CN112607996B - Thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process - Google Patents
Thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process Download PDFInfo
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- CN112607996B CN112607996B CN202011485891.6A CN202011485891A CN112607996B CN 112607996 B CN112607996 B CN 112607996B CN 202011485891 A CN202011485891 A CN 202011485891A CN 112607996 B CN112607996 B CN 112607996B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/127—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering by centrifugation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention belongs to the field of sludge treatment and recycling of urban sewage treatment plants, and particularly relates to a thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process. The method comprises the following steps: (1) performing centrifugal dehydration; (2) thermal hydrolysis; (3) anaerobic digestion; (4) dehydrating a plate frame; (5) granulating; (6) drying; (7) and (6) carbonizing. The invention can be used in the fields of urban domestic sewage pretreatment and advanced treatment, industrial sewage treatment, soil improvement, carrier materials and the like. The invention solves the problem of matching of the processing capacity of each system unit by controlling the process conditions, realizes high-efficiency operation and energy self-sufficiency, and has high popularization and application values.
Description
Technical Field
The invention belongs to the field of sludge treatment and recycling of urban sewage treatment plants, and particularly relates to a thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process.
Background
Sludge from urban sewage treatment plants is a byproduct of sewage treatment, and concentrates about 50% of COD in the sewage treatment process. Whether the sludge is subjected to harmless treatment and resource treatment is a key link for evaluating the sewage treatment effect. The sludge pyrohydrolysis advanced anaerobic digestion system realizes the harmlessness of sludge. The sludge pyrolysis carbonization adopts town sludge as a raw material to prepare a sludge-based activated carbon material, thereby realizing the recycling of the sludge.
The sludge carbonization process comprises two processes of sludge drying and carbonization so as to reduce the water content of the raw materials and the pyrolysis reaction, and the two processes both need to consume a large amount of energy, so that the operation cost is high, and the popularization and the application of the pyrolysis carbonization process are limited. Compared with the traditional sludge, the advanced anaerobic digestion sludge has smaller particles and is more difficult to dewater, and a large amount of conditioner with high conductivity needs to be added into the sludge, so that the TDS content in the dewatered sludge is too high, and the land utilization of the sludge is not facilitated.
Therefore, how to fully utilize the energy of the sludge to supply the sludge carbonization process is the key for popularizing the application of the sludge carbonization engineering.
Disclosure of Invention
The invention aims to solve the problems and provides a thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process, which provides clean high-grade energy by fully excavating the capability of sludge anaerobic digestion to generate methane and realizes the self-sufficiency of the energy of an advanced anaerobic digestion system and a pyrolysis carbonization coupling system to the greatest extent.
In order to achieve the above object, the present invention provides a thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process, comprising:
(1) and (3) centrifugal dehydration: centrifugally dewatering the sludge until the water content is 80-85%;
(2) thermal hydrolysis: carrying out thermal hydrolysis on the sludge obtained in the step (1) in a thermal hydrolysis unit;
(3) anaerobic digestion: carrying out anaerobic digestion on the sludge subjected to thermal hydrolysis in an anaerobic digestion unit to generate biogas, so that the organic matter content of the sludge subjected to anaerobic digestion is less than or equal to 45%;
(4) plate frame dehydration: carrying out plate-and-frame dehydration on the anaerobic digestion sludge to reduce the water content of the sludge to 65-75% and obtain a mud cake;
(5) and (3) granulation: granulating or layering the mud cakes to obtain sludge particles;
(6) drying: drying treatment is carried out in a drying unit, and the energy source of the drying treatment is methane generated by anaerobic digestion;
wherein the processing capacity of the drying unit is more than or equal to 0.6 x the processing capacity of the thermal hydrolysis unit, and the granulated sludge particles are dried by a drying machine in the drying unit until the water content is 20-30% to obtain dried sludge;
(7) carbonizing: conveying the dried sludge to a carbonization furnace of a carbonization unit for carbonization treatment to obtain a sludge carbonization product, wherein the treatment capacity of the carbonization unit is not less than 0.45 × that of a thermal hydrolysis unit;
wherein, the biogas generated by the anaerobic digestion unit is purified and then is respectively supplied to the thermal hydrolysis unit, the drying unit and the carbonization unit.
