Salt-containing waste liquid incineration treatment apparatus and salt-containing waste liquid incineration treatment method

Abstract

The application discloses a salt-containing waste liquid incineration treatment device and a salt-containing waste liquid incineration treatment method, and belongs to the technical field of waste liquid incineration. The salt-containing waste liquid incineration treatment device comprises an incineration system, a waste heat utilization system, a residue discharging system and a flue gas purification system. The incineration system comprises a first combustor and an incineration furnace, and the incineration furnace comprises a first cross incineration boiler, a second cross incineration boiler and a third cross incineration boiler which are sequentially communicated. The waste heat utilization system comprises a plurality of heat exchange modules and a steam-water pipeline, and the heat exchange modules are arranged downstream of the third cross incineration boiler. The residue discharging system is used for collecting salt residues in the first cross incineration boiler and the third cross incineration boiler. The flue gas purification system comprises a dust remover and a denitration device. The salt-containing waste liquid incineration treatment device of the application is used for treating salt-containing waste liquid, harmless treatment of which is carried out under high-temperature conditions, and salt residues generated in the incineration process can be discharged, so as to reduce the risk of blockage of the flue caused by the adhesion of salt residues to the flue wall surface and the surface of the heat exchange module.

Description

Technical Field

[0001] This application relates to the field of waste liquid incineration technology, and in particular to a saline waste liquid incineration treatment device and a saline waste liquid incineration treatment method. Background Technology

[0002] With the rapid development of industrial technology, the discharge of saline wastewater generated during the production processes of industries such as chemicals and pharmaceuticals has been increasing year by year. This type of wastewater has a complex composition, containing not only a large amount of organic matter that is difficult to biodegrade, but also a variety of salts. If discharged directly, it will cause serious pollution to the soil, water bodies, and atmospheric environment, threatening the ecological balance and human health.

[0003] In existing technologies, the main methods for treating saline wastewater include biodegradation, deep underground high-pressure storage, and thermal oxidation incineration. Biodegradation is limited by salt concentration and cannot effectively treat high-concentration saline organic wastewater; deep underground high-pressure storage is prohibited by national environmental protection laws due to potential environmental risks; while thermal oxidation incineration, with its thorough treatment effect, has become the mainstream technology for treating saline wastewater. The core principle of this method is to oxidize and decompose the organic matter in the saline wastewater into harmless small molecules such as carbon dioxide, water, and nitrogen under high-temperature conditions, which are then discharged after waste heat recovery. However, the salt residue produced during incineration easily adheres to the flue walls and heat exchange module surfaces, easily causing flue blockage and affecting the long-term stable operation of the equipment. Summary of the Invention

[0004] This application provides a saline waste liquid incineration treatment device and a saline waste liquid incineration treatment method. The saline waste liquid incineration treatment device is used to treat saline waste liquid, render it harmless under high temperature conditions, and can discharge the salt residue generated during the incineration process to reduce the salt residue adhering to the flue wall and the surface of the heat exchange module, thereby reducing the risk of flue blockage.

[0005] To achieve the above objectives, according to a first aspect of this application, a saline waste liquid incineration treatment apparatus is provided, comprising: An incineration system, the incineration system including a first burner and an incinerator, the incinerator including a first cross-section incinerator boiler, a second cross-section incinerator boiler and a third cross-section incinerator boiler connected in sequence, the first burner being disposed on top of the first cross-section incinerator boiler; The waste heat utilization system includes multiple heat exchange modules and steam-water pipelines. The heat exchange modules are located downstream of the third-span incineration boiler, and at least some of the heat exchange modules are connected through the steam-water pipelines. The slag removal system is connected to the first cross-type incinerator and the third cross-type incinerator respectively, and is used to collect liquid salt slag in the first cross-type incinerator and solid salt slag in the third cross-type incinerator. A flue gas purification system, comprising a dust collector and a denitrification device, wherein the dust collector is located downstream of the incinerator and the denitrification device is located downstream of the dust collector.

[0006] Optionally, the first burner is provided with a first fuel inlet, a first waste inlet, and a first air inlet, wherein the first waste inlet includes a first waste liquid inlet; The first cross-type incineration boiler is provided with a second waste inlet and a second air inlet. The second waste inlet includes a second waste liquid inlet. The second air inlet is located on the side wall of the first cross-type incineration boiler, and the distance between the second air inlet and the top of the first cross-type incineration boiler in the height direction is 1.5m to 4.0m. The incineration system also includes a first blower, which supplies air to the first burner through the first air interface and to the first cross-incineration boiler through the second air interface. At least one heat exchange module is provided between the first air interface and the first fan.

[0007] Optionally, the plurality of heat exchange modules include a high-temperature superheater, a low-temperature superheater, an air preheater, a high-temperature economizer, and a low-temperature economizer. The high-temperature superheater, the low-temperature superheater, the air preheater, and the high-temperature economizer are sequentially arranged downstream of the third-span incinerator in the flue gas flow path, and the low-temperature economizer is arranged downstream of the denitrification device. The waste heat utilization system also includes a steam drum. The low-temperature economizer, the steam drum, the high-temperature economizer, the low-temperature superheater, and the high-temperature superheater are connected in sequence through the steam-water pipeline. The low-temperature economizer is connected to the water-side inlet of the waste heat utilization system, and boiler feedwater flows into the low-temperature economizer. The high-temperature superheater is connected to the steam-side outlet of the waste heat utilization system, and high-temperature steam flows out of the high-temperature superheater. The heat exchange modules further include water-cooled walls, and at least one of the first, second, and third cross-type incinerators is provided with the water-cooled wall. The steam drum is also connected to the water-cooled wall via downcomers and upcomers.

[0008] Optionally, the incinerator further includes a fourth and a fifth incinerator connected in sequence. The fourth incinerator is connected to the third incinerator. The high-temperature superheater and the low-temperature superheater are located in the fourth incinerator, and the air preheater and the high-temperature economizer are located in the fifth incinerator.

[0009] Optionally, the waste heat recovery system further includes a water spray desuperheater, which is disposed between the low-temperature superheater and the high-temperature superheater, and is connected to the water-side inlet of the waste heat recovery system; and / or, The waste heat utilization system also includes a soot blowing device for removing salt residue from the heat exchange module.

[0010] Optionally, the ash removal system includes a first ash removal unit, a second ash removal unit, a device ash removal unit, and a collection unit. The first ash removal unit is located at the bottom of the first-span incinerator, the second ash removal unit is located at the bottom of the third-span incinerator, the device ash removal unit is located at the bottom of the high-temperature economizer and / or the dust collector, and the collection unit is used to collect the salt slag and fly ash discharged by the first ash removal unit, the second ash removal unit, and the device ash removal unit.

[0011] Optionally, the first slag discharge unit includes a first biaxial cooler and a first discharge valve, and a liquid molten slag pool is provided at the bottom of the first cross-burning boiler, and the first biaxial cooler is connected to the liquid molten slag pool; The second slag discharge unit includes a second biaxial cooler and a second discharge valve, wherein the second biaxial cooler is connected to the third cross-burning boiler; The ash discharge unit of the device includes a third discharge valve and a fourth discharge valve.

