A three-phase synergistic method for integrated sludge treatment using solid, liquid, and gas phases

Abstract

This invention belongs to the field of wastewater and sludge treatment technology, and discloses a comprehensive sludge treatment method involving solid-liquid-gas three-phase synergy. The method involves mixing sludge, a conditioning agent, and a flocculant for dewatering to obtain dewatered sludge; mixing the dewatered sludge and quicklime for drying to obtain dried sludge and drying carrier gas; condensing the drying carrier gas to obtain drying carrier gas condensate, which is then subjected to ammonia stripping to obtain ammonia water; mixing the dewatered sludge and dried sludge for incineration to obtain fly ash, flue gas, and steam; purifying the flue gas to obtain purified flue gas and flue gas washing wastewater; and subjecting the flue gas washing wastewater to ammonia stripping to obtain ammonia water. This invention, through solid-liquid-gas three-phase synergy, improves the degree of sludge dewatering, saves on the treatment cost of sludge drying carrier gas condensate, reduces the emission concentration of nitrogen oxides and nitrous oxide in flue gas, improves the efficiency of waste heat recovery from sludge incineration flue gas, and achieves the recovery and utilization of ammonia nitrogen resources in wastewater.

Description

Technical Field

[0001] This invention relates to the field of wastewater and sludge treatment technology, and in particular to a three-phase synergistic method for the comprehensive treatment of sludge involving solid, liquid, and gas. Background Technology

[0002] Currently, in my country, urban sewage sludge, after dewatering, is generally dried and incinerated. The steam generated from sludge incineration is used for sludge drying, and the ash residue from sludge incineration is disposed of according to hazardous waste requirements if classified as hazardous waste, and landfilled or used as building materials if classified as general solid waste. However, in this sludge treatment process of "sludge dewatering + drying + incineration," there is a lack of a comprehensive treatment method that coordinates the three phases: solids (such as dewatered sludge, sludge incineration ash residue, etc.), liquids (such as sludge liquid including sludge drying carrier gas condensate, sludge incineration washing wastewater, etc.), and gases (such as sludge drying carrier gas, sludge incineration flue gas, etc.). This results in low resource utilization efficiency and a lack of synergistic effects between different sludge treatment process stages. Summary of the Invention

[0003] To overcome the above-mentioned technical defects, this invention provides a sludge treatment method with solid-liquid-gas three-phase synergy, which solves the problems of high water content in dewatered sludge after conventional dewatering treatment, high ammonia concentration but insufficient alkalinity in nitrification and denitrification of sludge drying carrier gas condensate, requiring additional alkalinity addition, high concentration of nitrogen oxides and greenhouse gas nitrous oxide in sludge incineration flue gas, poor waste heat utilization efficiency of sludge incineration flue gas, lack of resource utilization of sludge incineration washing wastewater, insufficient in-situ resource utilization of sludge incineration fly ash, and lack of synergy between different treatment process stages.

[0004] To achieve the above-mentioned objectives, the present invention provides the following technical solution:

[0005] This invention provides a synergistic solid-liquid-gas three-phase sludge treatment method, comprising the following steps:

[0006] S1 Dewatering: Sludge, conditioner, and flocculant are mixed and dewatered to obtain dewatered sludge;

[0007] S2 drying: The above-mentioned dewatered sludge is mixed with quicklime in a certain mass ratio and dried to obtain dried sludge and drying carrier gas.

[0008] S3 Condensation: The above-mentioned dried carrier gas is condensed to obtain dried carrier gas condensate, and then the dried carrier gas condensate is subjected to ammonia stripping treatment to obtain ammonia water 1 and the treated dried carrier gas condensate.

[0009] S4 Incineration: Dewatered sludge and dried sludge are mixed and incinerated to obtain fly ash, flue gas and steam. The obtained flue gas is then treated with ammonia water 1 obtained in S3 to obtain purified flue gas and flue gas washing wastewater. The flue gas washing wastewater is then treated with ammonia stripping to obtain ammonia water 2 and the treated flue gas washing wastewater. The ammonia water 2 obtained in this step is then mixed with ammonia water 1 obtained in S3 and flue gas again for flue gas purification. The steam obtained is recycled for drying treatment and / or ammonia stripping treatment.

