and granulation unit together with the granulation water; ④ Fly ash, baking soda desulfurization ash, washing liquid L2 The washing liquid L1, the washing liquid L5 and the sulfite oxidant enter the fly ash washing and decalcification unit together, and the unit realizes the heavy decalcification and sulfite oxidation of the fly ash. The generated washing liquid L4 enters the water treatment system, and the generated fly ash filter cake enters the fly ash water washing A unit; ⑤ The fly ash filter cake leaving the fly ash washing and decalcification unit, the washing liquid L6 and HCl and / or H2SO4 enter the fly ash water washing A unit together, the generated washing liquid L5 enters the fly ash washing and decalcification unit, and the generated fly ash filter cake enters the fly ash water washing B unit; ⑥ The fly ash filter cake leaving the fly ash water washing A unit and the washing liquid L2 enter the fly ash water washing B unit together, the generated washing liquid L6 enters the fly ash water washing A unit, and the generated fly ash filter cake enters the waste incinerator or cement kiln.

[0076] In process 2, the fly ash washing and decalcification unit operation realizes shallow decalcification of fly ash, the fly ash water washing A unit operation realizes dilution of salt in fly ash, and the fly ash water washing B unit operation realizes dilution of salt in fly ash. Specifically, the operating steps of the carbon black modification coordinated fly ash shallow decalcification + washing + washing process are as follows: ① Carbon black, HCl and / or H2SO4 and washing liquid L2 enter the carbon black pickling unit together, the generated slurry enters the carbon black water washing unit, and the generated washing liquid L1 enters the water treatment system; ② The slurry leaving the carbon black pickling unit enters the carbon black water washing unit together with the make-up water B1, and the generated carbon black filter cake enters the carbon black filter cake drying and granulation unit, a part of the generated washing liquid L2 enters the carbon black pickling unit, and the other part enters the fly ash water washing B unit, and no washing liquid L3 is generated; ③ The carbon black filter cake leaving the carbon black water washing unit enters the carbon black filter cake drying and granulation unit together with the granulation water. Element; ④ The fly ash, baking soda desulfurization ash, and washing liquid L5 enter the fly ash washing and decalcification unit together, which realizes shallow decalcification of the fly ash, and the generated washing liquid L4 enters the water treatment system, and the generated fly ash filter cake enters the fly ash water washing A unit; ⑤ The fly ash filter cake leaving the fly ash washing and decalcification unit enters the fly ash water washing A unit together with the washing liquid L6, and the generated washing liquid L5 enters the fly ash washing and decalcification unit, and the generated fly ash filter cake enters the fly ash water washing B unit; ⑥ The fly ash filter cake leaving the fly ash water washing A unit enters the fly ash water washing B unit together with the washing liquid L2, and the generated washing liquid L6 enters the fly ash water washing A unit, and the generated fly ash filter cake enters the waste incinerator or cement kiln.

[0077] In process (3), the fly ash washing and decalcification unit operation realizes moderate decalcification of fly ash, the fly ash water washing A unit operation realizes sulfite oxidation in fly ash, and the fly ash water washing B unit operation realizes heavy metal leaching in fly ash. Specifically, the operation steps of the carbon black modification and fly ash moderate decalcification + oxidation + acid leaching process are as follows: ① Carbon black, HCl and / or H2SO4 and washing liquid L2 enter the carbon black acid washing unit together, the generated slurry enters the carbon black water washing unit, and the generated washing liquid L1 enters the fly ash washing and decalcification unit; ② The slurry leaving the carbon black acid washing unit enters the carbon black water washing unit together with the make-up water B1, and the generated carbon black filter cake enters the carbon black filter cake drying and granulation unit, a part of the generated washing liquid L2 enters the carbon black acid washing unit, and the other part enters the fly ash water washing A unit, and the generated washing liquid L3 enters the fly ash washing and decalcification unit; ③ The carbon black filter cake leaving the carbon black water washing unit enters the carbon black filter cake drying and granulation unit together with the granulation water; ④ Fly ash, baking soda desulfurization ash ⑤ The fly ash filter cake leaving the fly ash washing and decalcification unit, the washing liquid L2, the sulfite oxidant and HCl and / or H2SO4 enter the fly ash water washing unit A together, the washing liquid L5 generates enters the fly ash water washing unit B, and the fly ash filter cake generates enters the fly ash water washing unit B; ⑥ The fly ash filter cake leaving the fly ash water washing unit A, the washing liquid L5 and HCl and / or H2SO4 enter the fly ash water washing unit B together, the washing liquid L6 generates enters the water treatment system, and the fly ash filter cake generates enters the waste incinerator or cement kiln.

[0078] Beneficial effects of the present invention:

[0079] (1) The present invention provides a method for the coordinated disposal of solid wastes from three different fields (fly ash from the incineration of domestic waste, carbon black from the pyrolysis of waste tires, and baking soda desulfurization ash), thereby achieving waste treatment with waste, greatly reducing the cost of harmless disposal and resource utilization of fly ash, obtaining high-quality modified carbon black, and solving the disposal problem of baking soda desulfurization ash, with significant energy-saving and emission reduction effects.

[0080] (2) The present invention uses baking soda desulfurization ash instead of sodium carbonate to remove calcium ions from waste incineration fly ash washing liquid, which not only realizes the resource utilization of baking soda desulfurization ash, but also greatly reduces the cost of fly ash washing chemicals.

[0081] (3) The present invention uses the high-concentration acid solution generated in the waste tire pyrolysis carbon black pickling process to neutralize the strongly alkaline fly ash water washing liquid, thereby solving the problem of treating the waste acid in the carbon black pickling modification process and achieving the pH value adjustment of the fly ash water washing liquid.

[0082] (4) The present invention not only realizes the granulation and drying of carbon black through the carbon black drying and granulation system, but also removes the residual acid (HCl or H2SO4) in the carbon black, thereby avoiding the problem of waste liquid treatment caused by washing the carbon black filter cake with a large amount of water. BRIEF DESCRIPTION OF THE DRAWINGS

[0083] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments of the present invention. Obviously, the drawings described below are only some embodiments of the present invention, and for ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0084] Figure 1 It is a flow chart of the carbon black pickling unit provided by the present invention;

[0085] Figure 2 This is a flow chart of a carbon black water washing unit provided by the present invention;

[0086] Figure 3 This is a flow chart of a carbon black filter cake drying and granulation unit provided by the present invention;

[0087] Figure 4 This is a flow chart of a fly ash washing and decalcification unit provided by the present invention;

[0088] Figure 5 This is a flow chart of the fly ash washing unit A provided by the present invention;

[0089] Figure 6 This is a flow chart of the fly ash washing unit B provided by the present invention;

[0090] Figure 7 This is a process flow chart of carbon black modification and fly ash heavy decalcification, oxidation + acid leaching + washing provided in Example 1 of the present invention;

[0091] Figure 8 This is a process flow chart of carbon black modification and fly ash shallow decalcification + washing + washing provided in Example 2 of the present invention;

[0092] Fig. 9 This is the process flow chart of carbon black modification and fly ash moderate decalcification + oxidation + acid leaching provided in Example 3 of the present invention. DETAILED DESCRIPTION

[0093] The technical solution of the present invention is further described below in conjunction with the embodiments. If no specific techniques or conditions are specified in the embodiments, the techniques or conditions described in the literature in the art or the product instructions are used. If the manufacturer of the reagents or instruments used is not specified, they are all conventional products that can be obtained commercially.