According to the invention, the thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process can adopt the existing anaerobic digestion and pyrolysis carbonization coupling system. In the invention, biogas generated by the anaerobic digestion unit enters a biogas tank for storage after being purified, the biogas is respectively conveyed to a biogas boiler for supplying heat energy to the thermal hydrolysis unit and a combustion furnace for supplying heat to the drying unit and the carbonization unit through pipelines, and the biogas distribution amount of each unit is realized through biogas flow control. The difference from the conventional method is that the invention accurately defines the relationship between the processing capacity of the drying unit and the processing capacity of the thermal hydrolysis unit and the processing capacity of the carbonization unit. In the actual operation process, the biogas amount consumed by the thermal hydrolysis unit, the biogas amount consumed by the drying unit, the biogas amount consumed by the carbonization unit and the biogas residual amount are approximately equal to the biogas amount generated by the anaerobic digestion unit. The residual amount of the biogas may be 0 or not 0, even if not 0, in the continuous operation process, because the amount of the biogas consumed by the thermal hydrolysis unit, the amount of the biogas consumed by the drying unit and the amount of the biogas consumed by the carbonization unit are basically unchanged, the residual amount of the biogas is a fixed value, so that the residual biogas can be quantitatively used in other process steps.
Preferably, in the step (1), the sludge is at least one of grid slag, primary sludge and excess sludge generated in a sewage treatment process mainly including domestic sewage, such as sludge generated in a municipal domestic sewage treatment process.
Preferably, in the step (1), the initial organic content of the sludge is more than or equal to 50%.
Preferably, in the step (1), the initial water content of the sludge is 95% to 99.7%.
Preferably, in the step (2), the reaction temperature of the thermal hydrolysis is 150-180 ℃, and the reaction time is 30-45 min.
Preferably, in the step (3), the reaction temperature of anaerobic digestion is 38-42 ℃, and the reaction time is 15-25 d.
Preferably, in the step (5), the diameter of the sludge particles is 3mm-5 mm.
Preferably, in the step (6), the dryer is a low-temperature heat pump dryer or a low-temperature vacuum dryer.
Preferably, in the step (7), the carbonization furnace is a continuous fixed bed pyrolysis reaction furnace, a continuous multi-stage solid pyrolysis reaction furnace, a continuous moving bed pyrolysis reaction furnace or a fluidized bed pyrolysis reaction furnace.
Preferably, in the step (7), the carbonization treatment temperature is 500-800 ℃, and the reaction time is 30-90 min.
Preferably, the steps of centrifugal dewatering and plate-and-frame dewatering each further comprise: the dehydration is assisted by a dehydration medicament, and the dosage rate of the dehydration medicament is 5 per mill-15 percent of the material to be dehydrated.
In the present invention, the equipment for dewatering can be selected by those skilled in the art according to the needs, such as a belt type dewatering machine and a plate and frame filter press.
The invention has the beneficial effects that:
the invention can be used in the fields of urban domestic sewage pretreatment and advanced treatment, industrial sewage treatment, soil improvement, carrier materials and the like. The invention solves the problem of matching of the processing capacity of each system unit by controlling the process conditions, realizes high-efficiency operation and energy self-sufficiency, and has high popularization and application values.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
Figure 1 shows a process flow diagram of the present invention.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
Figure 1 shows a process flow diagram of the present invention. Referring to fig. 1, in the embodiment of the present invention, the thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process includes the following steps, and the specific parameters are detailed in the embodiments:
(1) and (3) centrifugal dehydration: centrifugally dewatering sludge (at least one of grid slag, primary sludge and excess sludge generated in a sewage treatment process mainly comprising domestic sewage, wherein the initial organic content is more than or equal to 50 percent, and the initial water content is 95-99 percent) to the water content of 80-85 percent;
(2) thermal hydrolysis: carrying out thermal hydrolysis on the sludge obtained in the step (1) in a thermal hydrolysis unit, wherein the reaction temperature of the thermal hydrolysis is 150-180 ℃, and the reaction time is 30-45 min;
(3) anaerobic digestion: carrying out anaerobic digestion on the sludge subjected to thermal hydrolysis in an anaerobic digestion unit (the reaction temperature of the anaerobic digestion is 38-42 ℃ and the reaction time is 15-25 d) and generating biogas, so that the organic matter content of the sludge subjected to the anaerobic digestion is less than or equal to 45%;
(4) plate frame dehydration: carrying out plate-and-frame dehydration on the anaerobic digestion sludge to reduce the water content of the sludge to 65-75% and obtain a mud cake;
(5) and (3) granulation: granulating or layering the mud cakes to obtain sludge particles with the diameter of 3-5 mm;
(6) drying: drying treatment is carried out in a drying unit, and the energy source of the drying treatment is methane generated by anaerobic digestion;
wherein the processing capacity of the drying unit is more than or equal to 0.6 x the processing capacity of the thermal hydrolysis unit, and the granulated sludge particles are dried by a drier (a low-temperature heat pump drier or a low-temperature vacuum drier) in the drying unit until the water content is 20-30% to obtain dried sludge;
(7) carbonizing: conveying the dried sludge into a carbonization furnace (a continuous fixed bed pyrolysis reaction furnace, a continuous multi-section solid pyrolysis reaction furnace, a continuous moving bed pyrolysis reaction furnace or a fluidized bed pyrolysis reaction furnace) of a carbonization unit for carbonization treatment (the temperature of the carbonization treatment is 500-800 ℃, and the reaction time is 30-90 min) to obtain a sludge carbonization product, wherein the treatment capacity of the carbonization unit is more than or equal to 0.45 × the treatment capacity of the pyrohydrolysis unit;
wherein, the biogas generated by the anaerobic digestion unit is purified and then is respectively supplied to the thermal hydrolysis unit, the drying unit and the carbonization unit.
