A carbon black incineration process method

Abstract

The present invention belongs to the fields of fine chemical industry and natural gas chemical industry, and particularly relates to a process method for carbon black incineration. Aiming at the problems of large fuel consumption, high equipment investment, incomplete incineration and poor effect in existing incinerators, the following scheme is now proposed, which includes the following steps: S1: A drying separator, a first-stage incinerator, a second-stage incinerator, an incinerator heat recovery section, a steam drum, an induced draft fan and a chimney are provided; a burner I, a burner II and a burner III are respectively installed at the front end, the middle part of the first-stage incinerator and the front end of the second-stage incinerator; the incinerator heat recovery section includes an evaporator I, an evaporator II, a steam superheater I, a steam superheater II, an evaporator III and a boiler water preheater; the present invention uses the superheated steam produced by the incineration flue gas to gasify the water and organic waste liquid in the carbon black, reduces the load of the incinerator, greatly reduces the consumption of supplementary fuel, and improves the economic efficiency of the equipment investment and operation of the incineration device.

Description

Technical Field

[0001] The present invention relates to the technical fields of fine chemical industry and natural gas chemical industry, and particularly relates to an efficient, economical and reliable carbon black incineration process method which, according to the characteristics of carbon black produced from natural gas to acetylene, utilizes the superheated steam self-produced by carbon black incineration to evaporate the water and organic waste gas in the carbon black, burns the dry carbon black and the evaporated organic waste gas at different parts of the incinerator, greatly reduces the consumption of auxiliary fuel, and fully utilizes the incineration heat energy of the self-produced superheated steam. Background Art

[0002] The carbon black produced from natural gas to acetylene contains a large amount of water and adsorbs a small amount of organic (partially toxic) gases. Generally, it cannot be treated and reused, and it is a toxic and harmful waste liquid (including solid carbon black and organic toxic gases). Incineration is the most effective means for chemical plants to treat toxic and harmful wastes. Incineration treatment technology requires that the high-temperature gas generated by the incineration reaction must be quickly cooled (quenched) to avoid the occurrence of incineration reverse reactions and side reactions. The carbon black incineration reaction is an oxidation reaction at high temperatures. The method of using a waste heat boiler to quickly cool and by-product steam is adopted to improve the economic efficiency of the incineration device. In the existing incineration methods, liquid waste is directly fed into the furnace for incineration. Since the water content of the waste liquid is as high as 97%, a large amount of fuel is required to gasify the water in the waste liquid and raise it to the incineration temperature, resulting in a large fuel consumption and uneconomical operation of the device; due to the large water content of the waste, the flue gas volume is large after incineration. Therefore, the existing incinerators are relatively large in size and require a large equipment investment; most of the existing incinerators use cyclone incinerators with high incineration intensity. Due to the large flue gas volume, the incinerator is already very large in size, but its incineration time is very short, even less than 1 second, resulting in poor incineration effect; at the same time, since the carbon black has been vitrified, a long residence time is required for complete incineration. Therefore, the existing incinerators have high fuel consumption, high equipment investment, incomplete incineration and poor effect. Summary of the Invention