[0094] Example 1: Carbon black modification and fly ash heavy decalcification, oxidation + acid leaching + washing process

[0095] The rated processing capacity of a domestic waste power plant is 2000t / d, and its flue gas production is 360000Nm 3 / h, the average concentrations of HCl and SO2 were 550 mg / Nm 3 and 450mg / Nm 3 , operating for 8000 hours per year. The power plant uses Ca(OH)2 semi-dry deacidification, and the Ca / (S+0.5Cl) equivalent ratio is 1.3. The amount of fly ash generated accounts for 4% of the garbage treatment volume, that is, the fly ash output is 26666.7 tons / year. Sodium chloride and potassium chloride account for 15% of the fly ash, and the moisture content of the fly ash filter cake after solid-liquid separation is 35%. The pyrolysis carbon black produced by a waste tire pyrolysis plant has an ash content of 15%. After acid washing, the ash content is reduced to 8.6%, and the moisture content of the carbon black filter cake is 45%. The molar proportion of Na2CO3 in the baking soda desulfurization ash produced by a factory's flue gas dry desulfurization is 5%, and the molar proportions of Na2SO3 and Na2SO4 are 10% and 85%, respectively. The three types of waste are synergistically treated by carbon black modification and fly ash heavy decalcification, oxidation + acid leaching + washing process. The specific process flow is as follows (reference Figure 7 ):

[0096] ① Carbon black, HCl and washing liquid L2 enter the carbon black pickling unit together, the generated slurry enters the carbon black water washing unit, and the generated washing liquid L1 enters the fly ash washing and decalcification unit; ② The slurry leaving the carbon black pickling unit enters the carbon black water washing unit together with the make-up water B1, and the generated carbon black filter cake enters the carbon black filter cake drying and granulation unit, part of the generated washing liquid L2 enters the carbon black pickling unit, and the other part enters the fly ash water washing B unit, and no washing liquid L3 is generated; ③ The carbon black filter cake leaving the carbon black water washing unit enters the carbon black filter cake drying and granulation unit together with the granulation water; ④ Fly ash, baking soda desulfurization ash, washing liquid L1, washing liquid L5 and air ⑤ The fly ash filter cake leaving the fly ash washing and decalcification unit, the washing liquid L6 and HCl enter the fly ash water washing unit A together, the washing liquid L5 enters the fly ash washing and decalcification unit, and the fly ash filter cake enters the fly ash water washing unit B; ⑥ The fly ash filter cake leaving the fly ash water washing unit A enters the fly ash water washing unit B together with the washing liquid L2, the washing liquid L6 enters the fly ash water washing unit A, and the fly ash filter cake enters the waste incinerator.

[0097] Next, combine Figure 1-6 The process is described in detail:

[0098] (1) Carbon black pickling unit, process flow reference Figure 1, the operating conditions are as follows:

[0099] ① The particle size of carbon black in the 1# pickling pulping tank is within 60μm, the liquid-to-solid ratio of the slurry is 5:1L / kg, and the H in the slurry is adjusted by 30% HCl solution. + The concentration is 1.2mol / L, and the slurry stirring and mixing reaction time is 180min; ②The 1# carbon black solid-liquid separation equipment uses a device based on the principle of vacuum filtration to separate the slurry into solid and liquid; ③The washing liquid L1 leaving the 1# pickling liquid storage tank is transported to the fly ash washing and decalcification unit, and the liquid-to-solid ratio of the washing liquid L1 to the carbon black is 1:1L / kg; ④The liquid transported from the 2# pickling liquid storage tank to the 1# carbon black solid-liquid separation equipment has a liquid-to-solid ratio of 5:1L / kg to the carbon black, and the mixing and washing time is 20min. The liquid leaving the 2# pickling liquid storage tank enters the 1# pickling liquid storage tank, and the liquid-to-solid ratio of the liquid to the carbon black is 1.6:1L / kg; ⑤From 3 #The liquid-to-solid ratio of the liquid transported from the pickling liquid storage tank to the 1# carbon black solid-liquid separation equipment to the carbon black is 5:1L / kg, and the mixing and washing time is 20min. The liquid leaving the 3# pickling liquid storage tank enters the 2# pickling liquid storage tank, and the liquid-to-solid ratio of the liquid to the carbon black is 1.6:1L / kg. The liquid-to-solid ratio of the washing liquid L2 entering the 3# pickling liquid storage tank to the carbon black is 1.6:1L / kg; ⑥The liquid-to-solid ratio of the washing liquid L2 transported from the carbon black water washing unit to the 1# carbon black solid-liquid separation equipment to the carbon black is 5:1L / kg, and the mixing and pulping time is 20min. The generated slurry is transported to the 2# pickling pulping tank for temporary storage, and finally transported to the carbon black water washing unit;

[0100] (2) Carbon black washing unit, process flow reference Figure 2 , the operating conditions are as follows:

[0101] ①The 2# carbon black solid-liquid separator is a washing filter press, which filters the slurry from the carbon black pickling unit, and the separated liquid enters the 1# water washing liquid storage tank; ②The liquid-to-solid ratio of the washing liquid L2 leaving the 1# water washing liquid storage tank and entering the fly ash water washing B unit to the fly ash is 2.4:1L / kg; ③The time for the liquid in the 2# water washing liquid storage tank to rinse the carbon black filter cake is 30min, and the liquid-to-solid ratio of the liquid leaving the 2# water washing liquid storage tank and entering the 1# water washing liquid storage tank to the fly ash is 2.4:1L / kg; ④The time for the liquid in the 3# water washing liquid storage tank to rinse the carbon black filter cake is 30min, and the liquid-to-solid ratio of the liquid leaving the 3# water washing liquid storage tank and entering the 2# water washing liquid storage tank to the fly ash is 2.4:1L / kg, the liquid-to-solid ratio of the make-up water B1 entering the 3# water washing liquid storage tank and the fly ash is 3.7:1L / kg, and the washing liquid L3 leaving the 3# water washing liquid storage tank is 0;

[0102] (3) Carbon black filter cake drying and granulation unit, process flow reference Figure 3 , the operating conditions are as follows:

[0103] ① The moisture content of the carbon black filter cake entering the carbon black filter cake drying equipment is 45%, and the moisture content of the carbon black leaving the carbon black filter cake drying equipment is 30%; ② The moisture content of the carbon black particles leaving the carbon black granulation equipment is 45%; ③ The moisture content of the dried particles leaving the carbon black drying equipment is 1.2%.

