System and method for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln

Abstract

The application provides a system and method for co-processing waste liquid and household garbage incineration fly ash in a cement kiln. After being modified by a small amount of quicklime, the household garbage incineration fly ash is mixed and reacted with waste hydrochloric acid, waste emulsion and the like, and is separated to obtain high-value-added materials such as organic matter aggregate, fine powder, high-calorific-value waste oil, ultrafine calcium carbonate, ammonium chloride crystals and miscellaneous salt. Meanwhile, the process is coupled with a cement clinker production line, and the characteristics of waste heat contained in the flue gas system of the cement production line, heat supplement required by the firing system and water supplement required by the raw material batching station system are utilized to realize the accommodation of part of the materials. The system and method have the characteristics of treating and disposing industrial solid waste in the mode of 'waste treatment by waste', multiple products with added value are produced in the whole process, waste heat of the cement kiln is recycled, carbon dioxide supplement of the cement line can be realized, and the system and method have a broad prospect in the hazardous waste utilization and disposal industry.

Description

Technical Field

[0001] This invention belongs to the field of hazardous waste disposal and resource utilization, specifically relating to a system and method for co-processing waste liquid and fly ash from municipal solid waste incineration in a cement kiln. Background Technology

[0002] Waste incineration fly ash, industrial waste acid, and waste emulsions are widely present in industrial production, constituting large quantities of industrial waste that are difficult to dispose of and costly to treat. Among these, municipal solid waste incineration fly ash is listed in the National Hazardous Waste List due to pollutants such as heavy metals and dioxins. With the increasing volume of waste incineration fly ash and the growing scarcity of land, the resource utilization of fly ash and its solidified products will become an inevitable requirement and trend in future fly ash treatment. Future fly ash treatment technologies will inevitably develop towards universal applicability, high stability, low cost, and resource recycling. Waste inorganic acids specifically refer to the various waste inorganic acids listed in the National Hazardous Waste List "HW34 Waste Acids," which are classified as hazardous waste. They are characterized by high corrosivity, high toxicity, easy accumulation, instability, low calorific value, and easy loss. If not properly treated and arbitrarily dumped, they will cause serious secondary pollution; furthermore, treatment requires high costs for reagents and secondary pollution control. With rapid economic development, the production of waste emulsions has gradually increased. Due to the presence of a large amount of surfactants in emulsion waste, its stability is extremely high, and conventional coagulation sedimentation and coagulation flotation methods are not ideal for its treatment. Therefore, low-cost, high-efficiency treatment processes for these wastes are of great significance for promoting the healthy development of the industry and the construction of ecological civilization.

[0003] CN201810813627.7 discloses a waste acid co-treatment process in the resource-based refining of fly ash from municipal solid waste incineration. This process involves dissolving the fly ash with a large amount of waste acid, followed by multiple rinsings and treatment of the filtrate to reduce the content of dioxins, heavy metals, and salts, while simultaneously separating industrial salts such as sodium chloride and potassium chloride. CN202310174452.0 discloses a circulating fluidized bed boiler system for co-firing industrial solid and oily liquid hazardous wastes. This invention utilizes a circulating fluidized bed boiler to resource-based, energy-based, and harmlessly treat industrial solid hazardous wastes such as waste activated carbon and waste resin, as well as hazardous wastes such as waste engine oil, waste lubricating oil, waste emulsion, and waste diesel. CN201710872466.4 discloses a combined treatment system for industrial sludge, waste emulsion slag, and metallurgical ash, and its power generation process. This system treats, dries, and uses the combined sludge and emulsion slag treatment device for industrial sludge, waste emulsion slag, and metallurgical ash for power generation. CN201911375178.3 discloses a waste emulsion treatment device and method, employing an oil-water separation system, an iron-carbon micro-electrolysis reaction system, and a Fenton reaction system to decompose, oxidize, and dispose of the waste emulsion. CN201910145442.8 discloses a high-efficiency treatment process for high-concentration emulsions, disposing of the emulsions through flocculation separation and other methods. Overall, the harmless and resource-based treatment of waste incineration fly ash, waste acid, and waste emulsions faces challenges such as high cost, high energy consumption, and long process flows. Summary of the Invention

[0004] To address the aforementioned issues, this invention discloses a system and method for co-processing waste liquid and municipal solid waste incineration fly ash in cement kilns. This system solves the problems of insufficient harmlessness, low efficiency, and high cost in the current individual or mixed treatment of waste incineration fly ash, waste acid, and waste emulsion.

[0005] To achieve the above objectives, the technical solution of the present invention is as follows:

[0006] A system and method for co-processing waste liquid and fly ash from municipal solid waste incineration in a cement kiln, the system comprising a solid material mixer (1), a crusher (2), a reactor (3), a first-stage solid-liquid separator (4), an oil-water separator (5), a first-stage clarified liquid storage tank (6), a liquid mixer (7), a bubbling reactor (8), a second-stage solid-liquid separator (9), a second-stage clarified liquid storage tank (10), a cooling system (11), a freezing and salt separation system (12), a mother liquor storage tank (13), a flash concentration system (14), a bubbling bed dryer (15), a dryer (401), a screening machine (402), a silo (403), a pneumatic conveying pump (404), an oil storage tank (501), a conveying pump (502), and a refrigeration unit (1101).

