Industrial kiln gas and sludge dewatering co-processing apparatus and method

Abstract

The application discloses an industrial kiln gas and sludge dewatering collaborative treatment device and method, which adopts a cationic polymer flocculant with carbon dioxide and a temperature response group to flocculate sludge, and industrial kiln gas with high-concentration carbon dioxide, dust and waste heat is introduced into the flocculated sludge in the stirring and flocculation process, so that the industrial kiln gas and the flocculated sludge are fully contacted, and the cooling and dust removal pretreatment of the industrial kiln gas are simultaneously realized. The application realizes the collaborative implementation of the pretreatment of the industrial kiln gas and the flocculated sludge dewatering, in the industrial kiln gas reinforced sludge flocculation conditioning process, the industrial kiln gas passes through the flocculated sludge, and the cooling and dust removal are realized; meanwhile, the responsive polymer flocculant can respond to the carbon dioxide and heat in the industrial kiln gas, is changed from a linear molecule into a network molecule, so that the adsorption and flocculation performance is improved, and the dust in the kiln gas enters the sludge, so that the dust can play a supporting role in the further sludge squeezing and dewatering process, and the dewatering efficiency of the subsequent membrane pressure filtration is improved.

Description

Technical Field

[0001] This invention relates to the field of industrial kiln gas and sludge treatment, and more specifically to a device and method for the co-treatment of industrial kiln gas and sludge dewatering. Background Technology

[0002] With the rapid urbanization and improved living standards worldwide, urban wastewater treatment has developed rapidly. As a result, the amount of urban sludge, a byproduct of wastewater treatment, is also increasing. If this large accumulation of sludge is not properly treated, it will cause secondary pollution to the environment, becoming a major public nuisance affecting urban sanitation. Using industrial kilns such as rotary kilns and cement kilns for sludge incineration or co-processing is a major approach to sludge disposal and even resource utilization. However, this requires deep dewatering of the sludge. Currently, deep dewatering processes and systems generally involve first flocculating sludge with a moisture content of over 98%, then concentrating the sludge using a belt filter or belt filter press. Water is then added to adjust the sludge's moisture content, and inorganic additives such as quicklime, iron salts, or fly ash are added for conditioning. The conditioned sludge is then dewatered to a moisture content of below 60% by pressing it through a diaphragm plate and frame filter press. However, the sludge thickening process is complex and requires relatively large investments. It also significantly increases the amount of oven-dried sludge. Furthermore, the chloride ions carried by the added inorganic salts entering the dewatered sludge have a great impact on the normal operation of industrial kilns.

[0003] On the other hand, the operation of industrial kilns generates a large amount of industrial kiln gas, which needs to be dust-removed, cooled, and desulfurized before being discharged into the atmosphere. In the kiln flue gas treatment industry, wet desulfurization technology is currently the most mature and engineered treatment technology. In a wet desulfurization system, an alkaline solution meets the flue gas in a spray tower. Sulfur oxides in the flue gas dissolve in water and then neutralize with the alkaline substances dissolved in the water, thereby removing sulfur oxides from the flue gas. However, kiln flue gas often contains a large amount of dust. As the flue gas enters the desulfurization device, it easily coats the dust and accumulates on the packing and demister of the desulfurization device, causing great trouble for the use and maintenance of the desulfurization device. At best, it increases resistance and requires frequent adjustments; at worst, it causes blockage of the packing layer and demister of the desulfurization device, affecting the desulfurization efficiency of the flue gas. Therefore, it is necessary to remove dust and other pollutants from the flue gas before it enters the desulfurization device and to appropriately cool the flue gas to facilitate subsequent desulfurization treatment.

[0004] By utilizing high molecular weight CO2 and temperature-responsive cationic polymeric flocculants to flocculate sludge, and using the abundant CO2 and waste heat in industrial kiln gas as stimuli to enhance the sludge flocculation process, this method not only achieves pretreatment such as cooling and dust removal of industrial kiln gas, but also utilizes the heat and CO2 in the kiln gas to enhance flocculation stimulation. This enables the synergistic implementation of industrial kiln gas pretreatment and deep sludge dewatering, achieving the goal of treating waste with waste. Summary of the Invention

[0005] To achieve the above objectives, the present invention provides a device and method for the synergistic treatment of industrial kiln gas and sludge dewatering, with a temperature- and CO2-responsive cationic polymeric flocculant as the core. The device uses a cationic polymeric flocculant with carbon dioxide-related groups to flocculate the sludge. During the flocculation process, industrial kiln gas with high concentrations of carbon dioxide, dust, and waste heat is introduced into the flocculated sludge, thereby achieving the synergistic implementation of industrial kiln gas treatment and deep sludge flocculation dewatering.