[0104] (4) Fly ash washing and decalcification unit, process flow reference Figure 4 , the operating conditions are as follows:

[0105] ① Transport fly ash, baking soda desulfurization ash, and washing liquid L1 to the 1# fly ash slurry tank, control the pH value of the slurry to 4, control the liquid-to-solid ratio of the slurry to 6:1L / kg, and control the Ca content in the slurry to 2+ / SO4 2- The molar ratio is 1; ② Continue to introduce air into the 1# fly ash slurrying tank, and the slurry and air mixing reaction time is 120min; ③ The 1# fly ash solid-liquid separator adopts a washing filter press; ④ The liquid-solid ratio of washing liquid L4 to fly ash is 2.9:1L / kg, and the liquid-solid ratio of washing liquid L5 to fly ash is 2.4:1L / kg.

[0106] (5) Fly ash washing unit A, process flow reference Figure 5 , the operating conditions are as follows:

[0107] ① The fly ash filter cake is transported to the 2A# fly ash slurrying tank, and 30% HCl solution is introduced to control the pH value of the slurry to 2.5, the liquid-to-solid ratio of the slurry is controlled to 4:1L / kg, and the slurry stirring reaction time is 180min; ② The 2A# fly ash solid-liquid separator adopts a washing filter press; ③ The liquid-to-solid ratio of washing liquid L5 to fly ash is 2.4:1L / kg, and the liquid-to-solid ratio of washing liquid L6 to fly ash is 2.4:1L / kg.

[0108] (6) Fly ash washing unit B, process flow reference Figure 6 , the operating conditions are as follows:

[0109] ① Transport the fly ash filter cake to the 2B# fly ash slurrying tank, control the liquid-to-solid ratio of the slurry to 4:1L / kg, and stir and wash the slurry for 20min; ② The 2B# fly ash solid-liquid separator uses a washing filter press; ③ The liquid-to-solid ratio of washing liquid L6 to fly ash is 2.4:1L / kg, and the liquid-to-solid ratio of washing liquid L2 to fly ash is 2.4:1L / kg.

[0110] The process processes 26,666.7 tons of fly ash annually, 5,000 tons of baking soda desulfurization ash annually, 22,515 tons of carbon black annually, 5,911 tons of 30% HCl solution annually, and 98,962 tons of water B1 annually, of which 35,510 tons are used for carbon black pickling. Assuming that the cost of baking soda desulfurization ash and HCl solution to the factory is 300 yuan / ton and 500 yuan / ton respectively, the value-added of carbon black after pickling is 800 yuan, and the cost of evaporation and crystallization of a ton of water is 80 yuan, then the process makes a profit of about 476 yuan per ton of carbon black. Assuming that the cost of sodium carbonate to the factory is 3,000 yuan / ton, this process saves 2,300 tons of sodium carbonate reagents and consumes 3,000 tons of baking soda desulfurization ash annually compared with the ordinary fly ash washing process, and the cost of a ton of fly ash is reduced by 225 yuan.

[0111] Example 2: Carbon black modification and fly ash shallow decalcification + washing + washing process

[0112] The rated processing capacity of a domestic waste power plant is 2000t / d, and its flue gas production is 360000Nm 3 / h, the average concentrations of HCl and SO2 were 550 mg / Nm 3 and 450mg / Nm 3 , operating for 8000 hours per year. The power plant uses Ca(OH)2 semi-dry deacidification, and the Ca / (S+0.5Cl) equivalent ratio is 1.3. The amount of fly ash generated accounts for 4% of the garbage treatment volume, that is, the fly ash output is 26666.7 tons / year. Sodium chloride and potassium chloride account for 15% of the fly ash, and the moisture content of the fly ash filter cake after solid-liquid separation is 35%. The pyrolysis carbon black produced by a waste tire pyrolysis plant has an ash content of 15%. After acid washing, the ash content is reduced to 8.6%, and the moisture content of the carbon black filter cake is 50%. The molar proportion of Na2CO3 in the baking soda desulfurization ash produced by a factory's flue gas dry desulfurization is 5%, and the molar proportions of Na2SO3 and Na2SO4 are 10% and 85%, respectively. The three types of waste are synergistically treated using carbon black modification and fly ash shallow decalcification + washing + washing process, such as Figure 8 As shown, the process flow is as follows:

[0113] ① Carbon black, HCl and washing liquid L2 enter the carbon black pickling unit together, the generated slurry enters the carbon black water washing unit, and the generated washing liquid L1 enters the water treatment system; ② The slurry leaving the carbon black pickling unit enters the carbon black water washing unit together with the make-up water B1, and the generated carbon black filter cake enters the carbon black filter cake drying and granulation unit, part of the generated washing liquid L2 enters the carbon black pickling unit, and the other part enters the fly ash water washing B unit, and no washing liquid L3 is generated; ③ The carbon black filter cake leaving the carbon black water washing unit enters the carbon black filter cake drying and granulation unit together with the granulation water; ④ Fly ash, baking soda desulfurization ash, washing liquid L 5. The fly ash filter cakes leaving the fly ash washing and decalcification unit enter the fly ash washing unit A together with the washing liquid L6, and the washing liquid L5 enters the fly ash washing and decalcification unit, and the fly ash filter cakes entering the fly ash washing unit B; ⑥ The fly ash filter cakes leaving the fly ash washing unit A enter the fly ash washing unit B together with the washing liquid L2, and the washing liquid L6 enters the fly ash washing unit A, and the fly ash filter cakes entering the cement kiln.