[0010] Furthermore, in S1, the sludge is a dilute sludge with a moisture content of approximately 97-99%;

[0011] Furthermore, in S1, the conditioner is Fe. 2+ / S2O8 2- The system conditioner and fly ash are mixed, and Fe 2+ / S2O8 2- The dosage of the system conditioner is 0.4–2 / 0.32–1.6 mmol / g VSS of the dewatered sludge content. More preferably, the Fe... 2+ / S2O8 2- The dosage of the system conditioner is 0.8–2 / 0.6–1.6 mmol / g VSS of the dewatered sludge content. More preferably, the Fe... 2+ S2O8 2- The dosage of the system conditioning agent is 2 / 1.6 mmol / g VSS of the dewatered sludge content;

[0012] Further, in S1, the flocculant is 0.1-0.3% of the dewatered sludge mass; preferably, further, in S1, the flocculant is 0.2% of the dewatered sludge mass.

[0013] Further, the amount of fly ash used is 10-50% of the mass of the dewatered sludge; more preferably, the amount of fly ash used is 20-40% of the mass of the dewatered sludge; more preferably, the amount of fly ash used is 30% of the mass of the dewatered sludge.

[0014] Furthermore, the fly ash is fly ash obtained through incineration.

[0015] Furthermore, in S1, the flocculant is polyacrylamide (PAM);

[0016] Furthermore, in S1, the dehydration is mechanical dehydration;

[0017] Furthermore, in S2, the amount of quicklime used is 1 to 3% of the mass of the dry matter (i.e., oven-dried sludge) after all water has been removed from the sludge.

[0018] Furthermore, in S3, the dried carrier gas condensate is used for nitrification-denitrification denitrification treatment;

[0019] Furthermore, in S4, the mass ratio of the dewatered sludge to the dried sludge depends on the moisture content and calorific value of both. When the calorific value of the dried sludge is 10-15 MJ / kg, the mass ratio of the dewatered sludge to the dried sludge is approximately 1:9 to 2:3.

[0020] Furthermore, in S4, 20-40% of the volume of the purified flue gas is recycled for incineration, and the remaining purified flue gas is discharged into the atmosphere.

[0021] Furthermore, in S4, the treated flue gas washing wastewater is reused in the preparation of flocculants; beneficial effects

[0022] As can be seen from the above technical solution, compared with the prior art, the present invention has the following beneficial effects:

[0023] (1) In the sludge dewatering stage, fly ash and Fe obtained by incineration are used. 2 + / S2O8 2- This system of conditioner composites, used as sludge dewatering conditioners, improves sludge dewatering efficiency and reduces the moisture content of dewatered sludge. The conditioner possesses good porosity and mechanical strength, with its framework consisting of approximately 70% medium-diameter channels and approximately 30% small-diameter channels. The medium-diameter channels form dense Fe... 2 + / S2O8 2- The modified layer disrupts the cell structure of sludge flocs during the sludge dewatering process, allowing the bound water to be discharged from the sludge flocs through medium-diameter channels. This enhances the sludge dewatering effect, thereby achieving the goal of recycling sludge incineration fly ash and treating waste with waste.

[0024] (2) In the sludge drying stage, a small amount of quicklime is added for sludge drying. The drying heat source is steam generated from sludge incineration. The carrier gas generated from sludge drying undergoes indirect condensation treatment to reduce condensate volume and increase ammonia concentration in the condensate. The ammonia in the condensate from the drying carrier gas is stripped using steam generated from sludge incineration to form ammonia water, which is then reused at different heights in the combustion chamber of the incinerator to react with nitrogen oxides in the flue gas generated from sludge incineration, thereby reducing the emission concentration of nitrogen oxides in the flue gas. After stripping, the ammonia concentration in the condensate from the drying carrier gas is reduced, eliminating the need for additional alkalinity addition for nitrification and denitrification treatment of the condensate. This process not only recovers and utilizes ammonia nitrogen resources in the condensate from the sludge drying carrier gas, but also reduces the treatment cost of the condensate from the sludge drying carrier gas, and further reduces the emission concentration of nitrogen oxides in the flue gas.