[0012] Optionally, the first ash removal unit further includes a second burner and a second fan. The second burner is disposed on the bottom side wall of the first cross-burning boiler. The second burner is provided with a second fuel inlet and a third air inlet. The second fan supplies air to the second burner through the third air inlet; and / or, The first slag discharge unit also includes a drum slag cooler, which is located between the first twin-shaft cooler and the first discharge valve.

[0013] Optionally, the first ash removal unit further includes a third fan, the inlet end of which is connected to the first twin-shaft cooler, and the outlet end of which is connected to the bottom of at least one of the third cross-type incinerator, the fourth cross-type incinerator, and the fifth cross-type incinerator. The inlet of the third fan is also connected to the outside atmosphere to draw in air and reduce the temperature of the flue gas entering the third fan.

[0014] Optionally, the number of collection units is multiple, and the multiple collection units are respectively arranged corresponding to the first discharge valve, the second discharge valve, the third discharge valve, and the fourth discharge valve; or, The slag discharge system further includes a conveying device, which is disposed below at least one of the first discharge valve, the second discharge valve, the third discharge valve, and the fourth discharge valve. The conveying device is used to convey the salt slag discharged from the first discharge valve, the second discharge valve, the third discharge valve, and the fourth discharge valve to the collection unit.

[0015] Optionally, the denitrification device includes a denitrification agent delivery device, a third burner, a denitrification reactor, and a fourth fan. The third burner is located downstream of the dust collector, and the denitrification agent delivery device is arranged on the downstream flue of the third burner. The third burner is connected to the denitrification reactor. The third burner is provided with a third fuel interface and a fourth air interface, and the fourth fan supplies air to the third burner through the fourth air interface.

[0016] Optionally, the incineration system further includes an induced draft fan and a chimney, wherein the induced draft fan is located downstream of the denitrification unit and the chimney is located downstream of the induced draft fan.

[0017] According to a second aspect of this application, a method for incinerating saline waste liquid is provided, using a saline waste liquid incineration treatment device as described in any one of the above, the saline waste liquid incineration treatment method comprising: Salty waste and fuel are fed into the incineration system for incineration; The waste heat recovery system recovers the heat from the high-temperature flue gas and generates high-temperature steam. The slag and fly ash in the flue gas are collected through the slag removal system. The flue gas is treated by dust removal and denitrification through the flue gas purification system.

[0018] Optionally, the step of feeding the saline waste and fuel into the incineration system for incineration includes: The flue gas temperature at the outlet of the first cross-burning boiler is controlled by controlling the fuel flow rate. The oxygen content in the flue gas in the first burner and the first cross-burner boiler is controlled to be greater than or equal to 6% by controlling the air flow.

[0019] In the saline waste liquid incineration treatment equipment and method of this application embodiment, the saline waste liquid incineration treatment equipment is used to treat saline waste liquid and render it harmless under high temperature conditions. The saline waste liquid incineration treatment equipment is equipped with a waste heat utilization system and a slag discharge system. The heat exchange module of the waste heat utilization system is located downstream of the third span incineration boiler. The slag discharge system is connected to the first span incineration boiler and the third span incineration boiler respectively, and is used to collect the salt slag in the first span incineration boiler and the third span incineration boiler. This can discharge the salt slag generated during the incineration process, thereby reducing the salt slag adhering to the flue wall and the surface of the heat exchange module, thereby reducing the risk of flue blockage, ensuring the long-term stable operation of the saline waste liquid incineration treatment equipment, and improving the utilization efficiency and service life of the saline waste liquid incineration treatment equipment. Meanwhile, by setting up a dust collector and a denitrification device, with the dust collector located downstream of the incinerator and the denitrification device located downstream of the dust collector, the flue gas is first dusted and then denitrified. This can prevent the denitrification device from being blocked, which not only improves the denitrification efficiency but also extends the service life of the denitrification device.

[0020] Other features and advantages of this application will be described in detail in the following detailed description section. Attached Figure Description

[0021] To more clearly illustrate the technical solutions in the embodiments of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0022] To gain a more complete understanding of this application and its beneficial effects, the following description will be provided in conjunction with the accompanying drawings, wherein the same reference numerals in the following description denote the same parts.

[0023] Figure 1 This is a schematic diagram of the structure of the saline waste liquid incineration treatment equipment provided in an exemplary embodiment of this disclosure; Figure 2 yes Figure 1 A magnified schematic diagram of the partial structure at point A in the middle; Figure 3 This is a schematic diagram of the waste heat utilization system provided in an exemplary embodiment of this disclosure; Figure 4 This is a schematic structural diagram of the first burner and the first cross-burning boiler provided in an exemplary embodiment of this disclosure from one perspective; Figure 5 This is a structural schematic diagram of the first burner and the first cross-burning boiler provided in an exemplary embodiment of this disclosure from another perspective.

[0024] Explanation of reference numerals in the attached figures: 1. Incineration system; 11. First burner; 111. First fuel inlet; 112. First waste inlet; 1121. First waste liquid inlet; 1122. First waste gas inlet; 113. First air inlet; 12. Incinerator; 121. First span incinerator; 1211. Second waste inlet; 12111. Second waste liquid inlet; 12112. Second waste gas inlet; 1212. Second air inlet; 1213. Molten slag pool; 1214. First observation port; 122. Second span incinerator; 123. Third span incinerator; 124. Fourth span incinerator; 125. Fifth Span Incineration Boiler; 13. First Blower; 131. First Gas Pipe; 132. Second Gas Pipe; 14. Induced Draft Fan; 15. Chimney; 2. Waste Heat Utilization System; 21. Heat Exchange Module; 211. High-Temperature Superheater; 212. Low-Temperature Superheater; 213. Air Preheater; 214. High-Temperature Economizer; 215. Low-Temperature Economizer; 216. Water-Cooled Wall; 22. Steam-Water Pipeline; 23. Steam Drum; 231. Gas-Liquid Separator; 232. First Section; 233. Second Section; 234. Downcomer; 235. Riser; 24. Water Spray Desuperheater; 25. Soot Blowing Device; 3. Ash Removal System; 31 311. First slag discharge unit; 312. First twin-shaft cooler; 313. First unloading valve; 314. Drum slag cooler; 315. Second burner; 316. Second fuel inlet; 317. Third air inlet; 318. Second fan; 319. Third fan; 310. First air duct; 311. Second air duct; 311. Third air duct; 311. Second slag discharge unit; 321. Second twin-shaft cooler; 322. Second unloading valve; 331. Ash discharge unit; 332. Third unloading valve; 333. Fourth unloading valve; 34. Collection unit; 35. Conveying device; 4. Flue gas purification System; 41. Dust collector; 411. Air self-suction port; 42. Denitrification device; 421. Denitrification agent delivery device; 422. Third burner; 4221. Third fuel interface; 4222. Fourth air interface; 4223. Downstream flue; 423. Denitrification reactor; 424. Fourth fan; 5. Fuel system; 51. First fuel pipe; 52. Second fuel pipe; 53. Third fuel pipe; 6. Waste conveying system; 61. Waste liquid conveying unit; 611. First waste liquid pipe; 612. Second waste liquid pipe; 62. Waste gas conveying unit; 621. First waste gas pipe; 622. Second waste gas pipe. Detailed Implementation

[0025] The technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application. In addition, it should be understood that the specific embodiments described herein are only for illustration and explanation of this application and are not intended to limit this application. In this application, unless otherwise stated, directional terms such as "up," "down," "left," and "right" generally refer to up, down, left, and right in the actual use or working state of the device, specifically the drawing directions in the accompanying drawings.