[0114] Next, combine Figure 1-6 The process is described in detail:

[0115] (1) Carbon black pickling unit, process flow reference Figure 1 , the operating conditions are as follows:

[0116] ① The particle size of carbon black in the 1# pickling pulping tank is less than 70μm, the liquid-to-solid ratio of the slurry is 6:1L / kg, and the H + The concentration is 1mol / L, and the slurry stirring and mixing reaction time is 180min; ②The 1# carbon black solid-liquid separation equipment uses a device based on the principle of vacuum filtration to separate the slurry into solids and liquids; ③The liquid-to-solid ratio of the washing liquid L1 leaving the 1# pickling liquid storage tank to the carbon black is 0.5:1L / kg; ④The liquid transported from the 2# pickling liquid storage tank to the 1# carbon black solid-liquid separation equipment has a liquid-to-solid ratio of 6:1L / kg to the carbon black, and the mixing and washing time is 30min. The liquid leaving the 2# pickling liquid storage tank enters the 1# pickling liquid storage tank, and the liquid-to-solid ratio of the liquid to the carbon black is 1.3:1L / kg; ⑤The liquid transported from the 3# pickling liquid storage tank to The liquid-to-solid ratio of the liquid in the 1# carbon black solid-liquid separation equipment to the carbon black is 6:1L / kg, the mixing and washing time is 30min, the liquid leaving the 3# pickling liquid storage tank enters the 2# pickling liquid storage tank, the liquid-to-solid ratio of the liquid to the carbon black is 1.3:1L / kg, and the liquid-to-solid ratio of the washing liquid L2 entering the 3# pickling liquid storage tank to the carbon black is 1.3:1L / kg; ⑥ The liquid-to-solid ratio of the washing liquid L2 transported from the carbon black water washing unit to the 1# carbon black solid-liquid separation equipment to the carbon black is 6:1L / kg, the mixing pulping time is 20min, and the produced pulp is transported to the 2# pickling pulping tank for temporary storage, and finally transported to the carbon black water washing unit;

[0117] (2) Carbon black washing unit, process flow reference Figure 2 , the operating conditions are as follows:

[0118] ①The 2# carbon black solid-liquid separator is a washing filter press, which filters the slurry from the carbon black pickling unit, and the separated liquid enters the 1# water washing liquid storage tank; ②The liquid-to-solid ratio of the washing liquid L2 leaving the 1# water washing liquid storage tank and entering the fly ash water washing B unit to the fly ash is 2.4:1L / kg; ③The time for the liquid in the 2# water washing liquid storage tank to rinse the carbon black filter cake is 40min, and the liquid-to-solid ratio of the liquid leaving the 2# water washing liquid storage tank and entering the 1# water washing liquid storage tank to the fly ash is 2.4:1L / kg; ④The time for the liquid in the 3# water washing liquid storage tank to rinse the carbon black filter cake is 40min, and the liquid-to-solid ratio of the liquid leaving the 3# water washing liquid storage tank and entering the 2# water washing liquid storage tank to the fly ash is 2.4:1L / kg, the liquid-to-solid ratio of the make-up water B1 entering the 3# water washing liquid storage tank and the fly ash is 2.6:1L / kg, and the washing liquid L3 leaving the 3# water washing liquid storage tank is 0;

[0119] (3) Carbon black filter cake drying and granulation unit, process flow reference Figure 3 , the operating conditions are as follows:

[0120] ① The moisture content of the carbon black filter cake entering the carbon black filter cake drying equipment is 50%, and the moisture content of the carbon black leaving the carbon black filter cake drying equipment is 30%; ② The moisture content of the carbon black particles leaving the carbon black granulation equipment is 45%; ③ The moisture content of the dried particles leaving the carbon black drying equipment is 1%.

[0121] (4) Fly ash washing and decalcification unit, process flow reference Figure 4 , the operating conditions are as follows:

[0122] ① Transport fly ash and baking soda desulfurization ash to the 1# fly ash slurry tank, control the liquid-solid ratio of the slurry to 3.5:1L / kg, and control the Ca content in the slurry to 2+ / SO4 2- The molar ratio is 0.98, and the slurry is mixed and stirred for 20 minutes; ②The 1# fly ash solid-liquid separator adopts a washing filter press; ③The liquid-solid ratio of washing liquid L4 to fly ash is 2:1L / kg, and the liquid-solid ratio of washing liquid L5 to fly ash is 2.4:1L / kg.

[0123] (5) Fly ash washing unit A, process flow reference Figure 5 , the operating conditions are as follows:

[0124] ① Transport the fly ash filter cake to the 2A# fly ash slurrying tank, control the liquid-solid ratio of the slurry to 3.5:1L / kg, and the slurry stirring reaction time is 20min; ② The 2A# fly ash solid-liquid separator adopts a washing filter press; ③ The liquid-solid ratio of washing liquid L5 to fly ash is 2.4:1L / kg, and the liquid-solid ratio of washing liquid L6 to fly ash is 2.4:1L / kg.

[0125] (6) Fly ash washing unit B, process flow reference Figure 6 , the operating conditions are as follows:

[0126] ① Transport the fly ash filter cake to the 2B# fly ash slurrying tank, control the liquid-to-solid ratio of the slurry to 3.5:1L / kg, and the slurry stirring and washing time is 20min; ② The 2B# fly ash solid-liquid separator adopts a washing filter press; ③ The liquid-to-solid ratio of washing liquid L6 to fly ash is 2.4:1L / kg, and the liquid-to-solid ratio of washing liquid L2 to fly ash is 2.4:1L / kg.

[0127] The process processes 26,666.7 tons of fly ash annually, 3,080 tons of baking soda desulfurization ash annually, 4,850 tons of carbon black annually, 931 tons of 30% HCl solution annually, and 69,734 tons of water replenishment B1 annually, of which 6,281 tons are used for carbon black pickling. Assuming that the cost of baking soda desulfurization ash and HCl solution to the factory is 300 yuan / ton and 500 yuan / ton respectively, the value-added of carbon black after pickling is 800 yuan, and the cost of evaporation and crystallization of water per ton is 80 yuan, then the process makes a profit of about 410 yuan per ton of carbon black.

[0128] Example 3: Carbon black modification and fly ash moderate decalcification + oxidation + acid leaching process

[0129] The rated processing capacity of a domestic waste power plant is 2000t / d, and its flue gas production is 360000Nm 3 / h, the average concentrations of HCl and SO2 were 500 mg / Nm 3 and 450mg / Nm 3 , operating for 8000 hours per year. The power plant uses Ca(OH)2 semi-dry deacidification, and the Ca / (S+0.5Cl) equivalent ratio is 1.2. The amount of fly ash produced accounts for 4% of the garbage treatment volume, that is, the fly ash output is 26666.7 tons / year. Sodium chloride and potassium chloride account for 15% of the fly ash, and the moisture content of the fly ash filter cake after solid-liquid separation is 35%. The pyrolysis carbon black produced by a waste tire pyrolysis plant has an ash content of 15%. After acid washing, the ash content is reduced to 8.6%, and the moisture content of the carbon black filter cake is 50%. The molar proportion of Na2CO3 in the baking soda desulfurization ash produced by a factory's flue gas dry desulfurization is 5%, and the molar proportions of Na2SO3 and Na2SO4 are 10% and 85%, respectively. The three types of waste are synergistically treated using carbon black modification and fly ash moderate decalcification + oxidation + acid leaching process, such as Fig. 9 As shown, the process flow is as follows:

[0130] ① Carbon black, HCl and washing liquid L2 enter the carbon black pickling unit together, the generated slurry enters the carbon black water washing unit, and the generated washing liquid L1 enters the fly ash washing and decalcification unit; ② The slurry leaving the carbon black pickling unit enters the carbon black water washing unit together with the make-up water B1, the generated carbon black filter cake enters the carbon black filter cake drying and granulation unit, part of the generated washing liquid L2 enters the carbon black pickling unit, and the other part enters the fly ash water washing A unit, and the generated washing liquid L3 enters the fly ash washing and decalcification unit; ③ The carbon black filter cake leaving the carbon black water washing unit enters the carbon black filter cake drying and granulation unit together with the granulation water; ④ Fly ash, baking soda desulfurization ash, washing liquid L1 and The washing liquid L3 enters the fly ash washing and decalcification unit together, which realizes moderate decalcification of the fly ash. The generated washing liquid L4 enters the water treatment system, and the generated fly ash filter cake enters the fly ash water washing A unit; ⑤ The fly ash filter cake, washing liquid L2, air and HCl leaving the fly ash washing and decalcification unit enter the fly ash water washing A unit together, and the generated washing liquid L5 enters the fly ash water washing B unit, and the generated fly ash filter cake enters the fly ash water washing B unit; ⑥ The fly ash filter cake, washing liquid L5 and HCl leaving the fly ash water washing A unit enter the fly ash water washing B unit together, the generated washing liquid L6 enters the water treatment system, and the generated fly ash filter cake enters the waste incinerator.

[0131] Next, combine Figure 1-6 The process is described in detail:

[0132] (1) Carbon black pickling unit, process flow reference Figure 1 , the operating conditions are as follows:

[0133] ① The particle size of carbon black in the 1# pickling pulping tank is less than 50μm, the liquid-to-solid ratio of the slurry is 5.5:1L / kg, and the H + The concentration is 1.5mol / L, and the slurry stirring and mixing reaction time is 180min; ②The 1# carbon black solid-liquid separation equipment adopts a washing filter press; ③The liquid-to-solid ratio of the washing liquid L1 leaving the 1# pickling liquid storage tank to the carbon black is 1:1L / kg; ④The washing time of the carbon black filter cake by the liquid transported from the 2# pickling liquid storage tank to the 1# carbon black solid-liquid separation equipment is 30min, and the liquid leaving the 2# pickling liquid storage tank enters the 1# pickling liquid storage tank, and the liquid-to-solid ratio of the liquid to the carbon black is 1.7:1L / kg; ⑤The liquid transported from the 3# pickling liquid storage tank to the 1# carbon The washing time of the carbon black filter cake with the liquid of the black solid-liquid separation equipment is 30 minutes. The liquid leaving the 3# pickling liquid storage tank enters the 2# pickling liquid storage tank. The liquid-solid ratio of the liquid to the carbon black is 1.7:1L / kg. The liquid-solid ratio of the washing liquid L2 entering the 3# pickling liquid storage tank to the carbon black is 1.7:1L / kg; ⑥ The liquid-solid ratio of the washing liquid L2 transported from the carbon black washing unit to the 2# pickling pulping tank to the carbon black is 5.5:1L / kg. The stirring pulping time of the 2# pickling pulping tank is 10 minutes, and the generated slurry is transported to the carbon black washing unit;

[0134] (2) Carbon black washing unit, process flow reference Figure 2 , the operating conditions are as follows:

[0135] ①The 2# carbon black solid-liquid separator is a washing filter press, which filters the slurry from the carbon black pickling unit, and the separated liquid enters the 1# water washing liquid storage tank; ②The liquid-to-solid ratio of the washing liquid L2 leaving the 1# water washing liquid storage tank and entering the fly ash water washing A unit to the fly ash is 1.1:1L / kg; ③The time for the liquid in the 2# water washing liquid storage tank to wash the carbon black filter cake is 30 minutes, and the liquid leaving the 2# water washing liquid storage tank and entering the 1# water washing liquid storage tank and the fly ash are 1.1:1L / kg. The liquid-to-solid ratio is 1.1:1L / kg; ④ The time for the liquid in the 3# water washing liquid storage tank to flush the carbon black filter cake is 30min, the liquid-to-solid ratio of the liquid leaving the 3# water washing liquid storage tank and entering the 2# water washing liquid storage tank to the fly ash is 1.1:1L / kg, the liquid-to-solid ratio of the make-up water B1 entering the 3# water washing liquid storage tank to the fly ash is 3.1:1L / kg, and the liquid-to-solid ratio of the washing liquid L3 leaving the 3# water washing liquid storage tank to the fly ash is 1.3:1L / kg.

[0136] (3) Carbon black filter cake drying and granulation unit, process flow reference Figure 3 , the operating conditions are as follows:

[0137] ① The moisture content of the carbon black filter cake entering the carbon black filter cake drying equipment is 50%, and the moisture content of the carbon black leaving the carbon black filter cake drying equipment is 25%; ② The moisture content of the carbon black particles leaving the carbon black granulation equipment is 45%; ③ The moisture content of the dried particles leaving the carbon black drying equipment is 1.2%.

[0138] (4) Process flow reference of fly ash washing and decalcification unit Figure 4 , the operating conditions are as follows:

[0139] ① Transport fly ash, baking soda desulfurization ash, and washing liquid L1 to the 1# fly ash slurry tank, control the pH value of the slurry to 11, control the liquid-to-solid ratio of the slurry to 5:1L / kg, and control the Ca content in the slurry to 2+ / SO4 2- The molar ratio is 1.01, and the slurry is mixed and stirred for 30 minutes; ② The 1# fly ash solid-liquid separator adopts a washing filter press; ③ The liquid-solid ratio of washing liquid L4 to fly ash is 1.34:1L / kg.

[0140] (5) Fly ash washing unit A, process flow reference Figure 5 , the operating conditions are as follows:

[0141] ① The fly ash filter cake is transported to the 2A# fly ash slurrying tank, and the pH value of the slurry is controlled to be 4.5 by 30% HCl solution, the liquid-to-solid ratio of the slurry is controlled to be 5:1L / kg, and the reaction time of introducing air into the slurry is 150min; ② The 2A# fly ash solid-liquid separator adopts a washing filter press; ③ The liquid-to-solid ratio of washing liquid L5 to fly ash is 1.1:1L / kg, and the liquid-to-solid ratio of washing liquid L2 to fly ash is 1.1:1L / kg.