[0006] This invention is implemented as follows: an industrial kiln gas and sludge dewatering co-treatment device, characterized in that the industrial kiln gas and sludge dewatering co-treatment device consists of three parts: an industrial kiln gas enhanced sludge flocculation conditioning system A; a sludge deep dewatering system B; and an industrial kiln gas desulfurization system C. The sludge is flocculated using a cationic polymeric flocculant with carbon dioxide and temperature-responsive groups. During the stirring and flocculation process, industrial kiln gas containing high concentrations of carbon dioxide, dust, and waste heat is introduced into the flocculated sludge to ensure full contact between the industrial kiln gas and the flocculated sludge, thereby enhancing the sludge flocculation conditioning and simultaneously achieving cooling and dust removal pretreatment of the industrial kiln gas. The enhanced flocculated sludge undergoes further pre-dewatering and diaphragm filtration dewatering to achieve deep dewatering, and the industrial kiln gas is further treated by desulfurization before being discharged.

[0007] Furthermore, the industrial kiln gas enhanced sludge flocculation and conditioning system A includes a flocculant dissolving tank and a sludge flocculation and conditioning tank. The flocculant dissolving tank is equipped with a stirring device. The flocculant solution is pumped into the sludge pipeline by the flocculant dosing pump and mixed with the sludge before entering the sludge flocculation and conditioning tank. The sludge flocculation and conditioning tank includes a sludge stirring device and a kiln gas distribution device.

[0008] Furthermore, the sludge deep dewatering system B includes a pre-dewatering belt, a pre-dewatering sludge storage tank, a sludge screw pump, a diaphragm filter press, a clean water tank, a press pump, and a dewatered sludge conveyor belt. The output end of the pre-dewatering belt corresponds to the pre-dewatering sludge storage tank, and the output end of the pre-dewatering sludge storage tank is connected to the diaphragm filter press via the sludge screw pump. A dewatered sludge conveyor belt is installed below the diaphragm filter press, and the clean water tank is connected to the diaphragm filter press.

[0009] Furthermore, the industrial kiln gas desulfurization system C includes a desulfurization tower, a desulfurization liquid storage tank, a desulfurization liquid pump, and a fan. The desulfurization tower includes a desulfurization spray device, a bubbling tower plate, and a kiln gas distributor. The desulfurization liquid storage tank is connected to the desulfurization spray device inside the desulfurization tower. The top of the desulfurization tower is connected to a fan. The interior of the desulfurization tower has a bubbling tower plate and a kiln gas distributor.

[0010] Furthermore, the cationic monomer of the cationic polymeric flocculant used is one or more of the following: diallyl dimethyl ammonium chloride (DMDAAC), methacryloyloxyethyl trimethyl ammonium chloride (DMC), acryloyloxyethyl trimethyl ammonium chloride (DAC), and methacrylamide propyl trimethyl ammonium chloride (MAPTAC).

[0011] Furthermore, the carbon dioxide and temperature-responsive monomers of the cationic polymeric flocculant used are one or more of the following: dimethylaminoethyl methacrylate (DMAEMA), dimethylaminoethyl acrylate (DMAEA), dimethylaminopropyl methacrylamide (DMAPMA), and dimethylaminopropyl acrylamide (DMAPAA).

[0012] Furthermore, in the cationic polymeric flocculant used, the molar proportion of cationic monomers to total monomers is 5%-50%, and the molar proportion of carbon dioxide and temperature-responsive monomers to total monomers is 10%-50%.