[0003] The object of the present invention is to provide a new process for carbon black incineration. By using the present invention, the superheated steam produced from the incineration flue gas is mixed and heat-exchanged with the carbon black fed after pressure filtration in a drying separator to dry the carbon black and vaporize the moisture in the carbon black. At the same time, the organic (partially toxic) gases adsorbed in the carbon black are evaporated, and gas-solid separation is carried out. The separated gas enters the second-stage incinerator for incineration. The separated solid carbon black (in a relatively small amount) is transported into the low-temperature section (1200 °C) of the first-stage incinerator for incineration by the superheated steam produced from the incineration flue gas, then enters the high-temperature section (1300 °C) of the first-stage incinerator for incineration, and then enters the second-stage incinerator (1200 °C) for incineration together with the waste gas. Auxiliary fuel burners are arranged at the inlet of the first-stage incinerator, the end of the low-temperature section of the first-stage incinerator, and the inlet section of the second-stage incinerator to maintain the incineration temperature of each section. After the incineration flue gas exits the second-stage incinerator, it sequentially enters the incinerator heat recovery section composed of Evaporator I, Evaporator II, Steam Superheater I, Steam Superheater II, Evaporator III, and Boiler Feed Water Preheater to recover the sensible heat in the incineration flue gas. The flue gas is reduced to below 150 °C and discharged to the chimney through an induced draft fan. The incinerator adopts a first-stage and second-stage return-type cyclone incinerator. This incineration process method has a small amount of solids, can achieve a long residence time under the condition of a small equipment size, and has a high incineration temperature, which can completely incinerate the carbon black. At the same time, the waste entering the incinerator has a small water content, which can greatly reduce the consumption of auxiliary fuel. That is, on the basis of ensuring the efficient incineration of carbon black, the investment cost of the equipment and the operation cost of the device are greatly reduced. The present invention is particularly suitable for the incineration of solid-containing waste liquids with a large water content and a long solid incineration time.

[0004] In order to achieve the above object, the present invention adopts the following technical solutions:

[0005] A process for carbon black incineration, comprising the following steps:

[0006] S1: Set up a drying separator, a first-stage incinerator, a second-stage incinerator, an incinerator heat recovery section, a steam drum, an induced draft fan, and a chimney; install Burner I, Burner II, and Burner III at the front end, middle part of the first-stage incinerator, and the front end of the second-stage incinerator respectively; the incinerator heat recovery section includes Evaporator I, Evaporator II, Steam Superheater I, Steam Superheater II, Evaporator III, and Boiler Water Preheater;

[0007] S2: Establish a negative pressure through the induced draft fan and operate under negative pressure;

[0008] S3: Supplementary fuel enters through Burner I, Burner II, and Burner III. After burning in the burner, the flue gas tangentially enters the incinerator;

[0009] S4: The carbon black that has been pressure-filtered from the outside of the boundary enters the drying separator, and the superheated steam generated by Steam Superheater I is introduced into the drying separator for heat exchange and drying, and is separated into two streams of gas and solid in the drying separator;

[0010] S5: The dry carbon black output from the dry separator is pneumatically conveyed by the superheated steam generated by the steam superheater I. The pneumatically conveyed dry carbon black tangentially enters the burner I from the front end of the first-stage incinerator, is heated to the incineration temperature and then enters the front section of the first-stage incinerator, where it is mixed with the flue gas in a swirling manner for incineration.

[0011] S6: Superheated steam is tangentially supplemented in the middle of the first-stage incinerator. At the same time, fuel gas is burned through the burner II, and the burned flue gas tangentially enters the incinerator.

[0012] S7: The flue gas leaving the first-stage incinerator turns back and tangentially enters the second-stage incinerator.

[0013] S8: The waste gas leaving the dry separator tangentially enters from the front end of the second-stage incinerator and continues to burn with the incineration flue gas coming from the first-stage incinerator in the second-stage incinerator. The completely burned flue gas enters the heat recovery section of the incinerator. The incineration temperature of the second-stage incinerator is maintained by the burner III, and the flue gas after fuel combustion tangentially enters the second-stage incinerator.

[0014] S9: The incineration flue gas entering the heat recovery section of the incinerator horizontally flows through the evaporator I, evaporator II, steam superheater I, steam superheater II, and evaporator III in sequence.

[0015] S10: The incineration flue gas leaving the evaporator III turns downward and passes through the boiler water preheater to further cool the flue gas to 150 °C.

[0016] S11: The 150 °C flue gas leaving the heat recovery section of the incinerator is discharged to the chimney through the induced draft fan.

[0017] S12: The boiler water from outside the plant is preheated by the boiler water preheater and then enters the steam drum, where it is saturated.

[0018] S13: The saturated water in the steam drum enters the evaporator I, evaporator II, and evaporator III respectively through their respective downcomers. The steam-water mixture generated by the evaporators enters the steam drum through their respective risers for steam-water separation.