[0025] (3) In the sludge incineration stage, based on the moisture content and calorific value of dewatered and dried sludge, they are fed into the furnace in different mass ratios to reduce the amount of sludge dried and achieve self-sustaining combustion in the incinerator. This reduces the overall amount of dewatered sludge dried and decreases the external auxiliary energy required for the sludge drying and incineration system, thereby saving on system operating costs. Furthermore, by synergizing the purified flue gas with the flue gas generated during incineration, the waste heat of the flue gas is recovered, thereby improving the waste heat utilization efficiency of sludge incineration. At the same time, the oxygen content in the incinerator is reduced, thereby reducing the emission concentrations of nitrogen oxides and nitrous oxide in the flue gas. Simultaneously, the emission of NH3 during sludge incineration is increased, promoting its redox reaction with nitrogen oxides, thereby further reducing the emission concentration of nitrogen oxides in the flue gas.

[0026] (4) In the flue gas purification stage, the flue gas generated from incineration is first washed with water and then with alkali in a wet scrubbing system. The steam generated from incineration is used in a stripping tower to recover dissolved ammonia from the wastewater and circulate it back to different heights in the combustion chamber of the incinerator. This effectively reduces nitrogen oxide emissions from the flue gas, thereby lowering the concentration of nitrogen oxides and recovering ammonia nitrogen from the wastewater. Through the synergistic effect of the stripped wastewater and the dehydration stage, the stripped wastewater is recycled for flocculant preparation in the dehydration stage. Using stripped wastewater instead of conventional tap water saves water resources and reduces the system's wastewater discharge. Attached Figure Description

[0027] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below.

[0028] Figure 1 This is a schematic diagram of the sludge comprehensive treatment method of solid-liquid-gas three-phase synergy according to the present invention.

[0029] Figure 2 For different Fe in Example 2 2+ / S2O8 2- The effect of system conditioning agent dosage on sludge capillary absorption time (CST);

[0030] Figure 3 The effect of different fly ash dosages on sludge specific resistance (SRF) and sludge moisture content in Example 3;

[0031] Figure 4 The ammonia nitrogen concentration in the effluent of Example 4;

[0032] Figure 5 This illustrates the effect of oxygen content in the first group of incinerators in Example 5 on the emission concentration of nitrogen oxides in flue gas.

[0033] Figure 6 This illustrates the effect of oxygen content in the incinerator of the second group of experiments in Example 5 on the concentration of nitrogen oxides emitted from the flue gas.

[0034] Figure 7 This illustrates the effect of oxygen content in the first group of incinerators in Example 5 on the concentration of nitrous oxide emissions in flue gas.

[0035] Figure 8 This study examines the effect of oxygen content in the incinerator of the second group of experiments in Example 5 on the emission concentration of the greenhouse gas nitrous oxide in the flue gas. Detailed Implementation

[0036] The technical solutions in the embodiments of the present invention will be clearly and completely described below. 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 of ordinary skill in the art without creative effort are within the scope of protection of the present invention.

[0037] Example 1

[0038] This embodiment provides a synergistic solid-liquid-gas three-phase sludge treatment method, the specific process of which is as follows: Figure 1 As shown, it includes the following steps:

[0039] A method for integrated sludge treatment involving solid, liquid, and gas phases includes the following steps:

[0040] S1 Dewatering: Diluted sludge, conditioner, and flocculant are mixed and mechanically dewatered to obtain dewatered sludge; wherein, the conditioner is Fe. 2+ / S2O8 2- The mixture of system conditioner and fly ash obtained from incineration, Fe 2+ / S2O8 2- The dosage of the system conditioner is 2 / 1.6 mmol / g VSS, and the dosage of fly ash is 30% of the sludge mass; the flocculant is 0.2% of the dewatered sludge mass, and the flocculant is PAM;

[0041] S2 drying: The above-mentioned partially dewatered sludge is mixed with quicklime in a certain mass ratio and dried to obtain dried sludge and drying carrier gas; the amount of quicklime used is 1-3% of the dry sludge mass.