[0013] A method for co-treating industrial kiln gas and sludge dewatering includes an enhanced flocculation operation of industrial kiln gas; dissolving a responsive flocculant in a flocculant dissolving tank; extracting sludge from a sludge storage tank and adding the flocculant solution into the sludge inlet pipe via a flocculant dosing pump; after the sludge and flocculant solution are mixed and reacted in the pipeline, they enter the lower part of a sludge flocculation conditioning tank; under the stirring of a sludge stirring device, industrial kiln gas enters the sludge flocculation conditioning tank via a kiln gas distribution device located at the bottom of the sludge flocculation conditioning tank through a stirring rod and reacts with the flocculated sludge to enhance flocculation performance; after the sludge stays in the sludge flocculation conditioning tank, it enters a sludge deep dewatering system B from the upper outlet of the sludge flocculation conditioning tank, and the industrial kiln gas exits from the gas outlet at the upper part of the sludge flocculation conditioning tank and enters an industrial kiln gas desulfurization system C.

[0014] The industrial kiln gas and sludge dewatering co-treatment method described in this application further includes deep dewatering of sludge after flocculation conditioning; the conditioned sludge first enters a pre-dewatering belt to filter out the filtrate, and the pre-dewatered sludge is then conveyed to a pre-dewatered sludge storage tank via the dewatering belt; the sludge screw pump is started to pump the pre-dewatered sludge from the flocculated sludge storage tank into a diaphragm filter press to begin the filter press operation; the first stage of the filter press is the process of sludge screw pump feeding and using its pressure to dewater the sludge; when the pressure in the diaphragm filter press reaches the set working filter press pressure of the sludge screw pump, the filter press is shut off. The second stage of filtration involves using a press pump to force water from the clear water tank into the diaphragm of the diaphragm filter press. The set water pressure further presses the sludge in the diaphragm filter press, and the water in the diaphragm flows back into the clear water tank after pressing. The filtrate from both stages of the diaphragm filter press flows back into the wastewater treatment system through a drainage channel into the pipeline. After a certain period of secondary pressing, the press pump is turned off, and the diaphragm filter press is turned on to discharge the sludge cake. The falling sludge cake is conveyed out of the system via a dewatered sludge conveyor belt for further co-processing in the cement kiln.

[0015] The industrial kiln gas and sludge dewatering co-treatment method described in this application also includes desulfurization of pretreated industrial kiln gas: the pretreated kiln gas enters the desulfurization tower from the bottom of the desulfurization tower through the kiln gas distributor, the desulfurization liquid pump pumps the desulfurization liquid from the desulfurization liquid storage tank to the top of the desulfurization tower, and sprays it into the desulfurization tower in a spray manner through the desulfurization spray device. The kiln gas and the desulfurization liquid react in a bubbling tower plate in a bubbling manner and in a mist manner in the upper part of the desulfurization tower to achieve desulfurization, and finally the gas is discharged into the atmosphere by the fan.

[0016] The present invention has the following advantages: The present invention discloses a method and apparatus for the synergistic treatment of industrial kiln gas and sludge dewatering, which can realize the synergistic implementation of pretreatment of industrial kiln gas and deep dewatering of sludge flocculation: In the process of industrial kiln gas-enhanced sludge flocculation conditioning, on the one hand, the industrial kiln gas achieves cooling and dust removal through the flocculation of sludge; on the other hand, since the responsive polymeric flocculant can respond to carbon dioxide and heat in the industrial kiln gas, it transforms from linear molecules to network molecules, thereby improving the adsorption and flocculation performance. At the same time, the dust in the kiln gas enters the sludge and can act as a support agent in the further sludge pressing and dewatering process, thereby improving the dewatering efficiency of subsequent diaphragm filtration. Attached Figure Description

[0017] Figure 1 This is a schematic diagram of an industrial kiln gas and sludge dewatering co-processing device;

[0018] Figure 2 Schematic diagram showing the effect of industrial kiln gas introduction on (a) settling rate, (b) turbidity, and (c) filter cake moisture content under different flocculant dosages;

[0019] Figure 3Microscopic images of flocculated sediments with and without industrial kiln gas: (a) flocculated sediments without industrial kiln gas; (b) schematic diagram of flocculated sediments with industrial kiln gas.

[0020] Figure 4 Schematic diagram showing the effect of CO2 response monomer content at different dosages on (a) sedimentation rate (b) turbidity (c) Zeta potential (d) filter cake moisture content;

[0021] Figure 5 Microscopic images of polymer flocculent precipitates with different monomer molar ratios.