[0007] A small amount of quicklime and municipal solid waste incineration fly ash, evenly mixed, are fed into a solid material mixer (1) via a feeder for mixing. The quicklime serves to modify the fly ash. The outlet of the solid material mixer (1) is connected to the inlet of the crusher (2), and the outlet of the crusher (2) is connected to the inlet of the reactor (3). After mixing, the solid material is crushed by the crusher (2) and then fed into the reactor (3). Waste acid containing organic matter and waste emulsion are added to the reactor in proportion and mixed with the crushed solid material. At the same time, a certain amount of polyacrylamide is added to enhance the flocculation effect. The outlet of the reactor (3) is connected to the inlet of the first-stage solid-liquid separator (4), the outlet of the first-stage solid-liquid separator (4) is connected to the inlet of the oil-water separator (5), the outlet of the oil-water separator (5) is connected to the inlet of the first-stage clarified liquid storage tank (6), and the outlet of the first-stage clarified liquid storage tank (6) is connected to the liquid mixer (7). The first-stage solid-liquid separator (4) separates the solid and liquid phases of the water mixture from the reactor. The liquid phase enters the oil-water separator (5) for oil-water separation. The resulting water phase is sent to the first-stage clarified liquid storage tank (6) for temporary storage as the separated clarified liquid, and then sent to the liquid mixer (7). The outlet of the liquid mixer (7) is connected to the inlet of the bubbling reactor (8), and the air inlet of the bubbling reactor (8) is connected to the air outlet of the dryer (401). A certain concentration of ammonia solution is added to the liquid mixer (7) and mixed with the clarified liquid from the first-stage clarified liquid storage tank (6). Then, it is sent to the bubbling reactor (8) to react fully with the air from the dryer (401). The outlet of the bubbling reactor (8) is connected to the inlet of the second-stage solid-liquid separator (9), and the outlet of the second-stage solid-liquid separator (9) is connected to the inlet of the second-stage clarified liquid storage tank (10). After the second-stage solid-liquid separator (9) separates the solid and liquid phases of the mixture from the bubbling reactor (8), the liquid phase enters the second-stage clarified liquid storage tank (10) for temporary storage. The outlet of the second-stage clarified liquid storage tank (10) is connected to the inlet of the cooling system (11), the outlet of the cooling system (11) is connected to the inlet of the freezing salt separation system (12), and the outlet of the freezing salt separation system (12) is connected to the inlet of the mother liquor storage tank (13). The clarified liquid from the second-stage clarified liquid storage tank (10) is sent to the cooling system (11) for cooling, and then enters the freezing salt separation system (12). The different solubilities of different compounds change with temperature to separate the ammonium chloride crystals. The remaining mother liquor is temporarily stored in the mother liquor storage tank (13), and a portion of the temporarily stored mother liquor is returned to the cooling system (11) for further salt separation according to the process. The outlet of the mother liquor storage tank (13) is connected to the inlet of the flash concentration system (14) and the outlet is connected to the inlet of the bubble bed dryer (15). The air inlet of the bubble bed dryer (15) is connected to the air outlet of the dryer (401). The mother liquor in the mother liquor storage tank (13) is sent into the flash concentration system (14) to obtain sodium chloride mixed salt. The wastewater generated in the flash concentration system (14) is sent to the raw material station for batching. The mixed salt is dried by the bubble bed dryer (15) to obtain sodium chloride mixed salt crystals.

[0008] Preferably, the inlet of the first-stage solid-liquid separator (4) is connected to the outlet of the reactor (3). The first-stage solid-liquid separator (4) separates the solid and liquid phases of the mixture effluent from the reactor, and the separated solid material is aggregate containing organic matter. The solid phase outlet of the first solid-liquid separator (4) is connected to the inlet of the dryer (401), and the aggregate containing organic matter is fed into the dryer (401) to reduce its moisture content. The air inlet of the dryer (401) is connected to the air outlet of the SP boiler, and the high-temperature flue gas (200°C) from the SP boiler outlet is used as a heat source. The outlet of the dryer (401) is connected to the inlet of the screening machine (402), and the coarse and fine materials containing organic matter are screened. The coarse material separated by the screening machine (402) is used as organic aggregate and can be used to make ceramsite or building materials. The undersize outlet of the screening machine (402) is connected to the inlet of the silo (403), and the outlet of the silo (403) is connected to the cement kiln decomposition furnace. After the undersize fine material enters the silo (403) for temporary storage, it is sent into the cement kiln decomposition furnace through the pneumatic conveying pump (404).

[0009] Preferably, the inlet of the oil-water separator (5) is connected to the liquid phase outlet of the first-stage solid-liquid separator (4), and the oil-water separator (5) separates the oil and water in the mixture of solid and liquid. The outlet of the oil-water separator (5) is connected to the inlet of the oil storage tank (501), and the outlet of the oil storage tank (501) is connected to the tertiary air duct of the cement kiln. The separated oil phase material is sent into the tertiary air duct of the cement kiln through the transfer pump (502) to supply heat to the cement kiln.

[0010] Preferably, the inlet of the bubbling reactor (8) is connected to the outlet of the liquid mixer (7) to perform a bubbling reaction on the effluent from the liquid mixer. The air inlet of the bubbling reactor (8) is connected to the air outlet of the dryer (401), using carbon dioxide from the air outlet of the dryer (401) as the reaction raw material. The air outlet is the gas from the 200°C high-temperature flue gas at the outlet of the SP furnace after drying the organic aggregate. Its carbon dioxide content is 15-20% (dry air). The drying process does not consume carbon dioxide. When it enters the bubbling reactor (8), the temperature drops to 120°C. After the reaction, the gas is discharged from the kiln tail chimney. The second-stage solid-liquid separator (9) separates the solid and liquid phases of the effluent mixture from the bubbling reactor (8). The solid phase after separation is ultrafine calcium carbonate powder, which has a high added value.