[0019] S14: Part of the saturated steam leaving the steam drum is superheated by the steam superheater II and then merged into the steam pipeline for external transmission; part of it is superheated by the steam superheater I and then used as the heat source of the dry separator, the conveying gas of the dry carbon black, and the loosening gas for the feeding and conveying process of the dry carbon black.

[0020] Preferably, in S4, the carbon black from outside the plant after pressure filtration contains water, organic substances, and organic waste gas, and part of the organic substances and organic waste gas are toxic.

[0021] Preferably, in S4, among the two materials of gas and solid, the solid is dry carbon black; the gas is waste gas.

[0022] Preferably, in S1, the inner walls of the primary incinerator and the secondary incinerator are lined according to the requirements of the medium temperature.

[0023] Preferably, in S5, the incineration temperature at the front of the primary incinerator is 1200 °C.

[0024] Preferably, in S5, the incineration temperature at the rear of the primary incinerator is 1300 °C.

[0025] Preferably, in S7, the incineration temperature of the secondary incinerator is 1200 °C.

[0026] Preferably, in S8, the waste gas enters the incinerator from the secondary incinerator, and the co-current time is greater than 3 seconds.

[0027] Preferably, in S2, a single induced draft fan is configured, and the combustion air and the air distribution are naturally sucked in.

[0028] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0029] The solid-containing waste liquid is heated, dried, and gas-solid separated by mixing with superheated steam, and the relatively small amount of carbon black that has been partially vitrified is separated. A cyclone incinerator with good incineration intensity and incineration effect is adopted. By lengthening the length of the incinerator and making the flue gas turn back, the residence time of carbon black incineration is greatly extended. At the same time, the method of high-temperature continuous three-chamber incineration is adopted, so that the problem of carbon black incineration that is difficult to incinerate completely and has extremely high fuel consumption is well solved.

[0030] The process flow is simple. Natural circulation is adopted between the steam drum and the evaporator. The equipment layout and piping are highly integrated. The investment is low, the floor area is saved, the process is safe and reliable, and there are no dangerous processes and equipment.

[0031] Water and steam adopt natural circulation, reducing the operation cost of the incineration device.

[0032] The present invention uses the superheated steam produced by the incineration flue gas to gasify the water and organic waste liquid in the carbon black, reducing the load of the incinerator, greatly reducing the amount of supplementary fuel used, and improving the economic efficiency of the incineration device equipment investment and device operation. Brief Description of the Drawings

[0033] Figure 1 It is a schematic diagram of the process implementation example of a carbon black incineration process method proposed by the present invention. Detailed Embodiments

[0034] The technical solutions in the embodiments of the present invention will be clearly and completely described below. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments.

[0035] Embodiment 1

[0036] Refer to Figure 1 , a carbon black incineration process method, comprising the following steps:

[0037] S1: Set up a drying separator, a first-stage incinerator, a second-stage incinerator, an incinerator heat recovery section, a gas drum, an induced draft fan and a chimney; install burner I, burner II and burner III at the front end, middle part of the first-stage incinerator and the front end of the second-stage incinerator respectively; the incinerator heat recovery section includes evaporator I, evaporator II, steam superheater I, steam superheater II, evaporator III, and boiler water preheater;

[0038] S2: Establish a negative pressure through the induced draft fan and operate under negative pressure;

[0039] S3: Supplementary fuel enters through burner I, burner II and burner III. After burning in the burner, the flue gas tangentially enters the incinerator;

[0040] S4: The carbon black that has been filtered by pressure from the outside world enters the drying separator, and the superheated steam generated by steam superheater I is introduced into the drying separator for heat exchange drying, and the drying separator separates into two streams of gas and solid materials;