[0022] The components include: 1. Flocculant dissolving tank; 2. Stirring device; 3. Flocculant solution pump; 4. Sludge flocculation conditioning tank; 5. Sludge stirring device; 6. Kiln gas distribution device; 7. Pre-dewatering belt; 8. Pre-dewatered sludge storage tank; 9. Sludge screw pump; 10. Diaphragm filter press; 11. Clean water tank; 12. Press pump; 13. Dewatered sludge conveyor belt; 14. Desulfurization tower; 15. Sulfur spray device; 16. Bubbling tower plate; 17. Kiln gas distributor; 18. Desulfurization liquid storage tank; 19. Desulfurization liquid pump; and 20. Fan. Detailed Implementation

[0023] The present invention will now be described in detail, and the technical solutions in the embodiments of the present invention will be clearly and completely described. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0024] The present invention will now be described in further detail with reference to specific embodiments. Example

[0025] An industrial kiln gas and sludge dewatering co-treatment device is disclosed, which consists of three parts: an industrial kiln gas enhanced sludge conditioning system A; a sludge deep dewatering system B; and an industrial kiln gas desulfurization system C.

[0026] like Figure 1 As shown, the industrial kiln gas enhanced sludge conditioning system A includes a flocculant dissolving tank 1 and a sludge flocculation conditioning tank 4. The flocculant dissolving tank 1 is equipped with a stirring device 2. The flocculant solution is pumped into the sludge pipeline by the flocculant dosing pump 3 and mixed with the sludge before entering the sludge flocculation conditioning tank 4. The sludge flocculation conditioning tank 4 includes a sludge stirring device 5 and a kiln gas distribution device 6.

[0027] like Figure 1 As shown, the sludge deep dewatering system B includes a pre-dewatering belt 7, a pre-dewatering sludge storage tank 8, a sludge screw pump 9, a diaphragm filter press 10, a clean water tank 11, a press pump 12, and a dewatered sludge conveyor belt 13.

[0028] like Figure 1 As shown, the industrial kiln gas desulfurization system C includes a desulfurization tower 14, a desulfurization liquid storage tank 18, a desulfurization liquid pump 19, and a blower 20. The desulfurization tower 14 includes a desulfurization spray device 15, a bubbling tower plate 16, and a kiln gas distributor 17.

[0029] The implementation of the method for co-treatment of industrial kiln gas and sludge dewatering is as follows:

[0030] The industrial kiln gas enhanced flocculation operation method includes: dissolving a responsive flocculant in a flocculant dissolving tank 1; extracting sludge from a sludge storage tank; and adding the flocculant solution into the sludge inlet pipe via a flocculant dosing pump 3. After the sludge and flocculant solution mix and react in the pipeline, they enter the lower part of a sludge flocculation conditioning tank 4. Under the stirring of a sludge stirring device 5, industrial kiln gas enters the sludge flocculation conditioning tank 4 via a stirring rod from a kiln gas distribution device 6 located at the bottom of the sludge flocculation conditioning tank 4 to react with the flocculated sludge and enhance flocculation performance. After the sludge stays in the sludge flocculation conditioning tank 4, it enters the sludge deep dewatering system B from the upper outlet of the sludge flocculation conditioning tank 4. The industrial kiln gas exits from the gas outlet at the upper part of the sludge flocculation conditioning tank 4 and enters the industrial kiln gas desulfurization system C.

[0031] The deep dewatering method for sludge includes: the conditioned sludge first enters the pre-dewatering belt 7, filters out the filtrate, and the pre-dewatered sludge is conveyed into the pre-dewatered sludge storage tank 8 via the dewatering belt 7; the sludge screw pump 9 is turned on to pump the pre-dewatered sludge from the flocculated sludge storage tank 8 into the diaphragm filter press 10 to start the filter press operation; the first stage of filter press is the process of sludge entering the sludge screw pump 9 and using its pressure to filter and dewater the sludge, and when the pressure in the diaphragm filter press 10 reaches the set working filter press pressure of the sludge screw pump 9, the sludge screw pump 9 is turned off; the second stage of filter press is to use the pressing pump 12 to press water from the clear water tank 11 into the diaphragm of the diaphragm filter press 10, and use the set water pressure to further press the sludge in the diaphragm filter press 10, and the water in the diaphragm after pressing flows back into the clear water tank. The filtrate from both stages of the diaphragm filter press 10 flows back to the wastewater treatment system through a diversion channel into the pipeline. After a certain period of secondary pressing, the press pump 12 is turned off, and the diaphragm filter press 10 is turned on to discharge the sludge cake. The falling sludge cake is transported out of the system via the dewatered sludge conveyor belt 13 for further co-processing in the cement kiln.

