A low-concentration sodium salt-containing organic waste liquid incinerator, incineration system and incineration process

Abstract

The present invention relates to a low-concentration sodium salt-containing organic waste liquid incinerator, comprising a burner, a vertical top-burning incineration chamber, a first transition section, a gas-solid separation sedimentation chamber, and a Π-shaped convection chamber. The present invention also relates to an incineration system including the aforementioned incinerator, and also includes a waste liquid pump, a gasifier, an electrostatic precipitator, an induced draft fan, a chimney and a steam drum, and the incinerator is connected to the electrostatic precipitator, the induced draft fan and the chimney in sequence through the incineration flue gas outlet. The present invention also includes an incineration process using the aforementioned incineration system. The present invention uses the superheated steam produced by the incineration flue gas to gasify most of the water and light component organic waste liquid in the organic waste liquid, and integrates the technologies of molten liquid slagging (sodium peroxide), sodium peroxide conversion to sodium carbonate, gas-solid sedimentation separation, solid particle kinetic energy elimination sedimentation separation, equipment (soot blower) cleaning, and manual descaling, so as to extend the equipment inspection and maintenance cycle, so as to make the sodium salt incineration treatment method with economical recovery of waste heat and by-product steam, which was originally unable to operate stably, possible.

Description

Technical Field

[0001] The invention relates to the fields of fine chemical industry and petrochemical industry, and in particular to an incinerator, an incineration system and an incineration process for low-concentration sodium salt-containing organic waste liquid. Background Art

[0002] Incineration is an effective means for chemical plants to treat toxic and hazardous wastes. The incineration reaction is an oxidative pyrolysis reaction at high temperature. Incineration treatment technology requires that the high-temperature gas produced by the incineration reaction must be quickly cooled (quenched) to avoid the occurrence of incineration reverse reactions and side reactions. The quenching method generally adopts two methods: water quenching and rapid cooling of waste heat boilers. For incineration devices with a small amount of waste, the method of spraying water for quenching is generally adopted to treat the wastewater; for incineration devices with a relatively large amount of waste treatment, the method of rapid cooling of by-product steam by waste heat boilers is generally adopted to improve the economic efficiency of the operation of the incineration device. For low-concentration organic waste liquid, its incineration process requires the addition of a large amount of fuel to gasify the water in the waste liquid and make it reach the incineration temperature. It is difficult to treat the salt-containing waste liquid with a relatively large treatment volume after incineration, especially for organic waste liquid containing sodium salt. If the heat is not recovered, a large amount of heat energy will be lost, greatly reducing the economic efficiency of the device operation; if the heat is recovered, the molten and solid sodium peroxide and other inorganic sodium salts carried in the flue gas after incineration will adhere to the wall of the heat exchange tube to form a "dirt layer", reducing the heat exchange efficiency, shortening the equipment operation cycle, and even making the equipment unable to operate. Summary of the invention

[0003] The purpose of the present invention is to improve and innovate the shortcomings and problems existing in the background technology, and to provide a sodium salt incinerator, incineration system and incineration treatment method for recovering waste heat and by-product steam with good economy and strong stability.