[0041] S5: The dry carbon black output from the drying separator is pneumatically conveyed by the superheated steam generated by steam superheater I, and the pneumatically conveyed dry carbon black tangentially enters burner I from the front end of the first-stage incinerator, and after being heated to the incineration temperature, it enters the front section of the first-stage incinerator and is swirled and mixed with the flue gas for incineration;

[0042] S6: Supplementary superheated steam is tangentially added in the middle of the first-stage incinerator, and at the same time, fuel gas is burned through burner II, and the burned flue gas tangentially enters the incinerator;

[0043] S7: The flue gas exiting the first-stage incinerator turns back and tangentially enters the second-stage incinerator;

[0044] S8: The waste gas exiting the drying separator tangentially enters from the front end of the second-stage incinerator, and continues to burn with the incineration flue gas from the first-stage incinerator in the second-stage incinerator. After complete incineration, the flue gas enters the incinerator heat recovery section; the incineration temperature of the second-stage incinerator is maintained by burner III, and the flue gas after fuel combustion tangentially enters the second-stage incinerator;

[0045] S9: The incineration flue gas entering the incinerator heat recovery section sequentially flows horizontally through evaporator I, evaporator II, steam superheater I, steam superheater II, and evaporator III;

[0046] S10: The incineration flue gas exiting evaporator III turns downward and passes through the boiler water preheater to continue cooling the flue gas to 150 °C;

[0047] S11: The 150°C flue gas from the heat recovery section of the incinerator is discharged to the chimney through an induced draft fan.

[0048] S12: The boiler water from outside the plant is preheated by a boiler water preheater and then enters the steam drum, where it is saturated.

[0049] S13: The saturated water in the steam drum enters Evaporator I, Evaporator II, and Evaporator III through their respective downcomers. The steam-water mixtures generated by the evaporators enter the steam drum through their respective risers for steam-water separation.

[0050] S14: A part of the saturated steam leaving the steam drum is superheated by Superheater II and then merged into the steam pipe network for external transportation; a part is superheated by Superheater I and then used as the heat source for the drying separator, the conveying gas for dry carbon black, and the loosening gas for the feeding and conveying process of dry carbon black.

[0051] In this embodiment, in S4, the carbon black coming from outside the plant after pressure filtration contains water, organic substances, and organic waste gases, and some of the organic substances and organic waste gases are toxic.

[0052] In this embodiment, in S4, among the gas and solid materials, the solid is dry carbon black; the gas is waste gas.

[0053] In this embodiment, in S1, the inner walls of the primary incinerator and the secondary incinerator are lined according to the requirements of the medium temperature.

[0054] In this embodiment, in S5, the incineration temperature at the front of the primary incinerator is 1200°C.

[0055] In this embodiment, in S5, the incineration temperature at the rear of the primary incinerator is 1300°C.

[0056] In this embodiment, in S7, the incineration temperature of the secondary incinerator is 1200°C.

[0057] In this embodiment, in S8, the waste gas enters the incineration from the secondary incinerator, and the residence time is greater than 3 seconds.

[0058] In this embodiment, in S2, a single induced draft fan is configured, and the combustion air and the air distribution are naturally inhaled.

[0059] Embodiment Two

[0060] Refer to Figure 1 , a carbon black incineration process method, including the following steps:

[0061] S1: Set up a drying separator, a first-stage and a second-stage reverse-flow cyclone incinerator (the first-stage incinerator, the second-stage incinerator), the heat recovery section of the incinerator (with Evaporator I, Evaporator II, Steam Superheater I, Steam Superheater II, Evaporator III and Boiler Water Preheater installed), a steam drum, an induced draft fan, a chimney, etc.;

[0062] S2: The system operates under slightly negative pressure, and the negative pressure is established by the induced draft fan;

[0063] S3: The supplementary fuel enters through Burner I, Burner II and Burner III installed at the front end, middle of the first-stage incinerator and the front end of the second-stage incinerator. After burning in the burners, the flue gas tangentially enters the incinerator, which is used for heating up during the start-up of the incinerator and ensuring safe operation and providing auxiliary heat to maintain the set incineration temperature during normal operation;

