CN112607982B - Sludge pyrohydrolysis system and sludge anaerobic digestion system - Google Patents
Sludge pyrohydrolysis system and sludge anaerobic digestion system Download PDFInfo
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- CN112607982B CN112607982B CN202011487516.5A CN202011487516A CN112607982B CN 112607982 B CN112607982 B CN 112607982B CN 202011487516 A CN202011487516 A CN 202011487516A CN 112607982 B CN112607982 B CN 112607982B
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/20—Sludge processing
Abstract
The invention discloses a sludge pyrohydrolysis system, which comprises a slurrying tank, a pyrohydrolysis tank and a sludge storage tank, wherein all treatment tanks are sequentially communicated through sludge conveying pipelines. The invention also discloses a sludge anaerobic digestion system, which comprises an anaerobic digestion tank and the sludge pyrohydrolysis system, wherein the sludge storage tank is communicated with the anaerobic digestion tank through a sludge conveying pipeline, and the anaerobic digestion tank is communicated with the high-temperature oxidation device through a methane conveying pipeline. Under the condition of not adding chemical agents, the invention utilizes the thermal hydrolysis tail gas after high-temperature oxidation to be reused in the sludge treatment process, and one product methane after anaerobic digestion of the sludge is reused in the thermal hydrolysis odor high-temperature oxidation process, thus having the advantages of economy, environmental protection, low operation cost and the like.
Description
Technical Field
The invention relates to the field of environmental protection equipment, in particular to a sludge pyrohydrolysis system and a sludge anaerobic digestion system.
Background
In the sludge treatment process, compared with other technologies, the anaerobic digestion technology has the advantages of recycling carbon energy in sludge and realizing sludge stabilization, and is applied to more and more projects in China in recent years. Due to the blocking effect of the sludge cell wall, a sludge cell hydrolysis wall breaking pretreatment process is generally added at the front end of anaerobic digestion, organic matters and water in the sludge cells are released by realizing the hydrolysis wall breaking of the sludge cell wall, and macromolecular organic matters are converted into micromolecular soluble organic matters, so that the effects of shortening the hydrolysis stage duration in the anaerobic digestion process and improving the anaerobic digestion performance are achieved.
The existing hydrolysis wall-breaking pretreatment method comprises thermal hydrolysis and chemical hydrolysis technologies. The chemical hydrolysis technology is characterized in that a certain amount of acid/alkali and oxidation/reduction substances are added into the sludge, and the hydrolysis of sludge cell walls is promoted by chemical reaction, so that the pretreatment efficiency is improved. Patent document CN109942159 discloses a method for treating excess sludge with sulfite, which comprises adjusting the total solid concentration in the excess sludge to 3-20g/L, adding sulfite to make the sulfur content 0.1-0.8g S/L, adjusting pH to 5-7, and allowing the pretreated sludge to enter an anaerobic digester to destroy the sludge structure and release organic matters, thereby improving the dissolved chemical oxygen demand concentration in the pretreatment step and the methane yield in the digester. However, in the method, the addition cost of the materials is increased by adding sulfate outside, and chemical substances are additionally introduced to influence the quality of the methane. Patent documents with publication numbers CN110482822 and CN110028211 relate to a method for breaking walls of sludge by chemical oxidation, and by adding a certain amount of sodium sulfite/sodium bisulfite and potassium permanganate into the sludge, substances with strong oxidizability are generated to promote the hydrolysis of sludge cell walls, and macromolecular organic matters in the sludge can be degraded into micromolecular soluble organic matters. However, in the method, a medicament needs to be added externally, so that the material adding cost is increased, and the stability of the rear-end anaerobic digestion system is influenced.
Therefore, in the current practical application, a thermal hydrolysis technology is mainly adopted as a sludge pretreatment technology, the wall breaking of the sludge is realized through a thermal treatment process under the condition that the chemical properties of a system are not changed, and the basic process flow is as follows: the primary sludge enters a thermal hydrolysis tank after being pulped and preheated, the sludge is subjected to flash evaporation and pressure release in a high-temperature and high-pressure environment of the thermal hydrolysis tank to complete sludge cell wall breaking, then the solid content and the temperature are adjusted to enter an anaerobic digestion tank, waste heat steam generated by pressure release of the thermal hydrolysis tank returns to a pulping stage for waste heat recovery, and the tail gas discharged after the pulping tank absorbs the waste heat has high pollution concentration and complex components. The content of the reducing sulfide is extremely high, the reducing sulfide mainly comprises methyl mercaptan, methyl sulfide, hydrogen sulfide and the like, the pungent smell is large, the tail gas is difficult to effectively treat through biological deodorization and chemical deodorization, or the high-efficiency treatment of the thermal hydrolysis tail gas can be achieved through the combination of multiple process sections of washing heat exchange, incineration deodorization, chemical washing, biological deodorization and the like. Patent document No. CN206435049 discloses a device for treating high-concentration malodorous gas generated by sludge pyrohydrolysis, which adopts the processes of washing heat exchange, incineration deodorization, chemical washing and biological deodorization, and achieves high-efficiency treatment of high-sulfur tail gas through combination of multiple process sections, but the process links of the method are multiple.