[0004] The technical solution of the present invention is to construct a low-concentration sodium salt-containing organic waste liquid incinerator, including a burner, a vertical top-burning incineration chamber, a first transition section, a gas-solid separation sedimentation chamber, and a Π-shaped convection chamber. The burner is arranged at the top of the incineration chamber, and an organic waste liquid and water vapor inlet is arranged on the upper side of the incineration chamber. An organic waste liquid and water vapor distributor is arranged at a corresponding position in the incineration chamber, which is located below the burner. A funnel-shaped molten slag discharge port is arranged at the bottom of the incineration chamber. The Π-shaped convection chamber includes a first convection section, a second transition section, and a second convection section. The sedimentation chamber is arranged at the bottom of the first convection section of the Π-shaped convection chamber and is connected. A first solid slag discharge port is arranged at the bottom. The sedimentation chamber One side is connected with the side of the incineration chamber through the first transition section, the first evaporator is arranged in the first transition section, the second evaporator is arranged in the settling chamber, the third evaporator and the fourth evaporator are respectively arranged in the first convection section and the second convection section, wherein the third evaporator is located above the settling chamber, and a blocking pipe is arranged below, a steam superheater is arranged in the upper part of the Π-shaped convection chamber, i.e., the second transition section, and a boiler water preheater is arranged below the fourth evaporator, soot blowers are arranged at corresponding positions of the third evaporator, the steam superheater and the boiler water preheater, a second solid slag discharge port is arranged at the bottom of the second convection section of the Π-shaped convection chamber, and an incineration flue gas outlet is arranged on the side, which is located below the boiler water preheater. The third evaporator and the fourth evaporator are both vertical tube evaporators, including a number of vertical heat exchange sleeves, heat exchange tubes, and sleeve headers. The sleeve header is arranged above the heat exchange sleeve. The heat exchange sleeve includes a heat exchange sleeve outer tube and a heat exchange sleeve inner tube inside it. The sleeve header includes a sleeve header outer tube and a sleeve header inner tube inside it. The tops of all heat exchange sleeve inner tubes are connected to the sleeve header inner tube, and the bottom is open. At least four heat exchange tubes are arranged around each heat exchange sleeve. The upper and lower ends of the heat exchange tubes are respectively connected to the upper and lower ends inside the heat exchange sleeve outer tube, and are connected to the space between the sleeve header outer tube and the sleeve header inner tube. The sleeve header inner tube is provided with a saturated boiler water inlet, and the sleeve header outer tube is provided with a water and steam outlet. More preferably, six heat exchange tubes are evenly arranged around each heat exchange sleeve, and the heat exchange sleeves are distributed in a square array. The inner wall of the incinerator is lined. A cold air protection water injector is provided in the first transition section. The lower end caps of the outer tubes of the heat exchange sleeves in the third evaporator and the fourth evaporator are connected to the tube bundle or the cross-tube bundle to reduce vibration.Another technical solution of the present invention is to construct a low-concentration sodium salt-containing organic liquid incineration system, including an incinerator, a waste liquid pump, a gasifier, an electrostatic precipitator, an induced draft fan, a chimney and a steam drum, wherein the incinerator is connected to the electrostatic precipitator, the induced draft fan and the chimney in sequence through the incineration flue gas outlet; the gasifier includes an organic waste liquid inlet, an organic waste liquid outlet and an organic waste gas outlet, the organic waste liquid outlet is connected to the organic waste liquid and water vapor inlet of the incinerator, and the organic waste gas outlet is connected to the burner of the incinerator through the waste liquid pump; the steam drum is arranged above the incinerator, and its ascending pipe and descending pipe are respectively connected to the first evaporator, the second evaporator, the third evaporator, the steam superheater, the fourth evaporator and the boiler water preheater in the incinerator, and its steam pipe is connected to the steam superheater, and is connected to the gasifier, the burner and the soot blower through the steam superheater; the induced draft fan provides negative pressure for the incinerator and the electrostatic precipitator upstream thereof. The gasifier and the steam drum are supported by the steel structure of the incinerator. Another technical solution of the present invention is to construct a low-concentration sodium salt-containing organic waste liquid incineration process, the steps of which include: ① the system is provided with an induced draft fan, which operates under a slight negative pressure; ② supplementary fuel enters from the burner and burns in the incineration chamber, which is used to heat up the incinerator when it is started and to ensure safe operation and provide auxiliary heat during normal operation; ③ the low-concentration sodium salt-containing organic waste liquid enters the gasifier and is gasified by the superheated steam generated by the incineration flue gas; ④ the saturated water vapor and light component organic waste liquid gas generated in the gasifier are evenly distributed into the incineration chamber with a slight negative pressure and reaching the incineration temperature for incineration; ⑤ the organic waste liquid concentrated in the gasifier is pumped to the burner through the waste liquid pump, atomized by the self-produced superheated steam, and then enters the incineration chamber that has reached the incineration temperature for incineration; ⑥ the incineration temperature is much higher than the melting point of sodium peroxide, so that the inorganic sodium salt produced after incineration is completely converted into molten sodium peroxide; ⑦ the organic waste liquid is top-sprayed into the furnace after being atomized, so that the molten sodium peroxide droplets generated by incineration are evenly distributed The top jet (containing sodium peroxide droplets) is uniformly dispersed in the high-temperature gas after incineration; the top jet flow (containing sodium peroxide droplets) is in the same direction as gravity, which is conducive to gas-liquid separation and prevents droplets from splashing on the inner wall of the furnace body; ⑧ changing the direction of the airflow so that the gas is discharged from the side wall of the incineration chamber to achieve the separation of molten sodium peroxide droplets and gas; the molten sodium peroxide droplets are collected at the bottom of the incineration chamber and discharged from the incineration chamber by gravity; ⑨ the flue gas (containing molten sodium peroxide droplets) discharged from the incineration chamber is cooled by air distribution, sprayed with water and provided with reaction conditions, so that the flue gas temperature is reduced to below the melting point and decomposition temperature of sodium carbonate, so as to promote the conversion of molten sodium peroxide droplets into solid sodium carbonate particles as much as possible, and then further cooled by the first evaporator; ⑩ the flue gas (containing solid sodium carbonate particles and unconverted sodium peroxide droplets) enters the settling chamber, the flue gas (containing solid sodium carbonate particles and unconverted sodium peroxide droplets) is decelerated, and the second evaporator cools the flue gas (containing solid sodium carbonate particles and unconverted sodium peroxide droplets).