[0011] Preferably, the cooling system (11) uses a refrigeration unit (1101) for heat exchange and cooling. Part of the temporarily stored mother liquor in the mother liquor storage tank (13) is returned to the cooling system (11) at a return ratio of 1:10. After mixing with the clarified liquid in the second-stage clarified liquid storage tank (10), the liquid is cooled down and then enters the freezing and salt separation system (12). The system uses the difference in solubility of different compounds with temperature to separate the salts and separate ammonium chloride crystals, which can be used as raw materials for fertilizers and other products.

[0012] Preferably, the air inlet of the bubbling bed dryer (15) is connected to the air outlet of the dryer (401). The residual heat in the air outlet of the dryer (401) is used to dry the mixed salt solution in the flash concentration system (14). The air outlet is the gas containing organic aggregate after drying the 200°C high-temperature flue gas from the SP furnace outlet. When it enters the bubbling bed dryer (15), the temperature drops to 120°C. After the reaction, the gas is discharged from the kiln tail chimney. Sodium chloride mixed salt can be obtained after drying, which can be used as a raw material for hemolysin, etc.

[0013] The method of using a cement kiln co-processing waste liquid and municipal solid waste incineration fly ash system described in this invention includes S1: mixing municipal solid waste incineration fly ash with a certain amount of quicklime and then feeding it into a mixer (1) for mixing;

[0014] S2: The mixed material is fed into the crusher (2) to crush the large particles of fly ash;

[0015] S3: A certain proportion of waste hydrochloric acid (HCl effective concentration of 5-20%), waste emulsion (oil content of 2-10%), PAM / PAC and crushed fly ash mixture are sent into the reactor (3) and stirred for 30-60 min.

[0016] S4: The solid-liquid mixture is then fed into the first-stage solid-liquid separator (4). The wet solid material separated at the bottom of the first-stage solid-liquid separator (4) is organic aggregate, while the liquid at the top overflows into the oil-water separator (5).

[0017] S5: A high-temperature flue gas is drawn from the SP furnace outlet of the cement kiln clinker production line and the wet organic aggregate is dried in the dryer (401). The drying exhaust gas is then used in the downstream section, and the dried material enters the screening machine (402).

[0018] S6: The coarse material after screening is organic aggregate, while the fine material is mainly silicon-aluminum fine powder. The particle size of the coarse material is 0.5-15mm, and the particle size of the fine powder is 30-500μm. The fine material is sent to the cement kiln decomposition furnace via a pneumatic conveying pump (404).

[0019] S7: The high-calorific-value waste oil from the outlet of the oil-water separator (5) enters the oil storage tank (501) for storage. The waste oil is sent to the tertiary air duct for combustion by the transfer pump (502) to increase the furnace temperature of the decomposition furnace and reduce the coal consumption of the decomposition furnace.

[0020] S8: The clarified liquid produced by the oil-water separator (5) enters the first-stage clarified liquid storage tank (6) for storage. The clarified liquid contains a large amount of Ca. 2+ Cl - Na + K + SO4 2- Plasma;

[0021] S9: The ammonia solution and the clarified solution in S9 are mixed in a mixer (7). The mass concentration of the ammonia solution is about 5-28%, and the main ion in the mixer (7) is Ca. 2+ Cl - Na + K + SO4 2- NH4 + wait;

[0022] S10: After stabilization, the ammonia-containing clarified liquid is sent into the bubbling reactor (8), and at the same time, the CO2-containing dry flue gas from the cement kiln is introduced into the bubbling reactor (8). The CO2 in the flue gas reacts with the Ca in the clarified liquid. 2+ The reaction produces CaCO3 precipitate, partially solidifying the CO2 in the flue gas. The resulting waste gas is then sent to the kiln tail chimney of the cement production line. To ensure an excess of CO2 during the reaction, the pH of the liquid needs to be controlled to be less than 7.

[0023] S11: After the reaction is complete, the solid-liquid mixture in the bubbling reactor (8) is discharged and sent to the second-stage solid-liquid separator (9) to separate ultrafine calcium carbonate powder. The clarified liquid after the reaction is sent to the second-stage clarified liquid storage tank (10) for storage. The main ion in the clarified liquid is Cl. - Na + K + SO4 2- NH4 + wait;

[0024] S12: The clarified liquid and the refluxed mother liquor from S12 are sent to the cooling system (11) for cooling. After freezing and salt separation (12), NH4Cl crystals can be obtained. The mother liquor is then sent to the mother liquor storage tank (13). The main ion in the mother liquor is Cl. - Na + K + SO4 2- In order to control the stability of the liquid level in the mother liquor storage tank (13), a portion of the mother liquor in the mother liquor storage tank (13) is returned to the cooling system (11), and the return ratio is controlled to be 1:5-1:15.

[0025] S13: Finally, the mother liquor in the mother liquor storage tank (13) is sent to the flash evaporator (14) to obtain sodium chloride mixed salt. The wastewater generated in the flash evaporator (14) is sent to the raw material station for batching. The mixed salt is dried by the bubble bed dryer (15) to obtain sodium chloride mixed salt crystals.

[0026] The beneficial effects of this invention are:

[0027] 1. Comprehensive Utilization of Hazardous Waste. Fly ash from municipal solid waste incineration is an excellent neutralizing and flocculant. Mixing modified fly ash with waste acid and waste emulsion can break down the oil droplets in the waste emulsion, separating fatty acid soaps into fatty acids. Simultaneously, the fly ash can adsorb, flocculate, and precipitate the waste acid and demulsified fatty acids, while the salts in the fly ash dissolve into the solution, resulting in significant comprehensive utilization of hazardous waste.