[0026] In this application, unless otherwise expressly specified and limited, the terms "connected," "linked," "stacked," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two elements or the interaction between two elements. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific circumstances.

[0027] This application provides a saline wastewater incineration treatment device and a saline wastewater incineration treatment method, which are described in detail below. It should be noted that the order of description of the following embodiments is not intended to limit the preferred order of the embodiments of this application. Furthermore, in the following embodiments, the descriptions of each embodiment have their own emphasis; parts not described in detail in a certain embodiment can be referred to in the relevant descriptions of other embodiments.

[0028] According to the first aspect of this application, referring to Figure 1 One embodiment of this application provides a saline waste liquid incineration treatment device, including an incineration system 1, a waste heat utilization system 2, a slag discharge system 3, and a flue gas purification system 4. The systems work together to complete the entire process of saline waste liquid incineration, waste heat recovery, salt slag collection, and flue gas purification.

[0029] Specifically, refer to Figure 1 and Figure 2The incineration system 1 may include a first burner 11 and an incinerator 12. The incinerator 12 may employ a multi-span large-cavity structure and may include a first-span incinerator 121, a second-span incinerator 122, and a third-span incinerator 123 connected sequentially, providing sufficient residence time for complex saline wastewater, ensuring complete decomposition of organic matter, and improving treatment efficiency and operational reliability. The first-span incinerator 121, the second-span incinerator 122, and the third-span incinerator 123 may all employ large-cavity water-cooled walls 216 for heat exchange. To protect the water-cooled walls 216 from corrosion by molten slag, a lining of a certain thickness (not shown) is provided on the water-cooled walls 216 of the first-span incinerator 121, with a thickness ranging from 30 mm to 100 mm. The first burner 11 is located at the top of the first-span incinerator 121. The first burner 11 provides a stable combustion flame and has a continuous illumination function, which can improve the combustion safety and operational reliability of the incineration system 1.

[0030] Reference Figure 1 and Figure 3 The waste heat recovery system 2 is used to recover heat from high-temperature flue gas and generate steam. The waste heat recovery system 2 may include multiple heat exchange modules 21 and steam-water pipelines 22. The heat exchange modules 21 may be located downstream of the third-span incinerator 123, and each heat exchange module 21 may be arranged sequentially along the flue gas flow direction. At least some of the heat exchange modules 21 can be connected via the steam-water pipelines 22 to form a complete steam-water circulation system. As an example, boiler feedwater is injected into the steam-water pipelines 22. When the boiler feedwater passes through the heat exchange modules 21, it can exchange heat with the flue gas through the heat exchange modules 21, thereby generating high-temperature steam.

[0031] Reference Figure 1 The ash removal system 3 is used to collect and discharge the salt slag generated during the incineration process. The ash removal system 3 can be connected to both the first incinerator 121 and the third incinerator 123, and is used to collect the liquid salt slag in the first incinerator 121 and the solid salt slag in the third incinerator 123. For example, the temperature of the first incinerator 121 is higher than that of the third incinerator 123. Liquid molten salt can form in the first incinerator 121, while solid molten salt can form in the third incinerator 123. Discharging the liquid molten salt through the ash removal system 3 can reduce the corrosion and erosion of the incinerator 12 by the liquid molten salt.

[0032] Reference Figure 1 The flue gas purification system 4 is used to remove particulate matter and NO from the flue gas. xTo ensure that pollutants such as particulate matter are removed from the flue gas and that emissions meet standards, the flue gas purification system 4 may include a dust collector 41 and a denitrification device 42. The dust collector 41 may be a baghouse dust collector 41, which can be located downstream of the incinerator 12. The denitrification device 42 can be located downstream of the dust collector 41. The dust collector 41 filters particulate matter from the flue gas, preventing solid particles from clogging the denitrification device 42. This not only improves the denitrification efficiency of the denitrification device 42 but also extends its service life, thereby reducing the operating and maintenance costs of the equipment.

[0033] Reference Figure 1 An air self-suction port 411 can be provided upstream of the dust collector 41. This port can regulate the temperature of the flue gas entering the dust collector 41, for example, reducing it to below 250°C to prevent damage to the dust collector 41 due to excessively high flue gas temperature, thereby extending its service life. The air self-suction port 411 can be located in the flue between the dust collector 41 and the incinerator 12. In this embodiment, the air self-suction port 411 can be located in the flue between the dust collector 41 and the fifth incinerator boiler 125.

[0034] In some embodiments, refer to Figure 1 The incineration system 1 may also include an induced draft fan 14 and a chimney 15. The induced draft fan 14 may be located downstream of the denitrification device 42, and the chimney 15 may be located downstream of the induced draft fan 14. In this embodiment, the low-temperature economizer 215 is located downstream of the denitrification device 42, and the induced draft fan 14 may be located downstream of the low-temperature economizer 215. The incineration system 1 can operate under negative pressure, with a negative pressure setpoint, for example, from -100 PaG to -500 PaG. The induced draft fan 14 provides suction to ensure that the flue gas flows along a preset path. As an example, the flue gas flows sequentially through the first burner 11, the incinerator 12, the dust collector 41, the denitrification device 42, the induced draft fan 14, and the chimney 15. During the flue gas flow, it may also flow through heat exchange modules 21 located at different positions. To ensure the connection between the various equipment modules, a number of expansion joints (not shown) may be arranged on the flue. The expansion joints are used to absorb the thermal expansion of the various equipment modules and the flue due to high temperature.

[0035] In this application, a saline waste liquid incineration treatment device is used to treat saline waste liquid and render it harmless under high temperature conditions. By setting up a waste heat utilization system 2 and a slag discharge system 3, the heat exchange module 21 of the waste heat utilization system 2 is set downstream of the third-span incineration boiler 123. The slag discharge system 3 is connected to the first-span incineration boiler 121 and the third-span incineration boiler 123 respectively, and is used to collect the salt slag in the first-span incineration boiler 121 and the third-span incineration boiler 123. This can discharge the salt slag generated during the incineration process, thereby reducing the salt slag adhering to the flue wall and the surface of the heat exchange module 21, thus reducing the risk of flue blockage, ensuring the long-term stable operation of the saline waste liquid incineration treatment device, and improving the efficiency and lifespan of the saline waste liquid incineration treatment device. Meanwhile, by setting up a dust collector 41 and a denitrification device 42, with the dust collector 41 located downstream of the incinerator 12 and the denitrification device 42 located downstream of the dust collector 41, the flue gas is first dusted and then denitrified. This can prevent the denitrification device 42 from being blocked, which not only improves the denitrification efficiency but also extends the service life of the denitrification device 42.