[0005] Further cooling (so that the sodium peroxide droplets that have not been converted into sodium carbonate are completely converted into solid state) and speed reduction, and a plugging pipe is set on the top of the sedimentation chamber to reduce the kinetic energy of the solid particles and further separate the gas and solid;

[0006] The separated sodium carbonate and sodium peroxide solid particles are discharged from the sedimentation chamber, and the tube row of the sedimentation chamber is designed to be maintainable and quickly replaceable; The dry ash (solid sodium carbonate particles and sodium peroxide particles) from the settling chamber enters the Π-shaped convection chamber, is cooled by the third evaporator, the fourth evaporator, and the boiler water preheater, and then is sent to the electrostatic precipitator. The convection chamber is provided with a soot blower and a manhole. The third evaporator, the steam superheater, and the fourth evaporator have vertical pipes, and the steam superheater has a square pipe. The dry ash (solid sodium carbonate particles and sodium peroxide particles) accumulated on the surface of the heat exchange tube is removed by a soot blower or manually. Part of the dry ash is discharged from the settling chamber, and part of it is discharged from the

[0007] The second convection chamber is discharged from the bottom, and the other part enters the electrostatic precipitator along with the flue gas; The flue gas (containing solid sodium carbonate particles and sodium peroxide particles) enters the electrostatic precipitator for dust removal and then meets the emission standards. The removed dust (solid sodium carbonate particles and sodium peroxide particles) is collected and discharged from the electrostatic precipitator. In one embodiment, the temperature control in the incineration process is as follows: the incineration temperature is ≥1100°C, the flue gas after incineration is ≥1100°C, and the air-sprayed water is used to cool the flue gas to 650-700°C; the by-product steam is deposited

[0008] The flue gas temperature in the chamber drops to 350-390℃; the flue gas temperature out of the convection section is 200-250℃.

[0009] Advantages and beneficial effects of the present invention:

[0010] The present invention utilizes the superheated steam produced by the incineration flue gas to gasify most of the water and light organic waste liquid in the organic waste liquid, convert the molten liquid slag (sodium peroxide), sodium peroxide into sodium carbonate, gas-solid sedimentation separation, solid particle kinetic energy elimination sedimentation separation, equipment (soot blower)

[0011] The integration of technologies such as dust cleaning and manual descaling prolongs the equipment inspection and maintenance cycle, making it possible to economically recover the waste heat and byproduct steam containing sodium salt incineration treatment methods that could not be stably operated. The process flow of the present invention is simple, the equipment investment is low, the land is small, the process is safe and reliable, and there are no dangerous processes and equipment. The third evaporator and the fourth evaporator are arranged vertically, so that water and steam can circulate naturally, reducing the operating cost of the incineration device. Its unique arrangement of heat exchange tubes improves the heat efficiency per unit volume and reduces equipment investment. The superheated steam produced by the incineration flue gas is used to gasify most of the water and light organic waste liquid in the organic waste liquid, which reduces the load of the incinerator and greatly reduces the use of supplementary fuel, greatly improving the equipment investment and economic efficiency of the incineration device. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] Figure 1 It is a schematic diagram of the structure of an embodiment.