[0032] The pretreated industrial kiln gas desulfurization method is as follows: the pretreated kiln gas enters the desulfurization tower 14 from the bottom of the desulfurization tower 14 through the kiln gas distributor 17. The desulfurization liquid pump 19 pumps the desulfurization liquid from the desulfurization liquid storage tank 18 to the top of the desulfurization tower 14, and sprays it into the desulfurization tower 14 in a spray manner through the desulfurization spray device 15. The kiln gas and the desulfurization liquid react in a bubbling manner on the bubbling tower plate 16 and in a mist manner at the top of the desulfurization tower to achieve desulfurization. Finally, the gas is discharged into the atmosphere by the fan 20.

[0033] A polymeric flocculant product copolymerized from methacryloyloxyethyltrimethylammonium chloride (DMC) and dimethylaminoethyl methacrylate (DMAEMA) in a 1:1 molar ratio was applied to sludge flocculation. Industrial kiln gas was introduced during the flocculation process, and the results were compared with those without industrial kiln gas to investigate the effect of industrial kiln gas introduction on its flocculation performance. Figure 2 (a), (b), and (c) respectively demonstrate the relationship between the sedimentation rate, supernatant turbidity, and filter cake moisture content and the dosage of the polymeric flocculant used in the flocculation process. It can be seen that when industrial kiln gas is introduced into the sludge for flocculation, the sedimentation rate of the flocs is significantly higher than when no industrial kiln gas is introduced, while the supernatant turbidity and filter cake moisture content are lower. This indicates that introducing industrial kiln gas significantly improves the flocculation effect. This may be because, while the polymer binds to the particles, it reacts uniformly with carbon dioxide in the industrial kiln gas, causing the tertiary amine groups to protonate and transform into ionic hydrophilic quaternary ammonium salts. This enhances the electrostatic repulsion between polymer chains, weakening the interaction and making it easier for the polymer chains to extend and form bridges. This allows the polymer to simultaneously bind to multiple fine particles in a short time, increasing the floc volume, accelerating the sedimentation rate, and facilitating dewatering.

[0034] from Figure 3 Microscopic images of the precipitate show that the flocs are significantly larger when industrial kiln gas is introduced during the sludge flocculation process, while only small flocs are produced when industrial kiln gas is not introduced, and the structure is relatively dispersed. This is consistent with the above flocculation results, further indicating that introducing industrial kiln gas into the sludge will enable P(DMC-DMAEMA) to exert a better bridging ability and achieve better flocculation effect.

[0035] Figure 2 The effects of industrial kiln gas introduction on (a) settling rate, (b) turbidity, and (c) filter cake moisture content under different flocculant dosages. Figure 3 Microscopic images of flocculated sediments with and without industrial kiln gas: (a) flocculated sediments without industrial kiln gas; (b) flocculated sediments with industrial kiln gas.