Disclosure of Invention
The invention aims to solve the technical problem of overcoming the defects of the prior art and provide a pyrohydrolysis system which can treat pyrohydrolysis tail gas, improve the pretreatment efficiency and does not influence the stability of an anaerobic digestion process.
The invention further provides an anaerobic digestion system for realizing the recycling of the biogas.
In order to solve the technical problems, the invention adopts the following technical scheme:
the utility model provides a mud pyrohydrolysis system, includes pulp jar, pyrohydrolysis jar and stores up the mud jar, and each processing jar communicates in proper order through mud pipeline, and mud pyrohydrolysis system still includes high temperature oxidation device, heat sink and delivery fan, pyrohydrolysis jar, pulp jar, high temperature oxidation device, heat sink, delivery fan and storage mud jar communicate in proper order through tail gas pipeline.
As a further improvement of the technical scheme:
the thermal hydrolysis tank adopts a sequencing batch reactor.
The sludge storage tank adopts a complete mixing type reactor, the solid content of the sludge in the tank is 5-15%, the retention time is 5-10h, and the rotating speed of the stirrer is 20-200 rpm/min.
The high-temperature oxidation device comprises an incinerator, the temperature is 800-900 ℃, and the retention time of waste gas is 2-5 s.
The cooling device is a spraying device, the temperature of the tail gas after cooling is 50-80 ℃, and the cooling device is communicated with the sludge storage tank through a spraying water conveying pipeline.
And at least three tail gas conveying pipelines are uniformly arranged at the bottom of the sludge storage tank.
The sludge anaerobic digestion system comprises an anaerobic digestion tank and the sludge pyrohydrolysis system, wherein the sludge storage tank is communicated with the anaerobic digestion tank through a sludge conveying pipeline, and the anaerobic digestion tank is communicated with a high-temperature oxidation device through a methane conveying pipeline.
As a further improvement of the above technical solution:
the anaerobic digestion tank adopts a complete mixing type reactor.
Compared with the prior art, the invention has the beneficial effects that:
according to the pyrohydrolysis system disclosed by the invention, the pyrohydrolysis tail gas is conveyed from the pyrohydrolysis tank to the slurrying tank and then to the high-temperature oxidation device for high-temperature oxidation, at the moment, the reductive sulfide in the pyrohydrolysis tail gas is oxidized into sulfur dioxide, the pyrohydrolysis tail gas is conveyed to the sludge storage tank by the conveying fan after being cooled by the cooling device and is subjected to chemical reaction with alkalinity in the sludge storage tank to generate sulfite and bisulfite, and the generated sulfite and bisulfite are subjected to chemical reaction with sludge cells, so that secondary hydrolysis wall breaking of the sludge cells is promoted.
The anaerobic digestion system disclosed by the invention comprises the thermal hydrolysis system, so that the advantages are also achieved, one of the products of biogas after anaerobic digestion is conveyed to the incinerator to be used as a heating source, the recycling of the biogas is realized, the environment is protected, the economy is realized, and the operation cost is low.
Drawings
FIG. 1 is a schematic structural view of a sludge pyrohydrolysis system and a sludge anaerobic digestion system according to the present invention.
The reference numerals in the figures denote:
1. a slurrying tank; 2. a thermal hydrolysis tank; 3. a sludge storage tank; 4. an anaerobic digestion tank; 5. a sludge conveying pipeline; 6. a high temperature oxidation unit; 7. a cooling device; 8. a conveying fan; 9. a tail gas conveying pipeline; 10. a spray water delivery conduit; 11. a biogas conveying pipeline;
Detailed Description
The technical scheme of the invention is further explained in detail by combining the drawings and the specific embodiments in the specification.
Fig. 1 shows an embodiment of the sludge pyrohydrolysis system of the present invention, the sludge pyrohydrolysis system of the present embodiment includes a slurrying tank 1, a pyrohydrolysis tank 2, and a sludge storage tank 3, each processing tank is sequentially communicated through a sludge conveying pipeline 5, the sludge pyrohydrolysis system further includes a high temperature oxidation device 6, a cooling device 7, and a conveying fan 8, and the pyrohydrolysis tank 2, the slurrying tank 1, the high temperature oxidation device 6, the cooling device 7, the conveying fan 8, and the sludge storage tank 3 are sequentially communicated through a tail gas conveying pipeline 9.