[0013] Figure 2 This is a diagram of the heat exchange tube bundle components of the third evaporator and the fourth evaporator.

[0014] Figure 3 This is the layout diagram of the heat exchange tube bundles of the third evaporator and the fourth evaporator.

[0015] Figure 4 It is a schematic structural diagram of another embodiment. DETAILED DESCRIPTION

[0016] In order to facilitate the understanding of the present invention, the present invention will be described more fully below with reference to the relevant drawings. The preferred embodiments of the present invention are shown in the drawings. However, the present invention can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, the purpose of providing these embodiments is to make the disclosure of the present invention more thorough and comprehensive. It should be noted that when an element is considered to be "set" on another element, it can be directly set or connected to another element or there may be a centering element at the same time. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those generally understood by technicians in the technical field of the present invention. The terms used in the specification are only for describing specific implementation purposes and are not intended to limit the present invention.

[0017] Example 1 Figure 1As shown, a low-concentration sodium salt-containing organic waste liquid incinerator 1 includes a burner 101, a vertical top-burning incineration chamber 102, a first transition section 103, a gas-solid separation settling chamber 104, and a Π-shaped convection chamber 105. The burner 101 is arranged at the top of the incineration chamber 102, and an organic waste liquid and water vapor inlet 106 is arranged on the upper side of the incineration chamber 102. An organic waste liquid and water vapor distributor 107 is arranged at a corresponding position in the incineration chamber 102, which is located below the burner 101. A funnel-shaped molten slag discharge port 108 is arranged at the bottom of the incineration chamber 102. The Π-shaped convection chamber 105 includes a first convection section 121, a second transition section 115, and a second convection section 122. The settling chamber 104 is arranged at the bottom of the first convection section 121 of the Π-shaped convection chamber 105 and is connected. A first solid slag discharge port 109 is arranged at the bottom. One side of the settling chamber 104 is connected to the first transition section 115. Section 103 is connected to the side of the incineration chamber 102, a first evaporator 110 is arranged in the first transition section 103, a second evaporator 111 is arranged in the settling chamber 104, a third evaporator 112 and a fourth evaporator 113 are arranged in the first convection section 121 and the second convection section 122 respectively, wherein the third evaporator 112 is located above the settling chamber 104, and a plugging pipe 114 is arranged below, a steam superheater 116 is arranged in the upper part of the Π-shaped convection chamber 105, i.e., the second transition section 115, and a boiler water preheater 117 is arranged below the fourth evaporator 113, soot blowers 118 are arranged at the corresponding positions of the third evaporator 112, the steam superheater 116 and the boiler water preheater 117, a second solid slag discharge port 119 is arranged at the bottom of the second convection section 122 of the Π-shaped convection chamber 105, and an incineration flue gas outlet 120 is arranged on the side, which is located below the boiler water preheater 117. Figure 2 , 3As shown, the third evaporator 112 and the fourth evaporator 113 are both vertical tube evaporators, including a plurality of vertical heat exchange sleeves 130, heat exchange tubes 131, and sleeve headers 132. The sleeve headers 132 are arranged above the heat exchange sleeves 130. The heat exchange sleeves 130 include a heat exchange sleeve outer tube 133 and a heat exchange sleeve inner tube 134 therein. The sleeve headers 132 include a sleeve header outer tube 135 and a sleeve header inner tube 136 therein. All heat exchange The top of the inner tube 134 of the casing is connected to the inner tube 136 of the casing header, and the bottom is open. At least four heat exchange tubes 131 are arranged around each heat exchange casing 130. The upper and lower ends of the heat exchange tube 131 are respectively connected to the upper and lower ends of the inner tube 133 of the heat exchange casing, and are connected to the space between the outer tube 135 of the casing header and the inner tube 136 of the casing header. The inner tube 136 of the casing header is provided with a saturated boiler water inlet 137, and the outer tube of the casing header is provided with a water and steam outlet 138. More preferably, six heat exchange tubes 131 are evenly arranged around each heat exchange casing 130, and the heat exchange casing 130 is distributed in a square array. The inner wall of the incinerator 1 is lined. A cold wind protection water injector is provided in the first transition section 103. The lower heads of the outer tube 133 of the heat exchange casing in the third evaporator 112 and the fourth evaporator 113 are connected to the tube bundle or the cross tube bundle to reduce vibration.