[0036] In some embodiments, refer to Figure 1 Fuel, such as natural gas, is supplied to the incineration system 1 via the fuel system 5. Waste, including waste liquid and waste gas, is supplied to the incineration system 1 via the waste conveying system 6. The waste conveying system 6 may include a waste liquid conveying unit 61 and a waste gas conveying unit 62. The waste liquid may include high-calorific-value waste liquid and low-calorific-value waste liquid, and the waste gas may include high-calorific-value waste gas and low-calorific-value waste gas. The waste liquid conveying unit 61 may include a first waste liquid pipe 611 and a second waste liquid pipe 612, and the waste gas conveying unit 62 may include a first waste gas pipe 621 and a second waste gas pipe 622.

[0037] Reference Figure 1 and Figure 2The first burner 11 may be equipped with a first fuel inlet 111, a first waste inlet 112, and a first air inlet 113. The fuel system 5 may include a first fuel pipe 51, and the first fuel inlet 111 may be connected to the first fuel pipe 51, through which fuel can be injected into the first burner 11. The first waste inlet 112 may include a first waste liquid inlet 1121, which is connected to a first waste liquid pipe 611, through which high-calorific-value waste liquid can be injected into the first burner 11. The temperature within the combustion system can be controlled by controlling the flow rate of fuel injected into the first burner 11. As an example, the temperature in at least a portion of the first incinerator 121 is controlled to be greater than or equal to 1100°C to ensure that the saline waste can be fully combusted. The area within the first incinerator 121 with a temperature greater than or equal to 1100°C is, for example, the area of ​​the first incinerator 121 near the first burner 11. Simultaneously, the residence time of the flue gas in the temperature range greater than or equal to 1100°C can be controlled to be greater than 2.0 s to further ensure that the saline waste can be fully combusted. In some embodiments, the flow rate of the flue gas can also be adjusted by controlling the power of the induced draft fan 14 to ensure that the residence time of the flue gas in the temperature range greater than or equal to 1100°C is greater than 2.0 s, further ensuring that the saline waste can be fully combusted. In some embodiments, the first waste inlet 112 may also include a first exhaust gas inlet 1122, which is connected to a first exhaust gas pipe 621, through which high-calorific-value exhaust gas is injected into the first burner 11.

[0038] The first burner 11 may also be equipped with multiple spray guns (not shown), through which fuel, high-calorific-value waste liquid, and high-calorific-value exhaust gas can be sprayed into the first burner 11, thereby improving the uniformity of combustion. The spray guns used for spraying high-calorific-value waste liquid and exhaust gas can be evenly distributed on the inner wall of the first burner 11, further improving the uniformity of combustion. In some embodiments, the first burner 11 may also be equipped with 1-2 observation holes (not shown) and 1-4 flame detectors (not shown) for real-time monitoring of the combustion status.

[0039] Reference Figure 1 and Figure 2The first incinerator 121 may be provided with a second waste inlet 1211 and a second air inlet 1212. The second waste inlet 1211 may include a second waste liquid inlet 12111, which is connected to a second waste liquid pipe 612, through which low-calorific-value waste liquid is injected into the first incinerator 121. The second air inlet 1212 is disposed on the side wall of the first incinerator 121, and the distance between it and the top of the first incinerator 121 in the height direction is 1.5m to 4.0m. In some embodiments, the second waste inlet 1211 may further include a second waste gas inlet 12112, which is connected to a second waste gas pipe 622, through which low-calorific-value waste gas is injected into the first incinerator 121.

[0040] As an example, refer to Figure 4 and Figure 5 There are nine second air inlets 1212, with three on each of the front, left, and right walls of the first incinerator 121. The distance between each second air inlet 1212 and the top of the first incinerator 121 is 2.0m. There are six second waste liquid inlets 12111, with three on each of the left and right walls of the first incinerator 121. There is one second waste gas inlet 12112, located near the center of the front wall of the first incinerator 121. There are two first observation holes 1214, located at both ends of the front wall of the first incinerator 121. The second waste liquid inlets 12111, the second waste gas inlets 12112, and the first observation holes 1214 are respectively located within the second air inlets 1212.

[0041] As an example, the parameters of the high-calorific-value waste liquid are: flow rate 2000 kg / h, calorific value 39070 kJ / kg, and it is connected to the first burner 11 through the first waste liquid interface 1121.

[0042] The parameters of the low-calorific-value waste liquid are: flow rate 6000~10000 kg / h, calorific value -1670 kJ / kg, and it is connected to the first incineration boiler 121 through the second waste liquid interface 12111.

[0043] The parameters for the high-calorific-value exhaust gas are: flow rate 900 Nm³. 3 / h, calorific value 88745kJ / Nm 3 It is connected to the first burner 11 through the first exhaust gas interface 1122.

[0044] The parameters for low-calorific-value exhaust gas are: flow rate 0~1000 Nm³. 3 / h, with a calorific value close to zero, is connected to the first incineration boiler 121 through the second exhaust gas interface 12112.

[0045] Reference Figure 1 and Figure 2 The incineration system 1 may further include a first blower 13, which can be connected to a first air inlet 113 and a second air inlet 1212 via a first air pipe 131 and a second air pipe 132, respectively. The first blower 13 can pressurize the air and can supply air to the first burner 11 via the first air inlet 113 and to the first cross-burner boiler 121 via the second air inlet 121, thereby increasing the oxygen content in the first burner 11 and the first cross-burner boiler 121. For example, the oxygen content in the flue gas in the first burner 11 is greater than or equal to 6%, and the oxygen content in the flue gas in the first cross-burner boiler 121 is greater than or equal to 6%, thereby improving combustion efficiency.

[0046] Reference Figure 1 At least one heat exchange module 21 can be provided between the first air inlet 113 and the first fan 13. This heat exchange module 21 can be connected in series with the first air pipe 131. The first fan 13 drives air into one of the heat exchange modules 21, where it is heated, and then sent to the first burner 11 through the first air inlet 113 to preheat the air entering the first burner 11. When the calorific value of the waste is low and a large amount of additional fuel gas is required to maintain the combustion temperature in the first burner 11, preheating the air entering the first burner 11 can reduce fuel consumption and thus reduce costs. In some embodiments, when the calorific value of the waste is high and no large amount of additional fuel gas is required to maintain the combustion temperature in the first burner 11, preheating the air entering the first burner 11 may not be necessary.

[0047] In some embodiments, regulating valves (not shown) can be provided on both the first air pipe 131 and the second air pipe 132 for flow distribution control. The supplementary combustion air from the first air pipe 131 and the second air pipe 132 can achieve staged air supply to improve the combustion effect.