[0028] 2. Layered recovery of multiple value-added products reduces costs and generates profits. The system, through a progressive process involving reaction, solid-liquid separation, and cryogenic desalination, yields various products such as organic aggregates, ultrafine calcium carbonate powder, ammonium chloride crystals, and sodium chloride salts. Organic aggregates can be used to produce ceramsite or building materials; ultrafine calcium carbonate powder can be used as an additive in high-end cosmetics and facial cleansers; ammonium chloride crystals can be used as a raw material for fertilizers; and sodium chloride salts can be used to prepare de-icing agents. This process, employing a "waste-to-waste" approach, significantly reduces the disposal costs of waste acid and waste emulsions. Simultaneously, the revenue from various value-added products can offset some of the fly ash disposal costs, achieving the goal of cost reduction and profit generation.

[0029] 3. Carbon dioxide recovery from flue gas and carbon emission reduction. The high-temperature flue gas at the SP furnace outlet contains a large amount of carbon dioxide, accounting for approximately 15-20% of the dry weight of the flue gas. If it enters the kiln tail chimney directly without treatment, it will not only result in a large amount of carbon emissions but also waste carbon-containing resources. The system reacts the flue gas with components in ammonia water and fly ash through bubbling, turning the carbon dioxide in the high-temperature flue gas into a raw material for value-added products, thus achieving carbon dioxide recovery from the flue gas and achieving the goal of carbon emission reduction.

[0030] 4. Staged utilization of high-temperature flue gas waste heat to achieve comprehensive waste heat utilization. The high-temperature flue gas at the SP furnace outlet is about 200°C, with low moisture content and large air volume. In the system, it is used for drying aggregates after solid-liquid separation. After drying the aggregates, the flue gas temperature is about 120°C, which can be used for staged utilization of waste heat for the evaporation and drying of sodium chloride and other salt solutions, thus achieving the purpose of comprehensive waste heat utilization.

[0031] 5. The entire system has no wastewater discharge. After the added value products are recycled in layers during system operation, the wastewater generated is sent to the cement production line batching station to realize the resource utilization of wastewater. The entire system has no wastewater discharge. Attached Figure Description

[0032] The accompanying drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component shown in the various figures may be denoted by the same reference numeral. For clarity, not every component is labeled in each figure. Embodiments of various aspects of the invention will now be described by way of example and with reference to the accompanying drawings, wherein:

[0033] Figure 1System flowchart;

[0034] Among them: solid material mixer (1), crusher (2), reaction vessel (3), first-stage solid-liquid separator (4), oil-water separator (5), first-stage clarified liquid storage tank (6), liquid mixer (7), bubbling reactor (8), second-stage solid-liquid separator (9), second-stage clarified liquid storage tank (10), cooling system (11), freezing and salt separation system (12), mother liquor storage tank (13), flash evaporation and concentration system (14), bubbling bed dryer (15), dryer (401), screening machine (402), silo (403), pneumatic conveying pump (404), oil storage tank (501), conveying pump (502), and refrigeration unit (1101). Detailed Implementation

[0035] The present invention will be further illustrated below with reference to the accompanying drawings and specific embodiments. It should be understood that the following specific embodiments are for illustrative purposes only and are not intended to limit the scope of the invention. For those skilled in the art, modifications can still be made to the described technical solutions with reference to the following embodiments, or equivalent substitutions can be made to some of the technical features. Any modifications, equivalent substitutions, improvements, system deletions, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

[0036] The system flowchart provided by this invention is as follows: Figure 1 As shown, the system includes a solid material mixer (1), a crusher (2), a reactor (3), a first-stage solid-liquid separator (4), an oil-water separator (5), a first-stage clarified liquid storage tank (6), a liquid mixer (7), a bubble reactor (8), a second-stage solid-liquid separator (9), a second-stage clarified liquid storage tank (10), a cooling system (11), a freezing and salt separation system (12), a mother liquor storage tank (13), a flash concentration system (14), a bubble bed dryer (15), a dryer (401), a screening machine (402), a silo (403), a pneumatic conveying pump (404), an oil storage tank (501), a conveying pump (502), and a refrigeration unit (1101).

[0037] Specifically, the fly ash from municipal solid waste incineration is mixed with a certain amount of quicklime in a mixer (1). After the mixture is evenly mixed, the material is fed into a crusher (2) to break up the large particles of agglomerated fly ash in order to improve the efficiency of subsequent reactions.

[0038] Specifically, a certain proportion of waste hydrochloric acid (HCl effective concentration of 5-20%), waste emulsion (oil content of 2-10%), PAM / PAC and fly ash crushed by crusher (2) are fed into the reactor (3) for full reaction, and the stirring reaction time is 30-60 min.

[0039] Specifically, the solid-liquid mixture that has fully reacted in the reactor (3) is sent to the first-stage solid-liquid separator (4). The wet solid material separated at the bottom of the first-stage solid-liquid separator (4) is organic aggregate, while the liquid at the top overflows into the oil-water separator (5).

[0040] Specifically, the high-temperature flue gas from the SP furnace outlet of the cement kiln clinker production line is introduced into the dryer (401), where the wet organic aggregate is dried. The drying exhaust gas is then used in the downstream section, and the dried material enters the screening machine (402).

[0041] Specifically, the coarse material after screening by the screening machine (402) is organic aggregate, and the fine material is mainly silicon-aluminum fine powder. The particle size of the coarse material is 0.5-15mm, and the particle size of the fine powder is 30-500μm. The fine material is sent to the cement kiln decomposition furnace by the pneumatic conveying pump (404).