[0064] S4: The carbon black (containing about 50% water and organic gases, and some organic gases are toxic) filtered by pressure from outside the plant enters the drying separator, where it is mixed and heat-exchanged with the self-produced superheated steam I in the incinerator for drying, and then separated into two streams of gas and solid in the drying separator - waste gas and dry carbon black (the gas contains water vapor and organic gases, and some organic gases are toxic, this stream of gas is simply called waste gas; the solid is the dried carbon black, simply called dry carbon black);

[0065] S5: The dry carbon black pneumatically conveyed out of the drying separator by the self-produced superheated steam I in the incinerator tangentially enters the front section of the first-stage incinerator heated to the incineration temperature by the auxiliary fuel burner I from the front end of the first-stage incinerator, and swirls and mixes with the flue gas for incineration; the flue gas after the combustion of Burner I tangentially enters the incinerator;

[0066] S6: Superheated steam I is tangentially supplemented in the middle of the first-stage incinerator. At the same time, fuel gas is burned through Burner II, and the flue gas after combustion tangentially enters the incinerator to increase the incineration temperature and enhance the swirl mixing, so that the carbon black continues to burn more violently in the rear section of the first-stage incinerator;

[0067] S7: The flue gas (containing unburned dry carbon black) coming out of the first-stage incinerator returns and enters the second-stage incinerator;

[0068] S8: The waste gas coming out of the drying separator tangentially enters from the front end of the second-stage incinerator, and continues to burn in the second-stage incinerator with the incineration flue gas (containing unburned dry carbon black) coming from the first-stage incinerator. After complete incineration, the flue gas enters the heat recovery section of the incinerator; the incineration temperature of the second-stage incinerator is maintained by the auxiliary fuel burner III installed at the front end of the second-stage incinerator, and the flue gas after the combustion of the auxiliary fuel tangentially enters the second-stage incinerator to enhance the swirl mixing in the incinerator;

[0069] S9: The incineration flue gas entering the heat recovery section sequentially enters Evaporator I, Evaporator II, Steam Superheater I, Steam Superheater II, Evaporator III, and Boiler Feedwater Preheater to cool down the flue gas and recover the sensible heat in the incineration flue gas.

[0070] S10: The flue gas leaving the heat recovery section of the incinerator is discharged to the chimney through an induced draft fan.

[0071] S11: The boiler water from outside the plant is preheated by the Boiler Feedwater Preheater and then enters the steam drum, where it is saturated.

[0072] S12: The saturated water in the steam drum enters Evaporator I, Evaporator II, and Evaporator III respectively through their respective downcomers. The steam-water mixtures generated by the evaporators enter the steam drum through their respective risers for steam-water separation.

[0073] S13: A part of the saturated steam leaving the steam drum is superheated by Steam Superheater II and then merged into the steam pipe network for external transmission; a part is superheated by Steam Superheater I and then serves as the heat source for the drying separator, the conveying gas for dry carbon black, and the loosening gas for the feeding and conveying process of dry carbon black.

[0074] S14: The incinerator adopts a folded-flow cyclone first and second-stage three-chamber incinerator for strong incineration.

[0075] S15: The (solid-containing) waste liquid to be incinerated is dried and separated into waste solids and waste gas, which are respectively fed into the chambers for incineration.

[0076] S16: High-temperature incineration is carried out to ensure complete incineration. The temperatures of the three incineration chambers are 1200 °C, 1300 °C, and 1200 °C in sequence.

[0077] S17: The carbon black is continuously incinerated in the first, second, and third chambers with an extremely long incineration time, and the total time is greater than 6 seconds.

[0078] Example Three

[0079] Reference Figure 1 , a carbon black incineration process method, comprising the following steps:

[0080] S1: The system establishes a negative pressure through an induced draft fan, and the entire system operates under negative pressure.