[0036] The cationic polymeric flocculant molecules obtained by copolymerizing methacryloyloxyethyltrimethylammonium chloride (DMC) and dimethylaminoethyl methacrylate (DMAEMA) in different molar ratios are used to flocculate the sludge. Industrial kiln gas is introduced into the flocculation process to enhance flocculation. Figure 4(a), (b), (c), and (d) respectively show the relationships between the flocculant concentration, turbidity, Zeta potential, and filter cake moisture content and the dosage when the flocculant synthesized at three different monomer molar ratios is applied to the flocculation process. The figures clearly show that the sedimentation rate initially increases and then decreases with increasing dosage, and the sedimentation rate also increases with increasing DMAEMA content. Turbidity initially decreases and then increases with increasing dosage, and the higher the DMAEMA content, the lower the turbidity, resulting in a clearer supernatant. The Zeta potential increases with increasing dosage. n DMC : n DMAEMA When the ratio is 3:1, the high content of the cationic monomer DMC results in a strong electrostatic attraction to the colloidal particles, minimizing the dosage required to reach the zero potential point. n DMC : n DMAEMA =1:3 ratio n DMC : n DMAEMA When the concentration of DMAEMA is 1:1, a smaller dosage is required to reach the zero potential point. This is because when the proportion of CO2-responsive monomers is high, bridging and charge neutralization work synergistically after the industrial kiln gas is introduced, enabling the adsorption of a large number of colloidal particles. A strong charge neutralization capacity is observed even at a dosage of 36 mg / L. The moisture content of the filter cake initially decreases and then increases with increasing dosage; the higher the DMAEMA content, the lower the moisture content of the filter cake. The dehydration effect is best at a dosage of 36 mg / L. Figure 5 Microscopic images of the precipitates show that higher DMAEMA content results in larger floc volumes and denser structures, confirming the enhanced adsorption and bridging effect of the flocculant. Therefore, overall, increasing the content of the CO2-responsive monomer DMAEMA will have a positive impact on flocculation performance.

[0037] Figure 4 The effects of CO2 response monomer content at different dosages on (a) sedimentation rate, (b) turbidity, (c) zeta potential, and (d) filter cake moisture content. Figure 5 Microscopic images of polymer flocculent precipitates with different monomer molar ratios (a) n DMC : n DMAEMA =3:1; (b) n DMC : n DMAEMA =1:1; (c) n DMC : n DMAEMA =1:3.

[0038] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A device for the co-treatment of industrial kiln gas and sludge dewatering, characterized in that: The industrial kiln gas and sludge dewatering co-processing unit consists of three parts: an industrial kiln gas-enhanced sludge flocculation and conditioning system A; a sludge deep dewatering system B; and an industrial kiln gas desulfurization system C. The system uses a cationic polymeric flocculant with carbon dioxide and temperature-responsive groups to flocculate the sludge. During the agitation and flocculation process, industrial kiln gas containing high concentrations of carbon dioxide, dust, and waste heat is introduced into the flocculated sludge to ensure full contact between the industrial kiln gas and the flocculated sludge, thereby enhancing the flocculation and conditioning of the sludge and simultaneously achieving cooling and dust removal pretreatment of the industrial kiln gas. The enhanced flocculated sludge undergoes further pre-dewatering and diaphragm filtration dewatering to achieve deep dewatering, and the industrial kiln gas is further treated by desulfurization before being discharged. The cationic polymeric flocculant used has one or more of the following cationic monomers: diallyl dimethyl ammonium chloride, methacryloyloxyethyl trimethyl ammonium chloride, acryloyloxyethyl trimethyl ammonium chloride, and methacrylamidopropyl trimethyl ammonium chloride. The carbon dioxide and temperature-responsive monomers of the cationic polymeric flocculant used are one or more of the following: dimethylaminoethyl methacrylate, dimethylaminoethyl acrylate, dimethylaminopropyl methacrylamide, and dimethylaminopropyl acrylamide.

2. The industrial kiln gas and sludge dewatering co-treatment device according to claim 1, characterized in that; The industrial kiln gas enhanced sludge flocculation conditioning system A includes a flocculant dissolving tank (1) and a sludge flocculation conditioning tank (4). The flocculant dissolving tank (1) is equipped with a stirring device (2). The flocculant solution is pumped into the sludge pipeline by the flocculant dosing pump (3) and mixed with the sludge before entering the sludge flocculation conditioning tank (4). The sludge flocculation conditioning tank (4) includes a sludge stirring device (5) and a kiln gas distribution device (6).

3. The industrial kiln gas and sludge dewatering co-treatment device according to claim 1, characterized in that; The sludge deep dewatering system B includes a pre-dewatering belt (7), a pre-dewatering sludge storage tank (8), a sludge screw pump (9), a diaphragm filter press (10), a clean water tank (11), a press pump (12), and a dewatered sludge conveyor belt (13). The output end of the pre-dewatering belt (7) corresponds to the pre-dewatering sludge storage tank (8), and the output end of the pre-dewatering sludge storage tank (8) is connected to the diaphragm filter press (10) via the sludge screw pump (9). The dewatered sludge conveyor belt (13) is set below the diaphragm filter press (10), and the clean water tank (11) is connected to the diaphragm filter press (10).