[0018] Example 2 Figure 4 As shown, a low-concentration sodium salt-containing organic liquid incineration system includes an incinerator 1, a waste liquid pump 2, a gasifier 3, an electrostatic precipitator 4, an induced draft fan 5, a chimney 6 and a steam drum 7. The incinerator 1 is connected to the electrostatic precipitator 4, the induced draft fan 5 and the chimney 6 in sequence through an incineration flue gas outlet 120; the gasifier 3 includes an organic waste liquid inlet, an organic waste liquid outlet and an organic waste gas outlet, the organic waste liquid outlet is connected to the organic waste liquid and water vapor inlet 106 of the incinerator 1, and the organic waste gas outlet is connected to the combustion gas outlet 106 of the incinerator 1 through the waste liquid pump 2. The steam drum 7 is arranged above the incinerator 1, and its ascending pipe and descending pipe are respectively connected to the first evaporator 110, the second evaporator 111, the third evaporator 112, the steam superheater 116, the fourth evaporator 113 and the boiler water preheater 117 in the incinerator 1, and its steam pipe is connected to the steam superheater 116, and is connected to the gasifier 3, the burner 101 and the soot blower 118 through the steam superheater 116; the induced draft fan 5 provides negative pressure for the incinerator 1 and the electrostatic precipitator 4 upstream thereof. The gasifier and the steam drum are supported by the steel structure of the incinerator, so that the overall structure is compact and occupies a small area.