[0142] (6) Fly ash washing unit B, process flow reference Figure 6 , the operating conditions are as follows:

[0143] ① The fly ash filter cake is transported to the 2B# fly ash slurrying tank, the liquid-to-solid ratio of the slurry is controlled to be 5:1 L / kg, the pH value of the slurry is controlled to be 2.5 by 30% HCl solution, and the slurry stirring and washing time is 120 min; ② The 2B# fly ash solid-liquid separator adopts a washing filter press; ③ The liquid-to-solid ratio of washing liquid L6 to fly ash is 1.1:1 L / kg.

[0144] The process processes 26,666.7 tons of fly ash annually, 2,734 tons of baking soda desulfurization ash annually, 11,470 tons of carbon black annually, 30% HCl solution consumption annually 3,530 tons, and 83,417 tons of water replenishment B1 annually, of which 19,664 tons are used for carbon black pickling. Assuming that the cost of baking soda desulfurization ash and HCl solution to the factory is 300 yuan / ton and 500 yuan / ton respectively, the value-added of carbon black after pickling is 800 yuan, and the cost of evaporation and crystallization of water per ton is 80 yuan, then the process will make a profit of about 437 yuan per ton of carbon black.

[0145] It should be noted that the above specific implementations are only preferred embodiments of the present invention and the technical principles used. Those skilled in the art should understand that various modifications, equivalent substitutions, changes, etc. can be made to the present invention. However, as long as these changes do not deviate from the spirit of the present invention, they should be within the scope of protection of the present invention. In addition, some terms used in the specification and claims of this application are not restrictive, but are only for the convenience of description.

Claims

1. A method for treating fly ash by modifying carbon black, characterized in that: The following steps are involved: S10. Provide a carbon black modification system consisting of a carbon black acid washing unit, a carbon black water washing unit, and a carbon black filter cake drying and granulation unit, a fly ash treatment system consisting of a fly ash washing and decalcification unit and a fly ash water washing unit, a water treatment system, and a garbage incinerator or cement kiln; S20, adding carbon black, acid solution and washing liquid L2 from the carbon black water washing unit into the carbon black pickling unit, performing pickling treatment on the carbon black to produce washing liquid L1 and slurry, transporting the washing liquid L1 to the fly ash washing and decalcification unit or the water treatment system, and transporting the slurry to the carbon black water washing unit; S30, adding water supplement B1 to the carbon black washing unit, washing the carbon black in the carbon black washing unit to produce washing liquid L2, washing liquid L3 and carbon black filter cake, conveying part of the washing liquid L2 to the carbon black acid washing unit, conveying the remaining washing liquid L2 to the fly ash washing unit, conveying the washing liquid L3 to the fly ash washing and decalcification unit, and conveying the carbon black filter cake to the carbon black filter cake drying and granulation unit for granulation; S40, adding fly ash, baking soda desulfurization ash and sulfite oxidant into the fly ash washing and decalcification unit to generate washing liquid and fly ash filter cake, conveying the washing liquid to the water treatment system, and conveying the fly ash filter cake to the fly ash water washing unit; S50, adding acid solution and sulfite oxidant to the fly ash washing unit to generate washing liquid and fly ash filter cake, conveying the washing liquid to the water treatment system or the fly ash washing and decalcification unit, and conveying the fly ash filter cake to the waste incinerator or cement kiln.

2. The method for treating fly ash by carbon black modification according to claim 1, characterized in that: The carbon black pickling unit comprises a 1# pickling pulping tank, a 2# pickling pulping tank, a 1# pickling liquid storage tank, a 2# pickling liquid storage tank, a 3# pickling liquid storage tank and a 1# carbon black solid-liquid separator; Step S20 specifically includes the following steps: The carbon black with a particle size of less than 70 μm is transported to the 1# pickling pulping tank; part of the liquid in the 1# pickling liquid storage tank is transported to the 1# pickling pulping tank, and the liquid-solid ratio of the slurry in the 1# pickling pulping tank is adjusted to 2:1~10:1 L / kg; the acid solution is added to the 1# pickling pulping tank, and the H+ concentration of the slurry in the 1# pickling pulping tank is adjusted to 0.5~3 mol / L; the slurry is stirred and mixed for 30~180 min. The slurry produced after the pickling is transported to the 1# carbon black solid-liquid separator for solid-liquid separation, and the separated liquid is transported to the 1# pickling liquid storage tank, and the separated solid remains in the 1# carbon black solid-liquid separator; part of the liquid in the 1# pickling liquid storage tank is transported as washing liquid L1 to the fly ash washing and decalcification unit or the water treatment system, and the liquid-solid ratio of the washing liquid L1 to the carbon black added to the 1# pickling pulping tank is 0.5:1~3:1 L / kg; The liquid in the 2# pickling liquid storage tank is transported to the 1# carbon black solid-liquid separator for washing the carbon black filter cake. The washing time of the carbon black filter cake is 10-60 minutes. The washed liquid is returned to the 2# pickling liquid storage tank. A part of the liquid in the 2# pickling liquid storage tank is transported to the 1# pickling liquid storage tank. The liquid-solid ratio of the liquid to the carbon black added to the 1# pickling pulping tank is 1:1-4:1 L / kg. The liquid in the 3# pickling liquid storage tank is transported to the 1# carbon black solid-liquid separator for washing the carbon black filter cake. The washing time of the carbon black filter cake is 10-60 minutes. The washed liquid is returned to the 3# pickling liquid storage tank. A part of the liquid in the 3# pickling liquid storage tank is transported to the 2# pickling liquid storage tank. The liquid-solid ratio of the liquid to the carbon black added to the 1# pickling pulping tank is 1:1-4:1 L / kg. A part of the washing liquid L2 from the carbon black water washing unit is added to the 3# pickling liquid storage tank. The liquid-solid ratio of the washing liquid L2 to the carbon black added to the 1# pickling pulping tank is 1:1-4:1 L / kg. The slurry or filter cake produced in the 1# carbon black solid-liquid separator is transported to the 2# acid washing pulping tank, and the formed slurry is transported to the carbon black water washing unit.

3. The method for treating fly ash by carbon black modification according to claim 2, characterized in that: The 1# carbon black solid-liquid separator is a vacuum filtration device or a washing filter press. When the 1# carbon black solid-liquid separator is a vacuum filtration device, a part of the washing liquid L2 generated by the carbon black washing unit is transported to the 1# carbon black solid-liquid separator to be mixed with the carbon black filter cake for slurrying. The mixing slurrying time is 10~60min, and the liquid-solid ratio of the prepared slurry is 2:1~5:1 L / kg. The produced slurry is transported to the 2# pickling slurrying tank; when the 1# carbon black solid-liquid separator is a washing filter press, a part of the washing liquid L2 generated by the carbon black washing unit is transported to the 2# pickling slurrying tank and mixed with the filter cake transported from the 1# carbon black solid-liquid separator to the 2# pickling slurrying tank for slurrying. The mixing slurrying time is 10~60min, and the liquid-solid ratio of the prepared slurry is 2:1~5:1 L / kg.