[0048] In some embodiments, refer to Figure 1 and Figure 3The multiple heat exchange modules 21 may include a high-temperature superheater 211, a low-temperature superheater 212, an air preheater 213, a high-temperature economizer 214, and a low-temperature economizer 215. The high-temperature superheater 211, low-temperature superheater 212, air preheater 213, and high-temperature economizer 214 are sequentially arranged downstream of the third-span incinerator 123 in the flue gas flow path, while the low-temperature economizer 215 is located downstream of the denitrification device 42. The air preheater 213 can be connected in series with the first gas pipe 131. The first fan 13 can drive the air in the first gas pipe 131 through the air preheater 213, which heats the air to preheat the air entering the first burner 11. All heat exchange modules 21 can be bare tube heat exchangers or plate heat exchangers, which reduces the adhesion of salt residue to the surface of the heat exchange module 21. As an example, the air preheater 213 can be a plate heat exchanger, and the high-temperature superheater 211, the low-temperature superheater 212, the high-temperature economizer 214 and the low-temperature economizer 215 can all be bare tube heat exchangers.

[0049] Reference Figure 3 The waste heat recovery system 2 may further include a steam drum 23, and at least one of the first-span incinerator 121, the second-span incinerator 122, and the third-span incinerator 123 is provided with a water-cooled wall 216. In this embodiment, the first-span incinerator 121, the second-span incinerator 122, and the third-span incinerator 123 are all provided with water-cooled walls 216. The low-temperature economizer 215, the steam drum 23, the high-temperature economizer 214, the low-temperature superheater 212, and the high-temperature superheater 211 are connected sequentially via steam-water pipelines 22. The low-temperature economizer 215 is connected to the water-side inlet of the waste heat recovery system 2, and boiler feedwater flows into the low-temperature economizer 215. The boiler feedwater is, for example, liquid water. The high-temperature superheater 211 is connected to the steam-side outlet of the waste heat recovery system 2, and high-temperature steam flows out of the high-temperature superheater 211. As an example, boiler feedwater first enters the low-temperature economizer 215 through steam-water pipeline 22, and then sequentially enters the steam drum 23, high-temperature economizer 214, low-temperature superheater 212 and high-temperature superheater 211 through steam-water pipeline 22. The high-temperature steam generated is then incorporated into the steam network.

[0050] The heat exchange modules 21 may further include water-cooled walls 216. At least one of the first-span incinerator 121, the second-span incinerator 122, and the third-span incinerator 123 is provided with a water-cooled wall 216. The steam drum 23 is also connected to the water-cooled wall 216 via a downcomer 234 and a riser 235, respectively. In this embodiment, the first-span incinerator 121, the second-span incinerator 122, and the third-span incinerator 123 are all provided with water-cooled walls 216.

[0051] As an example, refer to Figure 3A gas-liquid separator 231 is installed inside the steam drum 23, which divides the steam drum 23 into a first part 232 and a second part 233. A low-temperature economizer 215 is connected to the first part 232 via a steam-water pipeline 22, and a high-temperature economizer 214 is connected to the second part 233 via the same pipeline. The first part 232 is connected to the inlet end of the water-cooled wall 216 via a downcomer 234, and the outlet end of the water-cooled wall 216 is connected to the first part 232 via a riser 235. Boiler feedwater exchanges heat with the flue gas in the incinerator 12 through the water-cooled wall 216 to form high-temperature steam or a steam-water mixture. The high-temperature steam or mixture enters the first part 232, then passes through the gas-liquid separator 231. The high-temperature steam can then enter the second part 233 and, via the steam-water pipeline 22, enter the high-temperature economizer 214.

[0052] In some embodiments, refer to Figure 3 The incinerator 12 may also include a fourth incinerator 124 and a fifth incinerator 125 connected in sequence. The fourth incinerator 124 may be connected to the third incinerator 123, and the fifth incinerator 125 may be connected to the dust collector 41. A high-temperature superheater 211 and a low-temperature superheater 212 may be installed in the fourth incinerator 124. The high-temperature superheater 211 may be installed near the bottom of the fourth incinerator 124, and the low-temperature superheater 212 may be installed near the top of the fourth incinerator 124. An air preheater 213 and a high-temperature economizer 214 may be installed in the fifth incinerator 125. The air preheater 213 may be installed near the top of the fifth incinerator 125, and the high-temperature economizer 214 may be installed near the bottom of the fifth incinerator 125. Sodium salts have high viscosity at temperatures above 600℃ and are prone to adhesion and blockage. The flue gas temperature at the outlet of the third-span incinerator 123 is controlled below 600℃, for example, the flue gas temperature at the outlet of the third-span incinerator 123 is 500±20℃. This ensures that the flue gas temperature entering the fourth-span incinerator 124 and the fifth-span incinerator 125 is less than 600℃, thereby reducing the viscosity of the sodium salt and thus reducing the risk of blockage of the heat exchange module 21.

[0053] In some embodiments, refer to Figure 3 The waste heat recovery system 2 may further include a water spray desuperheater 24, which can be installed between the low-temperature superheater 212 and the high-temperature superheater 211, and is connected to the water-side inlet of the waste heat recovery system 2. In this embodiment, the water spray desuperheater 24 can be connected in series on the steam-water pipeline 22 between the low-temperature superheater 212 and the high-temperature superheater 211, and the steam temperature is adjusted by supplying boiler feedwater to the water spray desuperheater 24.

[0054] Reference Figure 3The waste heat recovery system 2 may also include a soot blowing device 25, which is used to remove salt residue from the heat exchange modules 21. The number of soot blowing devices 25 may be one or more. The soot blowing devices 25 may be arranged between or inside the heat exchange modules 21. The soot blowing devices 25 may be, for example, shock wave soot blowers or steam soot blowers. The soot blowing devices 25 may perform soot blowing operations periodically, thereby reducing salt accumulation on the heat exchange modules 21, thus improving heat exchange efficiency and flue gas flow. In some embodiments, at least one explosion-proof door (not shown) may also be arranged on the incinerator 12. When the pressure inside the incinerator 12 is too high, the pressure can be released through the explosion-proof door, thereby reducing safety risks and improving the stability of equipment operation.

[0055] In some embodiments, refer to Figure 1 The ash removal system 3 may include a first ash removal unit 31, a second ash removal unit 32, a device ash removal unit 33, and a collection unit 34. The first ash removal unit 31 may be located at the bottom of the first-span incinerator 121 to collect the salt ash in the first-span incinerator 121. The second ash removal unit 32 may be located at the bottom of the third-span incinerator 123 to collect the salt ash in the third-span incinerator 123. The device ash removal unit 33 may be located at the bottom of the high-temperature economizer 214 and / or the dust collector 41. In this embodiment, the device ash removal unit 33 may be located at the bottom of the high-temperature economizer 214, that is, at the bottom of the fifth-span incinerator 125, or at the bottom of the dust collector 41. The collection unit 34 is used to collect the salt ash and fly ash discharged by the first ash removal unit 31, the second ash removal unit 32, and the device ash removal unit 33.