[0019] Example 3

[0020] A low-concentration sodium salt-containing organic waste liquid incineration process, using the incineration system described in Example 2, the steps of which include: ① the system is provided with an induced draft fan, which operates under a slight negative pressure; ② supplementary fuel enters from the burner 101 and burns in the incineration chamber 102, which is used to heat up when the incinerator 1 is started and to ensure safety and provide auxiliary heat during normal operation; ③ the low-concentration sodium salt-containing organic waste liquid enters the gasifier 3 and is gasified by the superheated steam generated by the incineration flue gas; ④ the saturated water vapor and light component organic waste liquid gas generated in the gasifier 3 are evenly distributed into the slightly negative pressure gas chamber 102 that has reached the incineration temperature. ⑤ The organic waste liquid concentrated in the gasifier 3 is sent to the burner 101 through the waste liquid pump 2, and is atomized by the self-produced superheated steam and then enters the incineration chamber 102 which has reached the incineration temperature for incineration; ⑥ The incineration temperature is much higher than the melting point of sodium peroxide, so that the inorganic sodium salt produced after incineration is completely converted into molten sodium peroxide; ⑦ The organic waste liquid is atomized and top-sprayed into the furnace, so that the molten sodium peroxide droplets generated by incineration are evenly dispersed in the high-temperature gas after incineration; the top jet flow (containing sodium peroxide droplets) is in the same direction as gravity, which is conducive to gas-liquid separation and avoids The droplets splash on the wall of the furnace body; ⑧ Change the direction of the air flow so that the gas is discharged from the side wall of the incineration chamber 102, so as to separate the molten sodium peroxide droplets and the gas; the molten sodium peroxide droplets are collected at the bottom of the incineration chamber 10 and discharged from the incineration chamber 102 by gravity; ⑨ The flue gas (containing molten sodium peroxide droplets) discharged from the incineration chamber is cooled by air, sprayed with water and provided with reaction conditions, so as to reduce the flue gas temperature to below the melting point and decomposition temperature of sodium carbonate, so as to promote the conversion of molten sodium peroxide droplets into solid sodium carbonate particles as much as possible, and then further cooled by the first evaporator; ⑩ The flue gas ( The flue gas (containing solid sodium carbonate particles and unconverted sodium peroxide droplets) enters the settling chamber, the flue gas (containing solid sodium carbonate particles and unconverted sodium peroxide droplets) slows down, the second evaporator cools the flue gas (containing solid sodium carbonate particles and unconverted sodium peroxide droplets) to further cool down (so that the sodium peroxide droplets that have not been converted into sodium carbonate are completely converted into a solid state) and the speed is reduced, and a blocking pipe is set on the top of the settling chamber to reduce the kinetic energy of the solid particles and further separate the gas and solid; the separated sodium carbonate and sodium peroxide solid particles are discharged from the settling chamber, and the settling chamber pipe row is designed to be a maintainable and quickly replaceable structure; The solid sodium carbonate particles and sodium peroxide particles) out of the sedimentation chamber enter the Π-shaped convection chamber, and are sent to the electrostatic precipitator after being cooled by the third evaporator, the steam superheater, the fourth evaporator, and the boiler water preheater. The convection chamber is provided with a soot blower and a manhole, and the third evaporator, the steam superheater, and the fourth evaporator have vertical pipes, and the steam superheater has a square pipe. The dry ash (solid sodium carbonate particles and sodium peroxide particles) accumulated on the surface of the heat exchange tube is removed by a soot blower or manually. A part of the blown dry ash is discharged from the sedimentation chamber, a part is discharged from the bottom of the second convection chamber, and the other part enters the electrostatic precipitator with the flue gas; The flue gas (containing solid sodium carbonate particles and sodium oxide particles) enters the sodium remover to remove the sodium and then meets the emission standards. The removed dust (solid sodium carbonate particles and sodium peroxide particles) is collected and discharged from the electrostatic precipitator. In one embodiment, the temperature control in the incineration process is as follows: the incineration temperature is ≥1100°C, the flue gas after incineration is ≥1100°C, and the air-sprayed water is cooled to 650-700°C; the flue gas temperature in the byproduct steam settling chamber is reduced to 350-390°C; the flue gas temperature out of the convection section is 200-250°C. The present invention utilizes the superheated steam produced by the incineration flue gas to gasify most of the water and light organic waste liquid in the organic waste liquid, integrates the technologies of molten liquid slag removal (sodium peroxide), sodium peroxide conversion to sodium carbonate, gas-solid sedimentation separation, solid particle kinetic energy elimination sedimentation separation, equipment (soot blower) cleaning, manual descaling, etc., to extend the equipment inspection and maintenance cycle, so that the sodium salt incineration treatment method with economic recovery of waste heat byproduct steam that could not be stably operated originally becomes possible. The process flow of the present invention is simple, the equipment investment is low, the land occupation is small, the process is safe and reliable, and there is no dangerous process and equipment. The third evaporator and the fourth evaporator are arranged vertically, so that water and steam can circulate naturally, reducing the operating cost of the incineration device. Its unique heat exchange tube arrangement method improves the heat efficiency per unit volume and reduces the equipment investment. The superheated steam produced by the incineration flue gas is used to gasify most of the water and light organic waste liquid in the organic waste liquid, reducing the load of the incinerator, and greatly reducing the amount of supplementary fuel used, greatly improving the equipment investment of the incineration device and the economy of the device operation.

[0021] The embodiments described in the present invention are merely descriptions of the preferred implementation modes of the present invention, and are not intended to limit the concept and scope of the present invention. Without departing from the design concept of the present invention, various modifications and improvements made to the technical solutions of the present invention by engineers and technicians in this field should fall within the protection scope of the present invention. The technical contents for which protection is sought in the present invention have all been recorded in the claims.