[0042] Specifically, the high-calorific-value waste oil from the oil-water separator (5) is stored in the oil storage tank (501). A transfer pump (502) then sends the waste oil to the tertiary air duct for combustion support, thereby increasing the furnace temperature of the decomposition furnace and reducing coal consumption. The clarified liquid produced by the oil-water separator (5) is stored in the first-stage clarified liquid storage tank (6). The clarified liquid contains a large amount of Ca. 2+ Cl - Na + K + SO4 2- Plasma.

[0043] Specifically, the clarified liquid stored in the first-stage clarified liquid storage tank (6) is mixed with ammonia water in a mixer (7). The mass concentration of ammonia water is approximately 5-28%, and the main ion in the mixer (7) is Ca. 2+ Cl - Na + K + SO4 2- NH 4+ wait.

[0044] Specifically, after the reaction in the mixer (7) stabilizes, the ammonia-containing clarified liquid is sent to the bubbling reactor (8), and at the same time, the CO2-containing dry flue gas from the cement kiln is introduced into the bubbling reactor (8). The CO2 in the flue gas reacts with the Ca in the clarified liquid. 2+ The reaction produces CaCO3 precipitate, partially solidifying the CO2 in the flue gas. The resulting waste gas is then sent to the kiln tail chimney of the cement production line. To ensure an excess of CO2 during the reaction, the pH of the liquid needs to be controlled to be less than 7.

[0045] Specifically, after the ammonia water clarified liquid reacts fully with the CO2-containing dry flue gas from the cement kiln, the solid-liquid mixture in the bubbling reactor (8) is discharged and sent to the second-stage solid-liquid separator (9) to separate ultrafine calcium carbonate powder. The clarified liquid after the reaction is sent to the second-stage clarified liquid storage tank (10) for storage. The main ion in the clarified liquid is Cl. - Na + K + SO4 2- NH 4+ wait;

[0046] Specifically, the clarified liquid in the second-stage clarified liquid storage tank (10) and the returned mother liquor are sent to the cooling system (11) for cooling. After freezing and salt separation (12), NH4Cl crystals can be obtained. The mother liquor is then sent to the mother liquor storage tank (13). The main ion in the mother liquor is Cl. - Na + K + SO4 2- In order to control the stability of the liquid level in the mother liquor storage tank (13), a portion of the mother liquor in the mother liquor storage tank (13) is returned to the cooling system (11), and the return ratio is controlled to be 1:5-1:15.

[0047] Specifically, the mother liquor in the mother liquor storage tank (13) is sent to the flash evaporator (14) to obtain sodium chloride mixed salt. The wastewater generated in the flash evaporator (14) is sent to the raw material station for batching. The mixed salt is dried by the bubble bed dryer (15) to obtain sodium chloride mixed salt crystals.

[0048] Example 1

[0049] The following analysis examines the test parameters of a 133,000 t / a cement kiln co-processing waste liquid and municipal solid waste incineration production line. The specific test operation parameters are as follows:

[0050] Cement kiln scale for co-processing: 5000t / d (clinker production capacity);

[0051] The capacity for treating fly ash from municipal solid waste incineration is 100,000 tons per year (13.9 tons per hour).

[0052] Waste hydrochloric acid treatment capacity: 13,000 t / a (1.8 t / h);

[0053] Waste emulsion: 20,000 t / a (2.8 t / h);

[0054] Quicklime consumption: 0.5 t / h;

[0055] PAC / PAM consumption: 20 kg / h;

[0056] Ammonia water consumption (20%): 30,000 t / a (4.2 t / h);

[0057] Organic aggregate production: 22,000 t / a (3.1 t / h);

[0058] Fine ash after treatment: 70,000 tons / year (9.7 t / h);

[0059] Production of ultrafine calcium carbonate: 45,000 t / a (6.25 t / h);

[0060] Waste oil generation: 2000 t / a;

[0061] Ammonium chloride crystal production (dry basis): 18,700 t / a (2.6 t / h);

[0062] Sodium chloride contaminants: 22,000 t / a (3.05 t / h);

[0063] High-temperature flue gas extracted from the SP furnace: 40000 Nm 3 / h;

[0064] The temperature of the flue gas extracted by the SP furnace is 200℃.

[0065] Flue gas volume of bubbling reaction tower: 30000 Nm3 / h;

[0066] Inlet flue gas temperature of the bubbling reaction tower: 120℃;

[0067] Bubble bed dryer inlet flue gas volume: 1200 Nm 3 / h;

[0068] Bubble bed dryer inlet flue gas temperature: 120℃;

[0069] Flue gas carbon dioxide replenishment capacity: 20,000 t / a (2.75 t / h);

[0070] Reflux ratio: 1:10;

[0071] Wastewater discharge: 0 t / a;

[0072] Example 2

[0073] The following analysis uses the 260,000 t / a cement kiln co-processing waste liquid and municipal solid waste incineration production line as an example to analyze the test parameters. The specific test operation parameters are as follows:

[0074] Cement kiln scale for co-processing: 10,000 t / d (clinker production capacity);

[0075] The capacity for treating fly ash from municipal solid waste incineration is 200,000 tons per year (27.8 tons per hour).