[0056] In some embodiments, refer to Figure 1 A liquid molten slag pool 1213 may be provided at the bottom of the first incinerator 121. To ensure that the liquid molten salt can be smoothly discharged from the liquid molten slag pool 1213, the outlet flue gas temperature of the first incinerator 121 shall not be lower than 950℃, for example, the outlet flue gas temperature of the first incinerator 121 shall be 1000±20℃. The first slag discharge unit 31 may include a first biaxial cooler 311 and a first discharge valve 312. The first biaxial cooler 311 may be connected to the liquid molten slag pool 1213. The first biaxial cooler 311 may adopt a water-cooled structure to cool, solidify and crush the liquid molten salt. The first discharge valve 312 may adopt a double-cut-off, double-baffle or star-shaped discharge valve type to discharge the cooled salt slag. The first discharge valve 312 may be electrically controlled to reduce manual operation.

[0057] When the temperature of the salt residue at the outlet of the first biaxial cooler 311 is higher than or equal to a preset value, such as 150°C, the first slag discharge unit 31 may further include a drum slag cooler 313, which is located downstream of the first biaxial cooler 311, i.e., between the first biaxial cooler 311 and the first discharge valve 312. The drum slag cooler 313 can further reduce the temperature of the salt residue, for example, to below 120°C. In some embodiments, when the temperature of the salt residue at the outlet of the first biaxial cooler 311 is lower than a preset value, such as 150°C, the drum slag cooler 313 may not be required.

[0058] Reference Figure 1 The first ash discharge unit 31 may further include a second burner 314 and a second fan 315. The second burner 314 may be disposed on the bottom side wall of the first cross-section incinerator 121. The second burner 314 is used to increase the outlet flue gas temperature of the first cross-section incinerator 121 to prevent the outlet flue gas temperature of the first cross-section incinerator 121 from being too low when the incinerator 12 is under low load. The second burner 314 may be provided with a second fuel inlet 3141 and a third air inlet 3142. The fuel system 5 may include a second fuel pipe 52, and the second fuel inlet 3141 may be connected to the second fuel pipe 52, through which fuel can be injected into the second burner 314. The second fan 315 can pressurize the air and deliver air to the second burner 314 through the third air inlet 3142 to improve combustion efficiency. In some embodiments, the second burner 314 may also be provided with a viewing hole (not shown) and a flame detector (not shown) for real-time monitoring of the combustion status.

[0059] Because the incineration system 1 operates under negative pressure, air can be reverse-flowed from the first slag discharge unit 31 to the first cross-section incineration boiler 121, thereby reducing the temperature of the liquid molten salt in the liquid slag pool 1213, and even causing the liquid molten salt to cool and solidify at the slag discharge port, thus blocking the slag discharge port. (Refer to...) Figure 1The first ash discharge unit 31 may further include a third fan 316. The inlet end of the third fan 316 can be connected to the first biaxial cooler 311 through a first duct 3161. The third fan 316 can ensure that the pressure inside the first biaxial cooler 311 is lower than the bottom pressure of the first cross-section incinerator 121, thereby preventing air backflow into the first cross-section incinerator 121. The inlet end of the third fan 316 can also be connected to the outside atmosphere through a third duct 3163 to draw in air and reduce the temperature of the flue gas entering the third fan 316. As an example, the third duct 3163 merges with the first duct 3161, where outside cold air mixes with the flue gas from the first biaxial cooler 311 to reduce the flue gas temperature, for example, to below 250°C. This prevents damage to the third fan 316 due to excessively high flue gas temperature, thereby extending the service life of the third fan 316. The third duct 3163 may be equipped with a valve (not shown) to control the airflow and thus regulate the temperature of the flue gas.

[0060] Reference Figure 1 The outlet end of the third blower 316 can be connected to the bottom of at least one of the third, fourth, and fifth incinerator boilers 123, 124, and 125 via the second duct 3162. In this embodiment, the outlet end of the third blower 316 can be connected to the bottom of the third incinerator boiler 123 via the second duct 3162. The cooled flue gas flows into the bottom of the third incinerator boiler 123 through the second duct 3162, thus regulating the temperature of the flue gas inside the third incinerator boiler 123. As an example, the outlet flue gas temperature of the third incinerator boiler 123 is controlled below 600°C, for example, 500±20°C. This ensures that the flue gas temperature entering the fourth and fifth incinerator boilers 124 and 125 is less than 600°C, reducing the viscosity of the sodium salt and thus reducing the risk of blockage of the heat exchange module 21.

[0061] Reference Figure 1 The second slag discharge unit 32 may include a second biaxial cooler 321 and a second discharge valve 322. The second biaxial cooler 321 may be connected to the third incinerator 123. The molten salt in the third incinerator 123 is solid molten salt. The second biaxial cooler 321 may adopt a water-cooled structure to cool, solidify, and crush the solid molten salt. The second discharge valve 322 may be a double-cutoff, double-baffle, or star-type discharge valve to discharge the cooled salt slag. The second discharge valve 322 may be electrically controlled to reduce manual operation.

[0062] Reference Figure 1The ash discharge unit 33 may include a third discharge valve 331 and a fourth discharge valve 332. The third discharge valve 331 may be located at the bottom of the high-temperature economizer 214, i.e., at the bottom of the fifth-span incinerator 125. The fourth discharge valve 332 may be located at the bottom of the dust collector 41, used to collect powdered salt residue from the flue gas, such as fly ash. Both the third discharge valve 331 and the fourth discharge valve 332 may be of the type of double-cutoff, double-baffle, or star-shaped discharge valve, used to discharge the cooled salt residue. Both the third discharge valve 331 and the fourth discharge valve 332 may be electrically controlled to reduce manual operation.

[0063] In some embodiments, refer to Figure 1 The collection unit 34 is, for example, a ton bag, and is used to load salt residue. There can be multiple collection units 34, which can be respectively configured with a first discharge valve 312, a second discharge valve 322, a third discharge valve 331, and a fourth discharge valve 332. The first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332 can respectively discharge the salt residue into their corresponding collection units 34.

[0064] Or, refer to Figure 1 The slag discharge system 3 may also include a conveying device 35, such as a scraper conveyor. The conveying device 35 may be located below at least one of the first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332. The first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332 may respectively discharge salt slag onto the conveying device 35, which is used to transport the salt slag discharged from the first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332 to the collection unit 34.

[0065] The number of conveying devices 35 can be one or more. For example, when there is only one conveying device 35, it is positioned below the first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332. When there are multiple conveying devices 35, each device can be positioned in a one-to-one correspondence with the first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332. When there are multiple conveying devices 35, at least one device is positioned below at least two of the first discharge valve 312, the second discharge valve 322, the third discharge valve 331, and the fourth discharge valve 332. The number and placement of the conveying devices 35 can be determined according to actual needs.