In the embodiment of the invention, the sludge generated by the urban sewage treatment plant is the sludge generated in the process of treating the domestic sewage of a certain town.
Example 1
Taking the sludge feeding amount of the thermal hydrolysis unit as 1tDS as an example:
the water content of sludge produced by a certain municipal sewage treatment plant is 97%, the content of organic components is 70%, and the sludge is centrifugally dewatered until the water content is 83.5%.
The thermal hydrolysis temperature is 165 ℃, the reaction time is 30min, and the methane consumption of a thermal hydrolysis unit is as follows: 150m3。
The anaerobic digestion temperature is 40 ℃, the reaction time is 18d, the organic matter content of the sludge after anaerobic digestion is 45 percent, and the methane generation amount is as follows: 400m3。
After the sludge cake is dewatered by a plate frame, the water content of the sludge cake is reduced to 65 percent.
And granulating the mud cakes to obtain sludge particles with the diameter of 3-5 mm.
Drying the granulated sludge by adopting a low-temperature heat pump dryer, wherein the water content of sludge particles is reduced to 30%, and the methane consumption of a drying unit is as follows: 87m3。
The carbonization unit adopts a continuous moving bed pyrolysis reaction furnace, the carbonization temperature is 800 ℃, the reaction time is 30min, and the methane consumption of the carbonization unit is as follows: 58m3The pyrolysis gas generated by the unit is supplied to the unit for use.
After crushing and screening, the obtained sludge carbonized product is used as a carbon-based dehydration material.
After treatment, the sludge is completely converted into a sludge carbonization product, and the residual methane is about 105m except for the methane generated by anaerobic digestion of the sludge which is used for thermal hydrolysis, drying and carbonization of the sludge3。
In this embodiment, the processing capacity of the drying unit is 0.65 × the processing capacity of the thermal hydrolysis unit, and the processing capacity of the carbonization unit is 0.55 × the processing capacity of the thermal hydrolysis unit.
Example 2
Taking the sludge feeding amount of the thermal hydrolysis unit as 1tDS as an example:
the water content of sludge produced by a certain municipal sewage treatment plant is 97%, the content of organic components is 60%, and the sludge is centrifugally dewatered until the water content is 83.5%.
The thermal hydrolysis temperature is 165 ℃, the reaction time is 30min, and the methane consumption of a thermal hydrolysis unit is as follows: 150m3。
The anaerobic digestion temperature is 40 ℃, and the reaction time is 18 d; the content of organic matters in the sludge after anaerobic digestion is 45 percent, and the methane yield is 310m3。
After the sludge cake is dewatered by a plate frame, the water content of the sludge cake is reduced to 65 percent.
And granulating the mud cakes to obtain sludge particles with the diameter of 3-5 mm.
Drying the granulated sludge by a heat pump dryer, reducing the water content of sludge particles to 30%, and reducing the methane consumption of a drying unit: 98m3。
The carbonization system adopts a continuous moving bed pyrolysis reaction furnace, the carbonization temperature is 500 ℃, the reaction time is 30min, and the methane consumption of the carbonization unit is as follows: 59m3The pyrolysis gas generated by the unit is discharged as waste heat after being combusted and purified at high temperature.
After crushing and screening, the obtained sludge carbonized product is used as a soil remediation material.
After treatment, the sludge is completely converted into a sludge carbonization product, and the biogas generated by anaerobic digestion of the sludge is used for thermal hydrolysis, drying and carbonization of the sludge, and the residual biogas is about 3m3。
In this embodiment, the processing capacity of the drying unit is 0.85 × that of the thermal hydrolysis unit, and the processing capacity of the carbonization unit is 0.75 × that of the thermal hydrolysis unit.
Example 3
Taking the sludge feeding amount of the thermal hydrolysis unit as 1tDS as an example:
the water content of sludge produced by a certain municipal sewage treatment plant is 97%, the content of organic components is 75%, and the sludge is centrifugally dewatered until the water content is 83.5%.
The thermal hydrolysis temperature is 180 ℃, the reaction time is 30min, and the methane consumption of a thermal hydrolysis unit is as follows: 190m3。
The anaerobic digestion temperature is 40 ℃, the reaction time is 18d, the organic matter content of the sludge after anaerobic digestion is 45 percent, and the methane generation amount is as follows: 530m3。
After the sludge cake is dewatered by a plate frame, the water content of the sludge cake is reduced to 65 percent.