Claims

1. A low-concentration sodium salt-containing organic waste liquid incinerator, characterized in that: The invention comprises a burner, a vertical top-burning incineration chamber, a first transition section, a gas-solid separation settling chamber, and a Π-shaped convection chamber, wherein the burner is arranged at the top of the incineration chamber, an organic waste liquid and water vapor inlet is arranged on the upper side of the incineration chamber, an organic waste liquid and water vapor distributor is arranged at a corresponding position in the incineration chamber, and is located below the burner, a funnel-shaped molten slag discharge port is arranged at the bottom of the incineration chamber, the Π-shaped convection chamber comprises a first convection section, a second transition section, and a second convection section, the settling chamber is arranged at the bottom of the first convection section of the Π-shaped convection chamber and is connected, a first solid slag discharge port is arranged at the bottom of the first convection section, and one side of the settling chamber passes through the first transition section. It is connected to the side of the incineration chamber, a first evaporator is arranged in the first transition section, a second evaporator is arranged in the settling chamber, a third evaporator and a fourth evaporator are arranged in the first convection section and the second convection section respectively, wherein the third evaporator is located above the settling chamber, and a plugging pipe is arranged below, a steam superheater is arranged in the upper part of the Π-shaped convection chamber, i.e., the second transition section, and a boiler water preheater is arranged below the fourth evaporator, soot blowers are arranged at corresponding positions of the third evaporator, the steam superheater and the boiler water preheater, a second solid slag discharge port is arranged at the bottom of the second convection section of the Π-shaped convection chamber, and an incineration flue gas outlet is arranged on the side, which is located below the boiler water preheater; The third evaporator and the fourth evaporator are both vertical tube evaporators, including a plurality of vertical heat exchange sleeves, heat exchange tubes, and sleeve headers. The sleeve header is arranged above the heat exchange sleeves. The heat exchange sleeves include a heat exchange sleeve outer tube and a heat exchange sleeve inner tube inside the sleeve. The sleeve header includes a sleeve header outer tube and a sleeve header inner tube inside the sleeve. The tops of all heat exchange sleeve inner tubes are connected to the sleeve header inner tube, and the bottom is open. At least four heat exchange tubes are arranged around each heat exchange sleeve. The upper and lower ends of the heat exchange tubes are respectively connected to the upper and lower ends inside the heat exchange sleeve outer tube, and are connected to the space between the sleeve header outer tube and the sleeve header inner tube. The sleeve header inner tube is provided with a saturated boiler water inlet, and the sleeve header outer tube is provided with a water and steam outlet; Six heat exchange tubes are evenly arranged around each heat exchange sleeve, and the heat exchange sleeves are distributed in a square array; The inner wall of the incinerator is lined; The first transition section is provided with a cold air protection water ejector; The lower end caps of the outer tubes of the heat exchange sleeves in the third evaporator and the fourth evaporator are connected to the tube bundle or the cross-tube bundle to reduce vibration.

2. The incineration system of a low-concentration sodium salt-containing organic waste liquid incinerator according to claim 1, characterized in that: It includes an incinerator, a waste liquid pump, a gasifier, an electrostatic precipitator, an induced draft fan, a chimney and a steam drum. The incinerator is connected to the electrostatic precipitator, the induced draft fan and the chimney in sequence through the incineration flue gas outlet; the gasifier includes an organic waste liquid inlet, an organic waste liquid outlet and an organic waste gas outlet. The organic waste liquid outlet is connected to the organic waste liquid and water vapor inlet of the incinerator, and the organic waste gas outlet is connected to the burner of the incinerator through the waste liquid pump; the steam drum is arranged above the incinerator, and its ascending pipe and descending pipe are respectively connected to the first evaporator, the second evaporator, the third evaporator, the steam superheater, the fourth evaporator and the boiler water preheater in the incinerator, and its steam pipe is connected to the steam superheater, and is connected to the gasifier, the burner and the soot blower through the steam superheater; the induced draft fan provides negative pressure for the incinerator and the electrostatic precipitator upstream thereof; The gasifier and steam drum are supported by the steel structure of the incinerator.