[0042] S3 Condensation: The above-mentioned dried carrier gas is condensed to obtain dried carrier gas condensate, and then the dried carrier gas condensate is subjected to ammonia stripping treatment to obtain ammonia water 1 and the treated dried carrier gas condensate; the dried carrier gas condensate is used for nitrification-denitrification denitrification treatment; the mass ratio of dewatered sludge to dried sludge depends on the moisture content and calorific value of both, and when the calorific value of dried sludge is 13-14 MJ / kg, the mass ratio of dewatered sludge to dried sludge is approximately 2:3;

[0043] S4 Incineration: Dewatered sludge and dried sludge are mixed and incinerated to obtain fly ash, flue gas, and steam. The resulting flue gas is then treated with ammonia water 1 obtained in S3 for flue gas purification to obtain purified flue gas and flue gas washing wastewater. The flue gas washing wastewater is then treated with ammonia stripping to obtain ammonia water 2 and the treated flue gas washing wastewater. The ammonia water 2 obtained in this step is then mixed with ammonia water 1 obtained in S3 and the flue gas again for flue gas purification. The resulting steam is recycled for drying and / or ammonia stripping treatment. 20-40% v / v of the purified flue gas is recycled for incineration, and the remaining purified flue gas is discharged into the atmosphere. The treated flue gas washing wastewater is recycled for the preparation of flocculants.

[0044] Example 2

[0045] This embodiment provides a synergistic solid-liquid-gas three-phase sludge treatment method, the specific process of which is as follows: Figure 1 As shown, it includes the following steps:

[0046] A method for integrated sludge treatment involving solid, liquid, and gas phases includes the following steps:

[0047] S1 Dewatering: Diluted sludge, conditioning agent, and flocculant are mixed and mechanically dewatered to obtain dewatered sludge; wherein, the conditioning agent is Fe. 2+ / S2O8 2- The mixture of system conditioner and fly ash obtained from incineration, Fe 2+ / S2O8 2- The dosage of the system conditioner is 1.5 / 1.2 mmol / g VSS, and the dosage of fly ash is 10% of the sludge mass; the flocculant is 0.2% of the dewatered sludge mass, and the flocculant is PAM;

[0048] S2 drying: The above-mentioned partially dewatered sludge is mixed with quicklime in a certain mass ratio and dried to obtain dried sludge and drying carrier gas; the amount of quicklime used is 1-3% of the dry sludge mass.

[0049] S3 Condensation: The above-mentioned dried carrier gas is condensed to obtain dried carrier gas condensate, and then the dried carrier gas condensate is subjected to ammonia stripping treatment to obtain ammonia water 1 and the treated dried carrier gas condensate; the dried carrier gas condensate is used for nitrification-denitrification denitrification treatment; the mass ratio of dewatered sludge to dried sludge depends on the moisture content and calorific value of both: when the calorific value of dried sludge is 11-12 MJ / kg, the mass ratio of dewatered sludge to dried sludge is approximately 1:9;

[0050] S4 Incineration: Dewatered sludge and dried sludge are mixed and incinerated to obtain fly ash, flue gas, and steam. The resulting flue gas is then treated with ammonia water 1 obtained in S3 for flue gas purification to obtain purified flue gas and flue gas washing wastewater. The flue gas washing wastewater is then treated with ammonia stripping to obtain ammonia water 2 and the treated flue gas washing wastewater. The ammonia water 2 obtained in this step is then mixed with ammonia water 1 obtained in S3 and the flue gas again for flue gas purification. The resulting steam is recycled for drying and / or ammonia stripping treatment. 20-40% v / v of the purified flue gas is recycled for incineration, and the remaining purified flue gas is discharged into the atmosphere. The treated flue gas washing wastewater is recycled for the preparation of flocculants.