[0081] S2: The supplementary fuel enters through Burner I, Burner II, and Burner III installed at the front end of the first-stage incinerator, the middle part, and the front end of the second-stage incinerator. After burning in the burners, the flue gas tangentially enters the incinerator, which is used to raise the temperature during the start-up of the incinerator and ensure safe operation and provide auxiliary heat to maintain the set incineration temperature during normal operation.

[0082] S3: The filtered carbon black from outside the plant (containing about 50% water and organic gases, and some of the organic gases are toxic) enters the drying separator, where it is mixed and heat-exchanged with the superheated steam I produced by the incinerator for drying, and then separated into two streams of gas and solid in the drying separator - waste gas and dry carbon black (the gas contains water vapor and organic gases, and some of the organic gases are toxic, and this stream of gas is simply referred to as waste gas; the solid is the dried carbon black, simply referred to as dry carbon black);

[0083] S4: The dry carbon black pneumatically conveyed out of the drying separator by the superheated steam I produced by the incinerator enters the front section of the first-stage incinerator from the tangential direction at the front end of the first-stage incinerator, and is heated to the incineration temperature in the auxiliary fuel burner I and then mixed and incinerated with the flue gas in a swirling manner;

[0084] S5: Superheated steam I is tangentially supplemented in the middle of the first-stage incinerator. At the same time, fuel gas is burned through burner II, and the burned flue gas enters the incinerator tangentially to increase the incineration temperature and enhance the swirling mixing, so that the carbon black continues to burn more violently in the rear section of the first-stage incinerator;

[0085] S6: The flue gas (containing unburned dry carbon black) exiting the first-stage incinerator turns back and enters the second-stage incinerator tangentially;

[0086] S7: The waste gas exiting the drying separator enters tangentially from the front end of the second-stage incinerator and continues to burn in the second-stage incinerator with the incineration flue gas (containing unburned dry carbon black) coming from the first-stage incinerator. After complete incineration, the flue gas enters the heat recovery section of the incinerator; the incineration temperature of the second-stage incinerator is maintained by the auxiliary fuel burner III installed at the front end of the second-stage incinerator, and the flue gas after combustion of the auxiliary fuel enters the second-stage incinerator tangentially to enhance the swirling mixing in the incinerator;

[0087] S8: The incineration flue gas entering the heat recovery section flows horizontally through the evaporator I, evaporator II, steam superheater I, steam superheater II, and evaporator III in sequence to cool the flue gas and recover the sensible heat in the incineration flue gas;

[0088] S9: The incineration flue gas exiting the evaporator III turns downward and passes through the boiler feed water preheater to further cool the flue gas to 150 °C and recover more heat in the incineration flue gas;

[0089] S10: The 150 °C flue gas exiting the heat recovery section of the incinerator is discharged to the chimney through the induced draft fan.

[0090] S11: The boiler water from outside the plant is preheated by the boiler feed water preheater and then enters the steam drum, where it is saturated;

[0091] S12: The saturated water in the steam drum enters the evaporator I, evaporator II, and evaporator III respectively through their respective downcomers, and the steam-water mixtures generated by the evaporators enter the steam drum through their respective risers for steam-water separation;

[0092] S13: Part of the saturated steam in the steam drum is superheated by the steam superheater II and then merged into the steam pipe network for external transportation; part of it is superheated by the steam superheater I and then used as the heat source of the drying separator, the conveying gas for dry carbon black, and the loosening gas during the feeding and conveying process of dry carbon black.

[0093] As mentioned above, it is only the preferred specific implementation mode of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention, according to the technical solution and inventive concept of the present invention, makes equivalent replacements or changes, and all should be covered within the protection scope of the present invention.