And granulating the mud cakes to obtain sludge particles with the diameter of 3-5 mm.
Drying the granulated sludge by adopting a low-temperature heat pump dryer, wherein the water content of sludge particles is reduced to 30%, and the methane consumption of a drying unit is as follows: 65m3。
The carbonization unit adopts a continuous moving bed pyrolysis reaction furnace, the carbonization temperature is 800 ℃, the reaction time is 30min, and the methane of the carbonization unit is consumedQuantity: 45m3The pyrolysis gas generated by the unit is supplied to the unit for use.
After crushing and screening, the obtained sludge carbonized product is used as a carbon-based dehydration material.
After treatment, the sludge is completely converted into a sludge carbonization product, and the residual methane is about 230m except for the methane generated by anaerobic digestion of the sludge which is used for thermal hydrolysis, drying and carbonization of the sludge3。
In this embodiment, the processing capacity of the drying unit is 0.60 × that of the thermal hydrolysis unit, and the processing capacity of the carbonization unit is 0.45 × that of the thermal hydrolysis unit.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (8)
1. A thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process is characterized by comprising the following steps:
(1) and (3) centrifugal dehydration: centrifugally dewatering the sludge until the water content is 80-85%;
(2) thermal hydrolysis: carrying out thermal hydrolysis on the sludge obtained in the step (1) in a thermal hydrolysis unit;
(3) anaerobic digestion: carrying out anaerobic digestion on the sludge subjected to thermal hydrolysis in an anaerobic digestion unit to generate biogas, so that the organic matter content of the sludge subjected to anaerobic digestion is less than or equal to 45%;
(4) plate frame dehydration: performing plate-frame dehydration on the anaerobic digestion sludge, and reducing the water content of the sludge to 65-75% to obtain a sludge cake;
(5) and (3) granulation: granulating or layering the mud cakes to obtain sludge particles;
(6) drying: drying treatment is carried out in a drying unit, and the energy source of the drying treatment is methane generated by anaerobic digestion;
wherein the processing capacity of the drying unit is more than or equal to 0.6 × that of the pyrohydrolysis unit, and the granulated sludge particles are dried by a drying machine in the drying unit until the water content is 20% -30%, so as to obtain dried sludge;
(7) carbonizing: conveying the dried sludge to a carbonization furnace of a carbonization unit for carbonization treatment to obtain a sludge carbonization product, wherein the treatment capacity of the carbonization unit is not less than 0.45 × that of a thermal hydrolysis unit;
wherein, the biogas generated by the anaerobic digestion unit is purified and then is respectively supplied to the thermal hydrolysis unit, the drying unit and the carbonization unit;
wherein in the step (2), the reaction temperature of the thermal hydrolysis is 150-180 ℃, and the reaction time is 30-45 min;
wherein in the step (7), the temperature of the carbonization treatment is 500-800 ℃, and the reaction time is 30-90 min.
2. The coupled process of pyrohydrolysis advanced anaerobic digestion and pyrolysis carbonization as claimed in claim 1, wherein in step (1), the sludge is at least one of grate sludge, primary sludge and excess sludge generated in a sewage treatment process mainly comprising domestic sewage.
3. The coupled thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization process of claim 1, wherein, in step (1),
the initial organic content of the sludge is more than or equal to 50 percent;
the initial water content of the sludge is 95% -99.7%.
4. The thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization coupling process as claimed in claim 1, wherein in the step (3), the reaction temperature of anaerobic digestion is 38-42 ℃, and the reaction time is 15-25 d.
5. The coupled thermal hydrolytic advanced anaerobic digestion and pyrolytic carbonization process according to claim 1, wherein in step (5) the sludge granules have a diameter of 3mm to 5 mm.
6. The coupled process of pyrohydrolysis advanced anaerobic digestion and pyrolysis carbonization as claimed in claim 1, wherein in step (6), the drier is a low temperature heat pump drier or a low temperature vacuum drier.
7. The coupled process of pyrohydrolysis advanced anaerobic digestion and pyrolysis carbonization as claimed in claim 1, wherein, in step (7), the carbonization furnace is a continuous fixed bed pyrolysis reactor, a continuous multi-stage solid pyrolysis reactor, a continuous moving bed pyrolysis reactor, or a fluidized bed pyrolysis reactor.
8. The coupled thermal hydrolysis advanced anaerobic digestion and pyrolysis carbonization process of claim 1, wherein the steps of centrifugal dewatering and plate and frame dewatering each further comprise: and (3) dehydrating by adopting a dehydrating agent, wherein the dosage rate of the dehydrating agent is 5 per mill-15% of the material to be dehydrated.
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