[0051] Example 3

[0052] This embodiment provides a synergistic solid-liquid-gas three-phase sludge treatment method, the specific process of which is as follows: Figure 1 As shown, it includes the following steps:

[0053] A method for integrated sludge treatment involving solid, liquid, and gas phases includes the following steps:

[0054] S1 Dewatering: Diluted sludge, conditioning agent, and flocculant are mixed and mechanically dewatered to obtain dewatered sludge; wherein, the conditioning agent is Fe. 2+ / S2O8 2- The mixture of system conditioner and fly ash obtained from incineration, Fe 2+ / S2O8 2- The system conditioning agent was used at a dosage of 1.0 / 0.8 mmol / g VSS, and the fly ash dosage was 20% of the sludge mass; the flocculant was 0.2% of the dewatered sludge mass, and the flocculant was PAM.

[0055] S2 drying: The above-mentioned partially dewatered sludge is mixed with quicklime in a certain mass ratio and dried to obtain dried sludge and drying carrier gas; the amount of quicklime used is 1-3% of the dry sludge mass.

[0056] S3 Condensation: The above-mentioned dried carrier gas is condensed to obtain dried carrier gas condensate. Then, the dried carrier gas condensate is subjected to ammonia stripping treatment to obtain ammonia water 1 and the treated dried carrier gas condensate. The dried carrier gas condensate is used for nitrification-denitrification denitrification treatment. The mass ratio of dewatered sludge to dried sludge depends on the moisture content and calorific value of both: when the dry basis high calorific value of sludge is 12-13 MJ / kg, the mixing ratio of dewatered sludge to dried sludge is generally about 1:3.

[0057] S4 Incineration: Dewatered sludge and dried sludge are mixed and incinerated to obtain fly ash, flue gas, and steam. The resulting flue gas is then treated with ammonia water 1 obtained in S3 for flue gas purification to obtain purified flue gas and flue gas washing wastewater. The flue gas washing wastewater is then treated with ammonia stripping to obtain ammonia water 2 and the treated flue gas washing wastewater. The ammonia water 2 obtained in this step is then mixed with ammonia water 1 obtained in S3 and the flue gas again for flue gas purification. The resulting steam is recycled for drying and / or ammonia stripping treatment. 20-40% v / v of the purified flue gas is recycled for incineration, and the remaining purified flue gas is discharged into the atmosphere. The treated flue gas washing wastewater is recycled for the preparation of flocculants.

[0058] (II) Experimental Examples

[0059] Experimental Example 1

[0060] This embodiment verifies different Fe... 2+ / S2O8 2- The effect of system conditioner dosage on sludge capillary water absorption time (CST) was investigated. Dosage levels of 0.4 / 0.32, 1.0 / 0.8, 1.5 / 1.2, and 2.0 / 1.6 mmol / g VSS were set, and the results are as follows: Figure 2 As shown.

[0061] Depend on Figure 2 It can be seen that the original sludge has the highest CST, which is 681.0 ± 0.4 s. With the decrease of Fe 2+ / S2O8 2- As the dosage of the system conditioner increases, CST gradually decreases, when Fe 2+ / S2O8 2- When the conditioning agent dosage was 0.4 / 0.32, 1.0 / 0.8, 1.5 / 1.2, and 2.0 / 1.6 mmol / g VSS, the CST decreased to 576.6±5.5, 277.1±7.2, 108.2±0.9, and 82.6±16.0 s after 2 min of reaction, respectively, with reduction rates of 15.3%, 59.3%, 84.1%, and 87.9%, indicating that increasing the dosage significantly improved the dewatering performance of the sludge. Specifically, at 2.0 mmol-Fe... 2+ / gVSS and 1.6mmol-S2O8 2-Under / gVSS conditions, the CST of the treated sludge was reduced by 87.9%, and the sludge dewatering effect was significantly enhanced.