Claims

1. A carbon black incineration process method, characterized in that, It includes the following steps: S1: Set up a drying separator, a primary incinerator, a secondary incinerator, a heat recovery section of the incinerator, a steam drum, an induced draft fan, and a chimney; install Burner I, Burner II, and Burner III at the front end, middle of the primary incinerator, and the front end of the secondary incinerator respectively; the heat recovery section of the incinerator includes Evaporator I, Evaporator II, Steam Superheater I, Steam Superheater II, Evaporator III, and Boiler Water Preheater; S2: Establish a negative pressure through the induced draft fan and operate under negative pressure; S3: Supplementary fuel enters through Burner I, Burner II, and Burner III. After combustion in the burners, the flue gas tangentially enters the incinerator; S4: The carbon black that has been pressure-filtered from outside the plant enters the drying separator, and superheated steam generated by Steam Superheater I is introduced into the drying separator for heat exchange and drying, and is separated into two streams of gas and solid in the drying separator; S5: The dry carbon black output from the drying separator is pneumatically conveyed by the superheated steam generated by Steam Superheater I. The pneumatically conveyed dry carbon black tangentially enters Burner I from the front end of the primary incinerator, is heated to the incineration temperature and then enters the front section of the primary incinerator, and swirls and mixes with the flue gas for incineration; S6: Superheated steam is tangentially supplemented in the middle of the primary incinerator, and at the same time, fuel gas is burned through Burner II, and the burned flue gas tangentially enters the incinerator; S7: The flue gas exiting the primary incinerator turns back and tangentially enters the secondary incinerator; S8: The waste gas exiting the drying separator tangentially enters from the front end of the secondary incinerator, continues to burn with the incineration flue gas from the primary incinerator in the secondary incinerator, and the completely burned flue gas enters the heat recovery section of the incinerator; the incineration temperature of the secondary incinerator is maintained by Burner III, and the flue gas after fuel combustion tangentially enters the secondary incinerator; S9: The incineration flue gas entering the heat recovery section of the incinerator sequentially flows horizontally through Evaporator I, Evaporator II, Steam Superheater I, Steam Superheater II, and Evaporator III; S10: The incineration flue gas exiting Evaporator III turns downward and passes through the boiler water preheater to continue cooling the flue gas to 150 °C; S11: The 150 °C flue gas exiting the heat recovery section of the incinerator is discharged to the chimney through the induced draft fan; S12: The boiler water from outside the plant is preheated by the boiler water preheater and then enters the steam drum, where it is saturated; S13: The saturated water in the steam drum respectively enters Evaporator I, Evaporator II, and Evaporator III through their respective downcomers, and the steam-water mixture generated by the evaporators respectively enters the steam drum through their respective risers for steam-water separation; S14: A part of the saturated steam exiting the steam drum is superheated by Steam Superheater II and then merged into the steam pipe network for external transmission; a part is superheated by Steam Superheater I and then used as the heat source of the drying separator, the conveying gas for dry carbon black, and the loosening gas during the feeding and conveying process of dry carbon black.

2. The method for carbon black incineration process according to claim 1, wherein, In S4, the carbon black that has been pressure-filtered from outside the plant contains water, organic substances, and organic waste gases, and some of the organic substances and organic waste gases are toxic.

3. A carbon black incineration process method according to claim 1, characterized in that, In S4, among the two streams of gas and solid, the solid is dry carbon black; the gas is waste gas.

4. A method for carbon black incineration process according to claim 1, wherein, In S1, the inner walls of the primary incinerator and the secondary incinerator are lined according to the requirements of the medium temperature.

5. A carbon black incineration process method according to claim 1, characterized in that, In S5, the front part of the first-stage incinerator has an incineration temperature of 1200 °C.

6. A carbon black incineration process method according to claim 1, characterized in that, In S5, the rear part of the first-stage incinerator has an incineration temperature of 1300 °C.

7. A carbon black incineration process method according to claim 1, characterized in that, In S7, the second-stage incinerator has an incineration temperature of 1200 °C.

8. A carbon black incineration process method according to claim 1, characterized in that, In S8, the waste gas enters the incinerator from the second-stage incinerator, and the co-flow time is more than 3 seconds.

9. A carbon black incineration process method according to claim 1, characterized in that, In S2, a single induced draft fan is configured, and the combustion air and air distribution are naturally inhaled.

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