4. The industrial kiln gas and sludge dewatering co-treatment device according to claim 1, characterized in that; The industrial kiln gas desulfurization system C includes a desulfurization tower (14), a desulfurization liquid storage tank (18), a desulfurization liquid pump (19), and a fan (20). The desulfurization tower (14) includes a desulfurization spray device (15), a bubbling tower plate (16), and a kiln gas distributor (17). The desulfurization liquid storage tank (18) is connected to the desulfurization spray device (15) in the inner cavity of the desulfurization tower (14). The top of the desulfurization tower (14) is connected to the fan (20). The interior of the desulfurization tower (14) has a bubbling tower plate (16) and a kiln gas distributor (17).

5. The industrial kiln gas and sludge dewatering co-treatment device according to claim 1, characterized in that, In the cationic polymeric flocculant used, the molar proportion of cationic monomers to total monomers is 5%-50%, and the molar proportion of carbon dioxide and temperature-responsive monomers to total monomers is 10%-50%.

6. A treatment method for the industrial kiln gas and sludge dewatering co-treatment device according to claim 1, characterized in that; The process includes industrial kiln gas enhanced flocculation operation; the responsive flocculant is dissolved in the flocculant dissolving tank (1), the sludge is extracted from the sludge storage tank, and the flocculant solution is added to the sludge inlet pipe through the flocculant dosing pump (3); after the sludge and flocculant solution are mixed and reacted in the pipeline, they enter the lower part of the sludge flocculation conditioning tank (4). Under the stirring of the sludge stirring device (5), the industrial kiln gas enters the sludge flocculation conditioning tank (4) through the kiln gas distribution device (6) located at the bottom of the sludge flocculation conditioning tank (4) via the stirring rod and reacts with the flocculated sludge to enhance the flocculation performance; after the sludge stays in the sludge flocculation conditioning tank (4), it enters the sludge deep dewatering system B from the upper outlet of the sludge flocculation conditioning tank (4), and the industrial kiln gas exits from the gas outlet at the upper part of the sludge flocculation conditioning tank (4) and enters the industrial kiln gas desulfurization system C.

7. The processing method according to claim 6, characterized in that; It also includes deep dewatering of sludge after flocculation conditioning; the conditioned sludge first enters the pre-dewatering belt (7), filters out the filtrate, and the pre-dewatered sludge is conveyed into the pre-dewatered sludge storage tank (8) through the dewatering belt (7); the sludge screw pump (9) is turned on to pump the pre-dewatered sludge from the flocculated sludge storage tank (8) into the diaphragm filter press (10) to start the filter press operation; the first stage of filter press is the process of sludge screw pump (9) feeding sludge and using its pressure to filter and dewater the sludge, and when the pressure in the diaphragm filter press (10) reaches the set working filter press pressure of the sludge screw pump (9), the sludge screw pump (9) is turned off; the second stage of filter press To use the press pump (12) to press water from the clear water tank (11) into the diaphragm of the diaphragm filter press (10), the sludge in the diaphragm filter press (10) is further pressed using the set water pressure. After pressing, the water in the diaphragm flows back into the clear water tank. The filtrate filtered out in the diaphragm filter press (10) in both stages enters the pipeline through the diversion channel and flows back to the sewage treatment system. After a certain period of pressing, the press pump (12) is turned off and the diaphragm filter press (10) is turned on to perform the sludge cake discharge operation. The falling sludge cake is transported out of the system by the dewatered sludge conveyor belt (13) for further cement kiln co-processing.

8. The processing method according to claim 6, characterized in that; It also includes desulfurization of pretreated industrial kiln gas: the pretreated kiln gas enters the desulfurization tower (14) from the bottom of the desulfurization tower (14) through the kiln gas distributor (17), the desulfurization liquid pump (19) pumps the desulfurization liquid from the desulfurization liquid storage tank (18) to the top of the desulfurization tower (14), and sprays it into the desulfurization tower (14) in a spray manner through the desulfurization spray device (15). The kiln gas and the desulfurization liquid react in a bubbling manner on the bubbling tower plate (16) and in a mist manner at the top of the desulfurization tower to achieve desulfurization. Finally, it is discharged into the atmosphere by the fan (20).

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