[0066] In some embodiments, refer to Figure 1 The denitrification device 42 may include a denitrification agent delivery device 421, a third burner 422, a denitrification reactor 423, and a fourth fan 424. The denitrification agent delivery device 421 provides the denitrification agent and may be located on the downstream flue 4223 of the third burner 422, which is connected to the denitrification reactor 423. The third burner 422 increases the temperature of the flue gas and may be located downstream of the dust collector 41. The third burner 422 is connected to the denitrification reactor 423 via a flue. The denitrification reactor 423 may be, for example, an SCR reactor (Selective Catalytic Reduction Reactor). Before entering the denitrification reactor 423, the denitrification agent is mixed with the heated flue gas in the flue to increase its temperature, preventing the denitrification efficiency from decreasing due to excessively low agent temperature, thereby improving the denitrification efficiency. The flue can also be equipped with a baffle plate (not shown) or a flue gas rectification module (not shown) to improve the uniformity of mixing between the denitrification agent and the heated flue gas, thereby further improving the denitrification efficiency of the denitrification agent. In some embodiments, when the temperature and denitrification efficiency of the denitrification agent meet the emission requirements, the third burner 422 may not be provided or the third burner 422 may be turned off.

[0067] Reference Figure 1 The third burner 422 may be equipped with a third fuel inlet 4221 and a fourth air inlet 4222. The fuel system 5 may include a third fuel pipe 53, and the third fuel inlet 4221 may be connected to the third fuel pipe 53, allowing fuel to be injected into the third burner 422 through the third fuel pipe 53 and the third fuel inlet 4221. A fourth fan 424 may pressurize air and supply air to the third burner 422 through the fourth air inlet 4222 to improve combustion efficiency. In some embodiments, the third burner 422 may also be equipped with a viewing window (not shown) and a flame detector (not shown) for real-time monitoring of the combustion status.

[0068] According to a second aspect of this application, one embodiment of this application provides a method for incinerating saline waste liquid, using saline waste liquid incineration equipment as described above, and the saline waste liquid incineration method includes the following steps.

[0069] Salty waste and fuel are fed into incineration system 1 for incineration.

[0070] Specifically, high-calorific-value waste liquid and high-calorific-value waste gas are injected into the first burner 11 through the first waste liquid interface 1121 and the first waste gas interface 1122, respectively. Low-calorific-value waste liquid and low-calorific-value waste gas are injected into the first cross-burning boiler 121 through the second waste liquid interface 12111 and the second waste gas interface 12112, respectively. Fuel is connected to the first burner 11 through the first fuel interface 111, and fuel for the second burner 314 is connected through the second fuel interface 3141.

[0071] The first blower 13 is started, and air enters the first burner 11 and the first cross-section incinerator 121 through the first air inlet 113 and the second air inlet 1212, respectively. The second blower 315 and the fourth blower 424 are started to provide air to the second burner 314 and the third burner 422. By controlling the fuel flow rate, the outlet flue gas temperature of the first cross-section incinerator 121 is kept at no less than 950°C, and the residence time of the flue gas in the temperature range above 1100°C is kept at more than 2.0 s. By controlling the air flow rate of the first blower 13, the oxygen content in the flue gas in the first burner 11 and the first cross-section incinerator 121 is kept at more than or equal to 6%, so as to achieve complete oxidation and decomposition of saline waste.

[0072] Start the induced draft fan 14 to maintain the incineration system 1 under a negative pressure environment of -100PaG to -500PaG. The flue gas flows sequentially through the first burner 11, the first span incineration boiler 121, the second span incineration boiler 122, the third span incineration boiler 123, the high-temperature superheater 211, the low-temperature superheater 212, the air preheater 213, the high-temperature economizer 214, the dust collector 41, the third burner 422, the denitrification reactor 423, the low-temperature economizer 215, the induced draft fan 14, and the chimney 15.

[0073] The waste heat recovery system 2 recovers the heat from the high-temperature flue gas and generates high-temperature steam.

[0074] Specifically, the high-temperature flue gas generated during combustion flows through each heat exchange module 21 in sequence, exchanging heat with the boiler feedwater in the steam-water pipeline 22. The high-temperature flue gas heats the boiler feedwater in the low-temperature economizer 215, and then heats the boiler feedwater in the high-temperature economizer 214. After entering the first part 232 of the steam drum 23, the boiler feedwater enters the water-cooled wall 216 for heat exchange and then enters the first part 232 of the steam drum 23 again. The steam passes through the gas-liquid separator 231 and enters the second part 233 of the steam drum 23. The steam in the second part 233 of the steam drum 23 enters the low-temperature superheater 212 and the high-temperature superheater 211, where it is heated into high-temperature steam and fed into the steam pipeline network. The air preheater 213 uses the waste heat of the flue gas to preheat the combustion air, improving combustion efficiency.

[0075] During operation, the steam temperature is adjusted by the water spray desuperheater 24 to ensure that the steam parameters meet the standards; the soot blowing device 25 is started regularly to remove the salt slag buildup on the heat exchange module 21 to ensure heat exchange efficiency.

[0076] Salt residue and fly ash in the flue gas are collected through the ash removal system 3.

[0077] Specifically, the liquid molten salt at the bottom of the first incinerator 121 flows into the first twin-shaft cooler 311. After cooling, solidification, and crushing, if further cooling is required, it is sent to the drum slag cooler 313 and finally discharged through the first discharge valve 312. The third fan 316 is operated to prevent cold air from backflowing into the first incinerator 121 and to control the temperature of the flue gas entering the third fan 316 to be below 250°C. The solid molten salt at the bottom of the third incinerator 123 is cooled and crushed by the second twin-shaft cooler 321 and discharged through the second discharge valve 322. The powdery salt slag collected at the bottom of the high-temperature economizer 214 and the dust collector 41 is discharged through the third discharge valve 331 and the fourth discharge valve 332, respectively.

[0078] Start the conveying device 35 to collect and transport the salt residue discharged from each unloading valve to the collection unit 34, or use multiple collection units 34 to collect it separately.

[0079] The flue gas is treated for dust removal and denitrification through the flue gas purification system 4.

[0080] Specifically, the flue gas enters the dust collector 41, where particulate matter is filtered out. The filtered flue gas then enters the third burner 422. The denitrification agent delivered by the denitrification agent delivery device 421 mixes with the flue gas in the flue downstream of the third burner 422 and then enters the denitrification reactor 423. Under the action of the catalyst in the denitrification reactor 423, NO is reduced. x It can be reduced to N2 and H2O. After the purified flue gas passes through the low-temperature economizer 215 to recover waste heat, it is sent into the chimney 15 by the induced draft fan 14 and discharged into the atmosphere.

[0081] In the description of this application, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Therefore, a feature defined as "first" or "second" may explicitly or implicitly include one or more features. In the description of this application, "multiple" means two or more, unless otherwise explicitly specified.

[0082] In the above embodiments, the descriptions of each embodiment have different focuses. For parts not described in detail in a certain embodiment, please refer to the relevant descriptions in other embodiments.

[0083] The embodiments, implementation methods, and related technical features of this application can be combined and substituted for each other without conflict.

[0084] The above are merely preferred embodiments of this application and are not intended to limit this application in any way. Any simple modifications, equivalent changes, and alterations made to the above embodiments based on the technical essence of this application without departing from the technical solution of this application shall still fall within the scope of the technical solution of this application.