4. The method for treating fly ash by carbon black modification according to claim 1, characterized in that: The carbon black washing unit includes a 1# washing liquid storage tank, a 2# washing liquid storage tank, a 3# washing liquid storage tank and a 2# carbon black solid-liquid separator, wherein the 2# carbon black solid-liquid separator is a washing filter press; Step S30 includes the following steps: The slurry from the carbon black pickling unit is transported to the 2# carbon black solid-liquid separator, and the separated liquid is transported to the 1# water washing liquid storage tank, and the separated solid remains in the 2# carbon black solid-liquid separator; a part of the washing liquid L2 in the 1# water washing liquid storage tank is transported to the carbon black pickling unit, and the other part is transported to the fly ash water washing unit. The liquid-solid ratio of the washing liquid L2 transported to the fly ash water washing unit and the fly ash added to the fly ash washing and decalcification unit is 0.5:1~4:1 L / kg; The liquid in the 2# water washing liquid storage tank is transported to the 2# carbon black solid-liquid separator for washing the carbon black filter cake, and the washing time is 10~60min; the washed liquid is returned to the 2# water washing liquid storage tank, and the washed solid remains in the 2# carbon black solid-liquid separator; a part of the liquid in the 2# water washing liquid storage tank is transported to the 1# water washing liquid storage tank, and the liquid-solid ratio of this part of the liquid to the fly ash added to the fly ash washing and decalcification unit is 1:1~7:1 L / kg; The liquid in the 3# water washing liquid storage tank is transported to the 2# carbon black solid-liquid separator for washing the carbon black filter cake, and the washing time is 10~60min. The washed liquid is returned to the 3# water washing liquid storage tank, and the washed solid is transported to the carbon black filter cake drying and granulation unit; a part of the liquid in the 3# water washing liquid storage tank is transported to the 2# water washing liquid storage tank, and the liquid-solid ratio of this part of the liquid to the fly ash added to the fly ash washing and decalcification unit is 1:1~7:1 L / kg; another part of the liquid in the 3# water washing liquid storage tank is transported to the fly ash washing and decalcification unit as washing liquid L3, and the liquid-solid ratio of this washing liquid L3 to the fly ash added to the fly ash washing and decalcification unit is 1:1~3:1 L / kg; make-up water B1 is added to the 3# water washing liquid storage tank, and the liquid-solid ratio of this make-up water B1 to the fly ash added to the fly ash washing and decalcification unit is 2:1~7:1 L / kg.

5. The method for treating fly ash by carbon black modification according to claim 1, characterized in that: The carbon black filter cake drying and granulation unit includes carbon black filter cake drying equipment, carbon black granulation equipment, carbon black particle drying equipment, packaging equipment, exhaust gas dust removal bags, exhaust gas washing tower and chimney; The carbon black filter cake from the carbon black washing unit is transported to the carbon black filter cake drying equipment for pre-drying. The water content of the pre-dried carbon black is 5% to 30% lower than that of the carbon black particles at the outlet of the carbon black granulation equipment. The pre-dried carbon black is transported to the carbon black granulation equipment, and the dusty and acidic waste gas generated during the pre-drying process is transported to the waste gas dust removal bag; The pre-dried carbon black and granulation water are added into the carbon black granulation equipment and stirred and mixed. The water content of the prepared carbon black particles is 35% to 55%. The prepared carbon black particles are transported to the carbon black particle drying equipment; In the carbon black pellet drying equipment, the moisture content of the carbon black pellets is reduced to less than 1.5%. After drying and cooling, the carbon black pellets are transported to the packaging equipment, and the dusty and acidic waste gas generated is transported to the waste gas dust removal bag; The dusty and acidic waste gas is purified in turn by the waste gas dust removal bag and the waste gas washing tower and then discharged into the chimney.

6. The method for treating fly ash by carbon black modification according to claim 1, characterized in that: The fly ash washing and decalcification unit includes a 1# fly ash slurry tank, a 1# fly ash liquid storage tank and a 1# fly ash solid-liquid separator, wherein the 1# fly ash solid-liquid separator adopts a washing filter press or a horizontal screw dehydration centrifuge; Step S40 specifically includes the following steps: Add the fly ash to the No. 1 fly ash slurry tank, and send part of the liquid in the No. 1 fly ash liquid storage tank to the No. 1 fly ash slurry tank for slurrying; Decalcify the slurry in the No. 1 fly ash slurry tank; The decalcified slurry in the No. 1 fly ash slurrying tank is transported to the No. 1 fly ash solid-liquid separator, the separated liquid is transported to the No. 1 fly ash liquid storage tank, and the separated fly ash filter cake is transported to the fly ash water washing unit; Part of the liquid in the No. 1 fly ash storage tank is transported to the water treatment system as washing liquid L4, and the liquid-to-solid ratio of the washing liquid L4 to the fly ash added to the fly ash washing and decalcification unit is 1:1~6:1 L / kg; Among them, the liquid in the 1# fly ash storage tank also comes from the carbon black water washing unit or the fly ash water washing unit. The liquid-to-solid ratio of the washing liquid L3 from the carbon black water washing unit and the fly ash added to the fly ash washing and decalcification unit is 1:1~3:1 L / kg, and the liquid-to-solid ratio of the washing liquid L5 from the fly ash water washing unit and the fly ash added to the fly ash washing and decalcification unit is 1:1~4:1 L / kg.