[0062] Experiment Example 2

[0063] This embodiment verifies the effect of different fly ash dosages on sludge specific resistance (SRF) and sludge moisture content. The fly ash dosages were 0%, 10%, 20%, 30%, 40%, and 50% by mass percentage, and the results are as follows: Figure 3 As shown. By Figure 3 It can be seen that when the fly ash dosage is between 10% and 30%, the moisture content of the dewatered sludge decreases, and the solid fractionation rate (SRF) decreases significantly. The SRF reaches its lowest point when the dosage is 30%. When the fly ash dosage exceeds 30%, the porous structure of the fly ash itself can continue to reduce the sludge moisture content, but the increased mechanical strength leads to a higher SRF. Therefore, a fly ash dosage of 30% is recommended to improve the dewatering performance of the sludge and reduce the moisture content of the dewatered sludge cake.

[0064] Experimental Example 3

[0065] The method described in Example 1 was used to purify sludge, and the effect of ammonia concentration in the drying carrier gas condensate on nitrification-denitrification nitrogen removal was verified. Three sets of equipment were set up. The influent water quality is shown in Table 1, and the effluent ammonia nitrogen concentration is shown in Table 2. Figure 4 As shown.

[0066] Table 1. Inlet water quality of condensate from drying carrier gas in the three sets of equipment (unit: mg / L)

[0067] Device serial number COD <![CDATA[NH4 + -N]]> TN <![CDATA[NO3 - -N]]> Remark No. 1 1460 346.42 362 1.56 No alkalinity replenishment No. 2 1430 337.54 353 1.44 Replenish alkalinity No. 3 1312 332.92 350 1.47 Replenish alkalinity

[0068] From Table 1 and Figure 4 It can be seen that, under similar influent water quality, the ammonia concentration in the effluent of Unit 2 (which does not require additional alkalinity) is significantly higher than that of Units 1 and 3. This indicates that, due to the high ammonia concentration in the sludge drying carrier gas condensate, alkalinity supplementation is required during the nitrification-denitrification process to achieve high ammonia nitrogen removal efficiency. However, this invention performs ammonia stripping treatment on the drying carrier gas condensate to form ammonia water, which is then reused, reducing the ammonia concentration in the condensate. Therefore, no additional alkalinity needs to be added during the nitrification-denitrification treatment of the sludge drying carrier gas condensate.

[0069] Experiment Example 4

[0070] This embodiment verifies the effect of oxygen content in the incinerator on the emission concentrations of nitrogen oxides and nitrous oxide in flue gas during sludge incineration. Two experimental groups were set up. In the first group, the oxygen content in the incinerator was increased from 4% v / v to 15% v / v, and in the second group, the oxygen content in the incinerator was increased from 2% v / v to 10% v / v. The results are as follows. Figures 5-8 As shown.

[0071] Depend on Figures 5-6 It can be seen that there is a clear linear relationship between NO concentration and oxygen content; the higher the oxygen content, the more NO is formed, and the higher the NO emission concentration. In the first group of experiments, when the oxygen content increased from 4% v / v to 15% v / v, the NO emission concentration increased by approximately 80 mg / Nm³. 3 In the second group of experiments, when the oxygen content increased from 2% v / v to 7% v / v, the NO emission concentration increased by approximately 45 mg / Nm³. 3 .

[0072] Depend on Figures 7-8 It can be seen that there is a clear linear relationship between N2O concentration and oxygen content; the higher the oxygen content, the more N2O is formed, and the higher the emitted N2O concentration. In the first group of experiments, when the oxygen content increased from 4% v / v to 8% v / v, the emitted N2O concentration increased from 10 mg / Nm³. 3 It rose rapidly to 115 mg / Nm 3 In the second group of experiments, when the oxygen content increased from 2% v / v to 10% v / v, the emitted N2O concentration increased from 20 mg / Nm³. 3 Rapidly rose to 100 mg / Nm 3 .

[0073] Therefore, in this invention, during the flue gas purification stage, a portion of the purified flue gas is recycled back to the combustion zone of the incinerator. This not only recovers the waste heat from the purified flue gas, thereby improving the waste heat utilization efficiency of the incineration process, but also reduces the oxygen content in the incinerator. This, in turn, reduces the emission concentrations of nitrogen oxides and nitrous oxide, which are pollutants in the flue gas. At the same time, it increases the emission of NH3 during sludge incineration, promoting its reduction reaction with nitrogen oxides and further reducing the emission concentration of nitrogen oxides.