[0076] Waste hydrochloric acid treatment capacity: 20,000 t / a (2.8 t / h);

[0077] Waste emulsion: 40,000 t / a (5.6 t / h);

[0078] Quicklime consumption: 0.9 t / h;

[0079] PAC / PAM consumption: 35 kg / h;

[0080] Ammonia water consumption (20%): 62,000 t / a (8.6 t / h);

[0081] Organic aggregate production: 44,000 t / a (6.1 t / h);

[0082] Fine ash after treatment: 142,000 tons / year (19.7 tons / hour);

[0083] Production of ultrafine calcium carbonate: 94,000 t / a (13.1 t / h);

[0084] Waste oil generation: 4500 t / a;

[0085] Ammonium chloride crystal production (dry basis): 38,600 t / a (5.4 t / h);

[0086] Sodium chloride contra-salts: 50,000 t / a (6.95 t / h);

[0087] High-temperature flue gas extracted from the SP furnace: 80000 Nm 3 / h;

[0088] The temperature of the flue gas extracted by the SP furnace is 200℃.

[0089] Flue gas volume of bubbling reaction tower: 60000 Nm3 / h;

[0090] Inlet flue gas temperature of the bubbling reaction tower: 120℃;

[0091] Bubble bed dryer inlet flue gas volume: 2400 Nm 3 / h;

[0092] Bubble bed dryer inlet flue gas temperature: 120℃;

[0093] Flue gas carbon dioxide replenishment capacity: 41,000 t / a (5.74 t / h);

[0094] Reflux ratio: 1:10

[0095] Wastewater discharge: 0 t / a;

[0096] The method of using a cement kiln co-processing waste liquid and municipal solid waste incineration fly ash system described in this invention includes S1: mixing municipal solid waste incineration fly ash with a certain amount of quicklime and then feeding it into a mixer (1) for mixing;

[0097] S2: The mixed material is fed into the crusher (2) to crush the large particles of fly ash;

[0098] S3: A certain proportion of waste hydrochloric acid (HCl effective concentration of 5-20%), waste emulsion (oil content of 2-10%), PAM / PAC and crushed fly ash mixture are sent into the reactor (3) and stirred for 30-60 min.

[0099] S4: The solid-liquid mixture is then fed into the first-stage solid-liquid separator (4). The wet solid material separated at the bottom of the first-stage solid-liquid separator (4) is organic aggregate, while the liquid at the top overflows into the oil-water separator (5).

[0100] S5: A high-temperature flue gas is drawn from the SP furnace outlet of the cement kiln clinker production line and the wet organic aggregate is dried in the dryer (401). The drying exhaust gas is then used in the downstream section, and the dried material enters the screening machine (402).

[0101] S6: The coarse material after screening is organic aggregate, while the fine material is mainly silicon-aluminum fine powder. The particle size of the coarse material is 0.5-15mm, and the particle size of the fine powder is 30-500μm. The fine material is sent to the cement kiln decomposition furnace via a pneumatic conveying pump (404).

[0102] S7: The high-calorific-value waste oil from the outlet of the oil-water separator (5) enters the oil storage tank (501) for storage. The waste oil is sent to the tertiary air duct for combustion by the transfer pump (502) to increase the furnace temperature of the decomposition furnace and reduce the coal consumption of the decomposition furnace.

[0103] S8: The clarified liquid produced by the oil-water separator (5) enters the first-stage clarified liquid storage tank (6) for storage. The clarified liquid contains a large amount of Ca. 2+ Cl - Na + K + SO4 2- Plasma;

[0104] S9: The ammonia solution and the clarified solution in S9 are mixed in a mixer (7). The mass concentration of the ammonia solution is about 5-28%, and the main ion in the mixer (7) is Ca. 2+ Cl - Na + K + SO4 2- NH4 + wait;

[0105] S10: After stabilization, the ammonia-containing clarified liquid is sent into the bubbling reactor (8), and at the same time, the CO2-containing dry flue gas from the cement kiln is introduced into the bubbling reactor (8). The CO2 in the flue gas reacts with the Ca in the clarified liquid. 2+The reaction produces CaCO3 precipitate, partially solidifying the CO2 in the flue gas. The resulting waste gas is then sent to the kiln tail chimney of the cement production line. To ensure an excess of CO2 during the reaction, the pH of the liquid needs to be controlled to be less than 7.

[0106] S11: After the reaction is complete, the solid-liquid mixture in the bubbling reactor (8) is discharged and sent to the second-stage solid-liquid separator (9) to separate ultrafine calcium carbonate powder. The clarified liquid after the reaction is sent to the second-stage clarified liquid storage tank (10) for storage. The main ion in the clarified liquid is Cl. - Na + K + SO4 2- NH4 + wait;

[0107] S12: The clarified liquid and the refluxed mother liquor from S12 are sent to the cooling system (11) for cooling. After freezing and salt separation (12), NH4Cl crystals can be obtained. The mother liquor is then sent to the mother liquor storage tank (13). The main ion in the mother liquor is Cl. - Na + K + SO4 2- In order to control the stability of the liquid level in the mother liquor storage tank (13), a portion of the mother liquor in the mother liquor storage tank (13) is returned to the cooling system (11), and the return ratio is controlled to be 1:5-1:15.

[0108] S13: Finally, the mother liquor in the mother liquor storage tank (13) is sent to the flash evaporator (14) to obtain sodium chloride mixed salt. The wastewater generated in the flash evaporator (14) is sent to the raw material station for batching. The mixed salt is dried by the bubble bed dryer (15) to obtain sodium chloride mixed salt crystals.

[0109] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any other way. Any person skilled in the art may make changes or modifications to the above-disclosed technical content to create equivalent embodiments for application in other fields. However, any simple modifications, equivalent changes, and modifications made to the above embodiments based on the technical essence of the present invention without departing from the scope of the present invention shall still fall within the protection scope of the present invention.