3. The incineration process of a low-concentration sodium salt-containing organic waste liquid incinerator according to claim 1 is characterized in that the steps include: ① The system is equipped with an induced draft fan, which operates under a slight negative pressure; ② The supplementary fuel enters from the burner and burns in the incineration chamber, which is used to heat up the incinerator when it is started and to ensure safety and provide auxiliary heat during normal operation; ③ The low-concentration sodium-containing organic waste liquid enters the gasifier and is gasified by the superheated steam generated by the incineration flue gas; ④ The saturated water vapor and light-component organic waste liquid gas generated in the gasifier are evenly distributed into the incineration chamber with a slight negative pressure and has reached the incineration temperature for incineration; ⑤ The concentrated organic waste liquid in the gasifier is sent to the burner through the waste liquid pump, atomized by the self-produced superheated steam, and then enters the incineration chamber that has reached the incineration temperature. Incineration in the incineration chamber; ⑥ The incineration temperature is much higher than the melting point of sodium peroxide, so that all the inorganic sodium salts produced after incineration are converted into molten sodium peroxide; ⑦ The organic waste liquid is atomized and then sprayed into the furnace, so that the molten sodium peroxide droplets generated by incineration are evenly dispersed in the high-temperature gas after incineration; The top jet flow containing sodium peroxide droplets is in the same direction as gravity, which is conducive to gas-liquid separation and prevents droplets from splashing on the inner wall of the furnace body; ⑧ Change the direction of the air flow so that the gas is discharged from the side wall of the incineration chamber, and the molten sodium peroxide droplets and gas are separated; The molten sodium peroxide droplets are collected at the bottom of the incineration chamber and discharged from the incineration chamber by gravity; ⑨ The flue gas containing molten sodium peroxide droplets discharged from the incineration chamber is cooled by air distribution and water spray cooling to provide reaction conditions, so as to reduce the flue gas temperature to below the melting point and decomposition temperature of sodium carbonate, so as to promote the conversion of molten sodium peroxide droplets into solid sodium carbonate particles as much as possible, and then further cooled by the first evaporator; ⑩ The flue gas containing solid sodium carbonate particles and unconverted sodium peroxide droplets enters the settling chamber, the flue gas containing solid sodium carbonate particles and unconverted sodium peroxide droplets is decelerated, and the second evaporator is cooled to further cool the flue gas containing solid sodium carbonate particles and unconverted sodium peroxide droplets, so that the sodium peroxide droplets that have not been converted into sodium carbonate are completely converted into a solid state, the speed is reduced, and a plugging pipe is set on the top of the settling chamber to reduce the kinetic energy of the solid particles and further separate the gas and solid; the separated sodium carbonate and sodium peroxide solid particles are discharged from the settling chamber, and the settling chamber pipe row is designed to be a maintainable and quickly replaceable structure; The flue gas containing solid sodium carbonate particles and sodium peroxide particles exiting the settling chamber enters the Π-shaped convection chamber, is cooled by the third evaporator, the steam superheater, the fourth evaporator, and the boiler water preheater, and then is sent to the electrostatic precipitator. The convection chamber is provided with a soot blower and a manhole, and the third evaporator, the steam superheater, and the fourth evaporator have vertical pipes, and the steam superheater has square pipes. The dry ash accumulated on the surface of the heat exchange tube is removed by a soot blower or manually. The dry ash is solid sodium carbonate particles and sodium peroxide particles. Part of the dry ash blown off is discharged from the settling chamber, part is discharged from the bottom of the second convection chamber, and the other part enters the electrostatic precipitator with the flue gas; The flue gas containing solid sodium carbonate particles and sodium peroxide particles enters the electrostatic precipitator for dust removal and then meets the emission standards. The removed dust containing solid sodium carbonate particles and sodium peroxide particles is collected and discharged from the electrostatic precipitator. The temperature control in the incineration process is as follows: incineration temperature ≥1100℃, flue gas after incineration ≥1100℃, air-sprayed water cooling to 650-700℃; flue gas temperature in the by-product steam settling chamber drops to 350-390℃; flue gas outlet convection section temperature 200-250℃.

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