[0074] The above description is only a preferred embodiment of the present invention. It should be noted that for those skilled in the art, several improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be considered within the scope of protection of the present invention.

[0075] Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Any person skilled in the art may make various modifications and alterations without departing from the spirit and scope of the present invention, and all such modifications and alterations shall be within the protection scope of the present invention.

Claims

1. A solid-liquid-gas three-phase synergistic sludge comprehensive treatment method, characterized in that, Comprising the following steps: S1 dewatering: mixing sludge, conditioning agent, flocculant, and carrying out mechanical dewatering treatment to obtain dewatered sludge; the sludge is dilute sludge with a water content of 97-99%; the conditioning agent is Fe 2+ / S2O8 2- system conditioning agent and fly ash, and Fe 2+ / S2O8 2- The system conditioning agent is used in an amount of 0.4-2 / 0.32-1.6 mmol / g VSS of the content of dewatered sludge, and the flocculant is 0.1-0.3% of the mass of dewatered sludge; the flocculant is polyacrylamide; S2 drying: mixing part of the above dewatered sludge with quicklime according to mass ratio, drying treatment is carried out to obtain dried sludge and dried carrier gas; the amount of quicklime is 1-3% of the mass of dry matter in sludge except for water removal; S3 condensation: condensing the above dried carrier gas to obtain dried carrier gas condensate, and then carrying out ammonia stripping treatment on the dried carrier gas condensate to obtain ammonia water 1 and treated dried carrier gas condensate; in S3, the dried carrier gas condensate is used for nitrification-denitrification denitrification treatment; S4 incineration: mixing dewatered sludge and dried sludge, incineration treatment is carried out to obtain fly ash, flue gas and steam, then the obtained flue gas and ammonia water 1 obtained in S3 are subjected to flue gas purification treatment to obtain purified flue gas and smoke washing wastewater, then the smoke washing wastewater is subjected to ammonia stripping treatment to obtain ammonia water 2 and treated smoke washing wastewater, and the ammonia water 2 obtained in this step is mixed with ammonia water 1 and flue gas obtained in S3 again for flue gas purification treatment, and the obtained steam is recycled for drying treatment and / or ammonia stripping treatment; the amount of fly ash is 10-50% of the mass of dewatered sludge; The mass ratio of the dewatered sludge and the dried sludge is determined according to the water content and the respective heat values of the two, when the heat value of the dried sludge is 10-15 MJ / kg, the mass ratio of the dewatered sludge and the dried sludge is 1:9-2:3; 20-40 v / v% of the purified flue gas is recycled for incineration treatment, and the remaining purified flue gas is discharged into the atmosphere; The treated smoke washing wastewater is recycled for preparation of flocculants.

2. The sludge comprehensive treatment method of the solid-liquid-gas three-phase cooperation according to claim 1, characterized in that, The Fe 2+ / S2O8 2- The dosage of the system conditioner is 0.8-2 / 0.6-1.6 mmol / g VSS of the dewatered sludge content.

3. The method according to claim 2, wherein the solid-liquid-gas three-phase synergistic sludge comprehensive treatment method is characterized by, The Fe 2+ / S2O8 2- The dosage of the system conditioner was 2 / 1.6 mmol / g VSS of dewatered sludge content.

4. The method according to claim 1, wherein the solid-liquid-gas three-phase synergistic sludge comprehensive treatment method is characterized by, In S1, the flocculant is 0.2% of the mass of dewatered sludge.

5. The method according to claim 1, wherein the solid-liquid-gas three-phase synergistic sludge comprehensive treatment method is characterized by, In S1, the amount of fly ash is 20-40% of the mass of dewatered sludge.

6. The method according to claim 1, wherein the method is characterized by, In S1, the amount of fly ash is 30% of the mass of dewatered sludge.

Images