Claims

1. A system for co-processing waste liquid and fly ash from municipal solid waste incineration in a cement kiln, characterized in that, The system includes a solid material mixer (1), a crusher (2), a reactor (3), a first-stage solid-liquid separator (4), an oil-water separator (5), a first-stage clarified liquid storage tank (6), a liquid mixer (7), a bubble reactor (8), a second-stage solid-liquid separator (9), a second-stage clarified liquid storage tank (10), a cooling system (11), a freezing and salt separation system (12), a mother liquor storage tank (13), a flash concentration system (14), a bubble bed dryer (15), a dryer (401), a screening machine (402), a silo (403), a pneumatic conveying pump (404), an oil storage tank (501), a conveying pump (502), and a refrigeration unit (1101). A small amount of quicklime and municipal solid waste incineration fly ash, which are mixed evenly, are fed by a feeder. The solid material is mixed in a solid material mixer (1); the outlet of the solid material mixer (1) is connected to the inlet of the crusher (2), and the outlet of the crusher (2) is connected to the inlet of the reactor (3). After mixing, the solid material is crushed by the crusher (2) and then fed into the reactor (3); waste acid containing organic matter and waste emulsion are added to the reactor in proportion and mixed with the crushed solid material, while a certain amount of polyacrylamide is added at the same time; the outlet of the reactor (3) is connected to the inlet of the first-stage solid-liquid separator (4), the outlet of the first-stage solid-liquid separator (4) is connected to the inlet of the oil-water separator (5), the outlet of the oil-water separator (5) is connected to the inlet of the first-stage clarified liquid storage tank (6), and the outlet of the first-stage clarified liquid storage tank (6) is connected to the liquid mixer (7). The apparatus (4) separates the solid and liquid phases of the mixture from the reactor effluent. The liquid phase enters the oil-water separator (5) for oil-water separation. The resulting aqueous phase is sent to the first-stage clarified liquid storage tank (6) for temporary storage, and then sent to the liquid mixer (7). The outlet of the liquid mixer (7) is connected to the inlet of the bubbling reactor (8), and the air inlet of the bubbling reactor (8) is connected to the air outlet of the dryer (401). A certain concentration of ammonia solution is added to the liquid mixer (7) and mixed with the clarified liquid from the first-stage clarified liquid storage tank (6). Then, it is sent to the bubbling reactor (8) and reacted fully with the air outlet of the dryer (401). The outlet of the bubbling reactor (8) is connected to the inlet of the second-stage solid-liquid separator (9), and the outlet of the second-stage solid-liquid separator (9) is connected to the inlet of the second-stage solid-liquid separator (9). The inlet of the second-stage clarified liquid storage tank (10) is connected. After the solid phase and liquid phase of the mixed water effluent from the bubbling reactor (8) are separated by the second-stage solid-liquid separator (9), the liquid phase enters the second-stage clarified liquid storage tank (10) for temporary storage. The outlet of the second-stage clarified liquid storage tank (10) is connected to the inlet of the cooling system (11). The outlet of the cooling system (11) is connected to the inlet of the freezing salt separation system (12). The outlet of the freezing salt separation system (12) is connected to the inlet of the mother liquor storage tank (13). The clarified liquid in the second-stage clarified liquid storage tank (10) is sent to the cooling system (11) for cooling and then enters the freezing salt separation system (12) to separate ammonium chloride crystals. The remaining mother liquor enters the mother liquor storage tank (13) for temporary storage. A portion of the temporarily stored mother liquor is returned to the cooling system (11) and salted again according to the process.The outlet of the mother liquor storage tank (13) is connected to the inlet of the flash concentration system (14), and the outlet of the flash concentration system (14) is connected to the inlet of the bubbling bed dryer (15). The generated wastewater is sent to the raw material batching station of the cement production line. The air inlet of the bubbling bed dryer (15) is connected to the air outlet of the dryer (401). The mixed salt solution in the flash concentration system (14) enters the bubbling bed dryer (15) and is dried by the air outlet of the dryer (401) to obtain sodium chloride mixed salt.

2. The system for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln according to claim 1, characterized in that, The inlet of the first-stage solid-liquid separator (4) is connected to the outlet of the reactor (3). The first-stage solid-liquid separator (4) separates the solid and liquid phases of the mixture of water and liquid from the reactor. The solid material obtained is organic aggregate. The solid phase outlet of the first solid-liquid separator (4) is connected to the inlet of the dryer (401). The organic aggregate is fed into the dryer (401) to reduce the moisture content. The air inlet of the dryer (401) is connected to the air outlet of the SP boiler. The high-temperature flue gas at 200°C from the outlet of the SP boiler is used as a heat source. The outlet of the dryer (401) is connected to the inlet of the screening machine (402). The coarse and fine materials containing organic aggregate are screened. The coarse material separated by the screening machine (402) is used as organic aggregate and can be used to make ceramsite or building materials. The undersize outlet of the screening machine (402) is connected to the inlet of the silo (403), and the outlet of the silo (403) is connected to the cement kiln decomposition furnace. After the undersize fine material enters the silo (403) for temporary storage, it is sent into the cement kiln decomposition furnace through the pneumatic conveying pump (404).

3. The system for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln according to claim 1, characterized in that, The inlet of the oil-water separator (5) is connected to the liquid phase outlet of the first-stage solid-liquid separator (4). The oil-water separator (5) separates the oil and water in the mixture of solid and liquid. The outlet of the oil-water separator (5) is connected to the inlet of the oil storage tank (501). The outlet of the oil storage tank (501) is connected to the tertiary air duct of the cement kiln. The separated oil phase material is sent into the tertiary air duct of the cement kiln through the transfer pump (502) to provide heat for the cement kiln.