Claims

1. A saline waste liquid incineration treatment device, characterized in that, include: An incineration system, the incineration system including a first burner and an incinerator, the incinerator including a first cross-section incinerator boiler, a second cross-section incinerator boiler and a third cross-section incinerator boiler connected in sequence, the first burner being disposed on top of the first cross-section incinerator boiler; The waste heat utilization system includes multiple heat exchange modules and steam-water pipelines. The heat exchange modules are located downstream of the third-span incineration boiler, and at least some of the heat exchange modules are connected through the steam-water pipelines. The slag removal system is connected to the first cross-type incinerator and the third cross-type incinerator respectively, and is used to collect liquid salt slag in the first cross-type incinerator and solid salt slag in the third cross-type incinerator. A flue gas purification system, comprising a dust collector and a denitrification device, wherein the dust collector is located downstream of the incinerator and the denitrification device is located downstream of the dust collector; The first burner is provided with a first fuel inlet, a first waste inlet and a first air inlet, wherein the first waste inlet includes a first waste liquid inlet; The first cross-type incineration boiler is provided with a second waste inlet and a second air inlet. The second waste inlet includes a second waste liquid inlet. The second air inlet is located on the side wall of the first cross-type incineration boiler, and the distance between the second air inlet and the top of the first cross-type incineration boiler in the height direction is 1.5m to 4.0m. The incineration system also includes a first blower, which supplies air to the first burner through the first air interface and to the first cross-incineration boiler through the second air interface. At least one heat exchange module is provided between the first air interface and the first fan.

2. The saline waste liquid incineration treatment equipment according to claim 1, characterized in that, The multiple heat exchange modules include a high-temperature superheater, a low-temperature superheater, an air preheater, a high-temperature economizer, and a low-temperature economizer. The high-temperature superheater, the low-temperature superheater, the air preheater, and the high-temperature economizer are sequentially arranged downstream of the third-span incinerator in the flue gas flow path, and the low-temperature economizer is arranged downstream of the denitrification device. The waste heat utilization system also includes a steam drum. The low-temperature economizer, the steam drum, the high-temperature economizer, the low-temperature superheater, and the high-temperature superheater are connected in sequence through the steam-water pipeline. The low-temperature economizer is connected to the water-side inlet of the waste heat utilization system, and boiler feedwater flows into the low-temperature economizer. The high-temperature superheater is connected to the steam-side outlet of the waste heat utilization system, and high-temperature steam flows out of the high-temperature superheater. The heat exchange modules further include water-cooled walls, and at least one of the first, second, and third cross-type incinerators is provided with the water-cooled wall. The steam drum is also connected to the water-cooled wall via downcomers and upcomers.

3. The saline waste liquid incineration treatment equipment according to claim 2, characterized in that, The incinerator also includes a fourth and a fifth incinerator connected in sequence. The fourth incinerator is connected to the third incinerator. The high-temperature superheater and the low-temperature superheater are located in the fourth incinerator, and the air preheater and the high-temperature economizer are located in the fifth incinerator.

4. The saline waste liquid incineration treatment equipment according to claim 2, characterized in that, The waste heat recovery system further includes a water spray desuperheater, which is disposed between the low-temperature superheater and the high-temperature superheater, and is connected to the water-side inlet of the waste heat recovery system; and / or, The waste heat utilization system also includes a soot blowing device for removing salt residue from the heat exchange module.

5. The saline waste liquid incineration treatment equipment according to claim 3, characterized in that, The ash removal system includes a first ash removal unit, a second ash removal unit, a device ash removal unit, and a collection unit. The first ash removal unit is located at the bottom of the first-span incineration boiler, the second ash removal unit is located at the bottom of the third-span incineration boiler, the device ash removal unit is located at the bottom of the high-temperature economizer and / or the dust collector, and the collection unit is used to collect the salt slag and fly ash discharged by the first ash removal unit, the second ash removal unit, and the device ash removal unit.

6. The saline waste liquid incineration treatment equipment according to claim 5, characterized in that, The first slag discharge unit includes a first biaxial cooler and a first discharge valve. A liquid molten slag pool is provided at the bottom of the first cross-burning boiler. The first biaxial cooler is connected to the liquid molten slag pool. The second slag discharge unit includes a second biaxial cooler and a second discharge valve, wherein the second biaxial cooler is connected to the third cross-burning boiler; The ash discharge unit of the device includes a third discharge valve and a fourth discharge valve.

7. The saline waste liquid incineration treatment equipment according to claim 6, characterized in that, The first ash removal unit further includes a second burner and a second fan. The second burner is disposed on the bottom side wall of the first cross-burning boiler. The second burner is provided with a second fuel inlet and a third air inlet. The second fan supplies air to the second burner through the third air inlet; and / or, The first slag discharge unit also includes a drum slag cooler, which is located between the first twin-shaft cooler and the first discharge valve.

8. The saline waste liquid incineration treatment equipment according to claim 6, characterized in that, The first ash removal unit also includes a third fan, the inlet end of which is connected to the first twin-shaft cooler, and the outlet end of which is connected to the bottom of at least one of the third-span incinerator, the fourth-span incinerator, and the fifth-span incinerator. The inlet of the third fan is also connected to the outside atmosphere to draw in air and reduce the temperature of the flue gas entering the third fan.

9. The saline waste liquid incineration treatment equipment according to claim 6, characterized in that, The number of collection units is multiple, and each of the multiple collection units is respectively configured to correspond to the first discharge valve, the second discharge valve, the third discharge valve, and the fourth discharge valve; or... The slag discharge system further includes a conveying device, which is disposed below at least one of the first discharge valve, the second discharge valve, the third discharge valve, and the fourth discharge valve. The conveying device is used to convey the salt slag discharged from the first discharge valve, the second discharge valve, the third discharge valve, and the fourth discharge valve to the collection unit.

10. The saline waste liquid incineration treatment equipment according to claim 1, characterized in that, The denitrification device includes a denitrification agent delivery device, a third burner, a denitrification reactor, and a fourth fan. The third burner is located downstream of the dust collector. The denitrification agent delivery device is arranged on the downstream flue of the third burner. The third burner is connected to the denitrification reactor. The third burner is provided with a third fuel interface and a fourth air interface. The fourth fan supplies air to the third burner through the fourth air interface.

11. The saline waste liquid incineration treatment equipment according to claim 1, characterized in that, The incineration system also includes an induced draft fan and a chimney, with the induced draft fan located downstream of the denitrification unit and the chimney located downstream of the induced draft fan.

12. A method for incinerating saline waste liquid, characterized in that, Using the saline waste liquid incineration treatment equipment as described in any one of claims 1 to 11, the saline waste liquid incineration treatment method includes: Salty waste and fuel are fed into the incineration system for incineration; The waste heat recovery system recovers the heat from the high-temperature flue gas and generates high-temperature steam. The slag and fly ash in the flue gas are collected through the slag removal system. The flue gas is treated by dust removal and denitrification through the flue gas purification system.

13. The method for incinerating saline wastewater according to claim 12, characterized in that, The step of feeding the saline waste and fuel into the incineration system for incineration includes: The flue gas temperature at the outlet of the first cross-burning boiler is controlled by controlling the fuel flow rate. The oxygen content in the flue gas in the first burner and the first cross-burner boiler is controlled to be greater than or equal to 6% by controlling the air flow.

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