7. The method for treating fly ash by carbon black modification according to claim 6, characterized in that: The decalcification treatment performed on the slurry in the No. 1 fly ash slurrying tank is any one of a shallow decalcification treatment, a medium decalcification treatment, and a heavy decalcification treatment; The shallow decalcification treatment is as follows: the baking soda desulfurization ash is mixed with part of the liquid in the 1# fly ash storage tank and then transported to the 1# fly ash slurry tank. The amount of baking soda desulfurization ash is adjusted to reduce the free Ca in the slurry. 2+ CO3 generated by hydrolysis of baking soda desulfurization ash 2- 、SO3 2- 、SO4 2- Generate CaCO3, CaSO3, CaSO4 precipitation to control Ca content in slurry 2+ / SO4 2- The molar ratio is 0.95-1.05; the liquid-solid ratio of the slurry is adjusted to 2:1-5:1 L / kg, and the slurry mixing reaction time is 10-60 min; The specific method of moderate decalcification is as follows: the washing liquid L1 from the carbon black pickling unit, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash are mixed and transported to the 1# fly ash slurry tank, and the H+ concentration in the mixed liquid of the washing liquid L1, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash is adjusted to 0.1~3mol / L; the pH value of the slurry in the 1# fly ash slurry tank is controlled to 10~12, and the Ca in the slurry is controlled to 1. 2+ / SO4 2- The molar ratio is 0.95-1.05; the liquid-to-solid ratio of the slurry is adjusted to 3:1-8:1 L / kg, and the slurry mixing reaction time is 10-60 min; The heavy decalcification treatment is as follows: the washing liquid L1 from the carbon black pickling unit, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash are mixed and transported to the 1# fly ash slurry tank, and the H content in the mixed liquid of the washing liquid L1, part of the liquid in the 1# fly ash storage tank and the baking soda desulfurization ash is adjusted. + The concentration is 0.1~3mol / L, the pH value of the slurry in the 1# fly ash slurry tank is controlled to be 3.5~5, and the Ca content in the slurry is controlled 2+ / SO4 2- The molar ratio is 0.95~1.05, and the liquid-to-solid ratio of the slurry is adjusted to 3:1~8:1 L / kg; sulfite oxidant is introduced into the 1# fly ash slurrying tank, and the mixing reaction time of the slurry and the sulfite oxidant is 30~180min.

8. The method for treating fly ash by modifying carbon black according to claim 1, characterized in that: The fly ash washing unit includes a fly ash washing unit A and a fly ash washing unit B. The fly ash washing unit A includes a 2A# fly ash slurry tank, a 2A# fly ash liquid storage tank, and a 2A# fly ash solid-liquid separator. The 2A# fly ash solid-liquid separator adopts a washing filter press or a horizontal screw dehydration centrifuge. Step S50 specifically includes the following steps: The fly ash filter cake from the fly ash washing and decalcification unit is transported to the 2A# fly ash slurry tank, and the liquid-solid ratio of the slurry in the 2A# fly ash slurry tank is adjusted by controlling the amount of liquid transported from the 2A# fly ash storage tank to the 2A# fly ash slurry tank; The liquid-solid ratio of the slurry in the 2A# fly ash pulping tank is controlled to be 2:1~5:1 L / kg, and acid is added to the 2A# fly ash pulping tank to adjust the pH value of the slurry to 1.5~3.

5. The slurry is stirred and reacted for 30~180 minutes, so that the salt and heavy metals in the fly ash filter cake enter the water; or, the liquid-solid ratio of the slurry in the 2A# fly ash pulping tank is controlled to be 3:1~8:1 L / kg, and acid is added to the 2A# fly ash pulping tank to adjust the pH value of the slurry to 3.5~5, and a sulfite oxidant is introduced, and the slurry and the sulfite oxidant are mixed and reacted for 30~180 minutes; or, the liquid-solid ratio of the slurry in the 2A# fly ash pulping tank is controlled to be 2:1~5:1 L / kg, and the slurry is stirred and reacted for 10~60 minutes, so that the salt in the fly ash filter cake enters the water; The slurry after fully mixing and reaction in the 2A# fly ash slurry making tank is transported to the 2A# fly ash solid-liquid separator, the separated liquid is transported to the 2A# fly ash liquid storage tank, and the separated fly ash filter cake is transported to the fly ash water washing unit B; Part of the liquid in the 2A# fly ash storage tank leaves the fly ash washing unit A and is transported to the fly ash washing and decalcification unit or the fly ash washing unit B as the washing liquid L5. The liquid-to-solid ratio of the washing liquid L5 to the fly ash added to the fly ash washing and decalcification unit is 0.5:1~4:1 L / kg; The washing liquid L2 from the carbon black water washing unit or the washing liquid L6 from the fly ash water washing B unit is transported to the 2A# fly ash storage tank, the liquid-solid ratio of the washing liquid L2 from the carbon black water washing unit to the fly ash added to the fly ash washing and decalcification unit is 0.5:1~2:1 L / kg, and the liquid-solid ratio of the washing liquid L6 from the fly ash water washing B unit to the fly ash added to the fly ash washing and decalcification unit is 1:1~4:1 L / kg.

9. The method for treating fly ash by carbon black modification according to claim 8, characterized in that: The fly ash washing unit B includes a 2B# fly ash slurry tank, a 2B# fly ash liquid storage tank, and a 2B# fly ash solid-liquid separator, wherein the 2B# fly ash solid-liquid separator adopts a washing filter press or a horizontal screw dehydration centrifuge; Step S50 also includes the following steps: The fly ash filter cake from the fly ash washing unit A is transported to the 2B# fly ash slurry tank, and the liquid-to-solid ratio of the slurry in the 2B# fly ash slurry tank is adjusted to 2:1~5:1 L / kg by controlling the amount of liquid transported from the 2B# fly ash storage tank to the 2B# fly ash slurry tank; Mix and stir the materials in the 2B# fly ash slurry tank to dilute the salt in the fly ash filter cake into the water. The slurry stirring time is 10-60 minutes. Alternatively, add acid to the 2B# fly ash slurry tank to adjust the pH value of the slurry to 1.5-3.5, so that the salt and heavy metals in the fly ash filter cake enter the water. The slurry stirring reaction time is 30-180 minutes. The slurry after fully mixing and reacting in the 2B# fly ash slurry making tank is transported to the 2B# fly ash solid-liquid separator, and the separated liquid is transported to the 2B# fly ash liquid storage tank. The separated fly ash filter cake is mixed with quicklime or slaked lime and then transported to the waste incinerator or cement kiln; Part of the liquid in the 2B# fly ash storage tank leaves the fly ash washing unit B and is transported to the 2A# fly ash storage tank or the water treatment system as the washing liquid L6. The liquid-to-solid ratio of the washing liquid L6 to the fly ash added to the fly ash washing and decalcification unit is 0.5:1~4:1 L / kg; The washing liquid L2 from the carbon black water washing unit or the washing liquid L5 from the 2A# fly ash storage tank is transported to the 2B# fly ash storage tank, the liquid-to-solid ratio of the washing liquid L2 from the carbon black water washing unit and the fly ash added to the fly ash washing and decalcification unit is 1:1~4:1 L / kg, and the liquid-to-solid ratio of the washing liquid L5 from the 2A# fly ash storage tank and the fly ash added to the fly ash washing and decalcification unit is 0.5:1~2:1 L / kg.

10. The method for treating fly ash by carbon black modification according to any one of claims 1 to 9, characterized in that: The added sulfite oxidant is air or H2O2 solution; if H2O2 solution is added, the molar ratio of H2O2 to sulfite is 1-1.2; if air is introduced, the molar ratio of O2 in the air to sulfite is 1.2-2.5.

Images