4. The system for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln according to claim 1, characterized in that, The inlet of the bubbling reactor (8) is connected to the outlet of the liquid mixer (7) to carry out the bubbling reaction of the water effluent from the liquid mixer; the air inlet of the bubbling reactor (8) is connected to the air outlet of the dryer (401). The air effluent from the dryer (401) is the gas after drying the 200°C high-temperature flue gas containing organic aggregate from the SP furnace outlet. Its carbon dioxide content is 15-20% of that of dry air. When it enters the bubbling reactor (8), the temperature drops to 120°C. After the reaction, the gas is discharged from the kiln tail chimney; the second-stage solid-liquid separator (9) separates the solid phase and liquid phase of the water mixture from the bubbling reactor (8). The solid phase after separation is ultrafine calcium carbonate powder.

5. A system for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln according to claim 1, characterized in that, The cooling system (11) cools down by heat exchange through the refrigerator (1101). Part of the temporary mother liquor in the mother liquor storage tank (13) is returned to the cooling system (11) at a return ratio of 1:

10. After mixing with the clarified liquid in the second-stage clarified liquid storage tank (10), the liquid is cooled down and then enters the freezing and salt separation system (12) to separate the ammonium chloride crystals by utilizing the difference in solubility of different compounds with temperature.

6. The system for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln according to claim 1, characterized in that, The air inlet of the bubbling bed dryer (15) is connected to the air outlet of the dryer (401). The residual heat in the air outlet of the dryer (401) is used to dry the mixed salt solution in the flash evaporator (14). Sodium chloride mixed salt can be obtained after drying. The air outlet of the dryer (401) is the gas after drying the organic aggregate contained in the 200°C high-temperature flue gas from the SP furnace outlet. When it enters the bubbling bed dryer (15), the temperature drops to 120°C. After the reaction, the gas is discharged from the kiln tail chimney.

7. The system for co-processing waste liquid and municipal solid waste incineration fly ash in a cement kiln as described in claim 1, characterized in that: S1: After mixing the fly ash from municipal solid waste incineration with a certain amount of quicklime, send it into the mixer (1) for mixing; S2: The mixed material is fed into the crusher (2) to crush the large particles of agglomerated fly ash; S3: A certain proportion of waste hydrochloric acid with an effective concentration of 5-20%, waste emulsion with an oil content of 2-10%, PAM / PAC and crushed fly ash mixture are fed into the reactor (3), and the stirring reaction time is 30-60 min. S4: The solid-liquid mixture is then fed into the first-stage solid-liquid separator (4). The wet solid material separated at the bottom of the first-stage solid-liquid separator (4) is organic aggregate, while the liquid at the top overflows into the oil-water separator (5). S5: A high-temperature flue gas is drawn from the SP furnace outlet of the cement kiln clinker production line and the wet organic aggregate is dried in the dryer (401). The drying exhaust gas is then used in the downstream section, and the dried material enters the screening machine (402). S6: The coarse material after screening is organic aggregate, while the fine material is mainly silicon-aluminum fine powder. The particle size of the coarse material is 0.5-15mm, and the particle size of the fine powder is 30-500μm. The fine material is sent to the cement kiln decomposition furnace via a pneumatic conveying pump (404). S7: The high-calorific-value waste oil from the outlet of the oil-water separator (5) enters the oil storage tank (501) for storage. The waste oil is sent to the tertiary air duct for combustion by the transfer pump (502) to increase the furnace temperature of the decomposition furnace and reduce the coal consumption of the decomposition furnace. S8: The clarified liquid produced by the oil-water separator (5) enters the first-stage clarified liquid storage tank (6) for storage. The clarified liquid contains a large amount of Ca. 2+ Cl - Na + K + SO4 2- Plasma; S9: The ammonia solution and the clarified solution in S9 are mixed in a mixer (7). The mass concentration of the ammonia solution is 5-28%, and the main ion in the mixer (7) is Ca. 2+ Cl - Na + K + SO4 2- NH4 + wait; S10: After stabilization, the ammonia-containing clarified liquid is sent into the bubbling reactor (8), and at the same time, the CO2-containing dry flue gas from the cement kiln is introduced into the bubbling reactor (8). The CO2 in the flue gas reacts with the Ca in the clarified liquid. 2+ The reaction produces CaCO3 precipitate, and CO2 in the flue gas is partially solidified. The waste gas after the reaction is sent to the kiln tail chimney of the cement production line. To ensure that there is excess CO2 during the reaction, the pH value of the liquid needs to be controlled to be less than 7. S11: After the reaction is complete, the solid-liquid mixture in the bubbling reactor (8) is discharged and sent to the second-stage solid-liquid separator (9) to separate ultrafine calcium carbonate powder. The clarified liquid after the reaction is sent to the second-stage clarified liquid storage tank (10) for storage. The main ion in the clarified liquid is Cl. - Na + K + SO4 2- NH4 + wait; S12: The clarified liquid and the refluxed mother liquor from S12 are sent to the cooling system (11) for cooling. NH4Cl crystals are obtained through the freezing and salt separation system (12). The mother liquor is then sent to the mother liquor storage tank (13). The main ion in the mother liquor is Cl. - Na + K + SO4 2- In order to control the stability of the liquid level in the mother liquor storage tank (13), a portion of the mother liquor in the mother liquor storage tank (13) is returned to the cooling system (11), and the return ratio is controlled to be 1:5-1:15; S13: Finally, the mother liquor in the mother liquor storage tank (13) is sent to the flash concentration system (14) to obtain sodium chloride mixed salt. The wastewater generated in the flash concentration system (14) is sent to the raw material station for batching. The mixed salt is dried by the bubble bed dryer (15) to obtain sodium chloride mixed salt crystals.

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