This pyrohydrolysis system, carry the pulpifying jar through carrying pyrohydrolysis tail gas from the pyrohydrolysis jar and go on high temperature oxidation to the high temperature oxidation device again, reductive sulfide in the pyrohydrolysis tail gas is oxidized to sulfur dioxide this moment, utilize conveying fan to carry to storage mud jar after the cooling through the heat sink, take place chemical reaction with the alkalinity in the storage mud jar, generate sulphite and bisulphite, utilize sulphite and the bisulphite that generates and sludge cell to take place chemical reaction, thereby promote macromolecular organic matter secondary hydrolysis broken wall in the sludge cell, under the condition of externally not adding chemical agent, both solved the problem that the pyrohydrolysis foul smell is difficult to handle, the efficiency of preliminary treatment has been improved again and anaerobic digestion process stability itself is not influenced.
In this embodiment, the thermal hydrolysis tank 2 is a sequencing batch reactor. The sequencing batch reactor realizes multi-flow continuous operation and is suitable for occasions with large intermittent discharge and flow change, such as sludge treatment and the like.
In the embodiment, the sludge storage tank 3 adopts a complete mixing type reactor, the solid content of the sludge in the tank is 5-15%, the retention time is 5-10h, and the rotating speed of the stirrer is 20-200rpm/min, so that the chemical reaction in the sludge storage tank 3 is more sufficient, and the reaction speed is accelerated.
In this embodiment, the high temperature oxidation device 6 comprises an incinerator with a temperature of 800 ℃ and 900 ℃ and a waste gas residence time of 2-5 s. One of the anaerobic digestion products, namely the biogas, can enter the incinerator again for incineration, so that the biogas can be recycled as a heating source.
In the embodiment, the cooling device 7 is a spraying device, the temperature of the cooled tail gas is 50-80 ℃, and the cooling device 7 is communicated with the sludge storage tank 3 through a spraying water conveying pipeline 10. The thermal hydrolysis tail gas after high-temperature oxidation is cooled in a spraying mode, and the water after being sprayed and cooled is conveyed to the sludge storage tank 3 through the spray water conveying pipeline 10 and used as sludge dilution water, so that two purposes are achieved, and the system operation cost is saved.
In this embodiment, the bottom of the sludge storage tank 3 is at least provided with three tail gas conveying pipelines 9, and the tail gas conveying pipelines 9 are preferably uniformly arranged. The pyrohydrolysis tail gas gets into from the tail gas pipeline 9 that 3 bottoms of mud storage tank evenly set up, can improve the degree of mixing of tail gas and mud for reaction rate.
Fig. 1 shows an embodiment of the anaerobic sludge digestion system of the present invention, which includes an anaerobic digestion tank 4 and the above-mentioned thermal sludge hydrolysis system, wherein the sludge storage tank 3 is communicated with the anaerobic digestion tank 4 through a sludge conveying pipeline 5, and the anaerobic digestion tank 4 is communicated with the high temperature oxidation device 6 through a methane conveying pipeline 11.
The sludge anaerobic digestion system comprises the thermal hydrolysis system, so that the sludge anaerobic digestion system also has the advantages, one of the products of the anaerobic digestion, namely the biogas, is conveyed to the incinerator to be used as a heating source, the recycling of the biogas is realized, and the sludge anaerobic digestion system is economical, environment-friendly and low in operation cost.
In this embodiment, the anaerobic digestion tank 4 employs a complete mixing reactor, so that the chemical reaction in the anaerobic digestion tank is more sufficient, and the efficiency of anaerobic digestion of sludge is also improved.
The method comprises the following steps of firstly feeding primary sludge (with the VSS content of 40%) into a slurry tank 1, keeping the temperature at 80 ℃ for 1h, feeding the slurry sludge into a thermal hydrolysis tank 2, keeping the thermal hydrolysis operation temperature at 165 ℃ for 30min, feeding thermal hydrolysis release steam into the slurry tank 1, recycling waste heat, feeding tail gas into an incinerator, keeping the temperature at 800 ℃ for 2s, spraying and cooling the incinerated tail gas to 60 ℃, conveying the incinerated tail gas to a sludge storage tank 3 through a conveying fan, and simultaneously feeding tail gas cooling spray water into the sludge storage tank 3. The sludge in the thermal hydrolysis tank 2 enters the rear sludge storage tank 3, the solid content is adjusted to 10%, the retention time is 7 hours, then the sludge enters the anaerobic digestion tank 4, the operation is carried out by adopting a high-temperature anaerobic digestion process, the operation temperature is 55 ℃, and the retention time is 20 days. Biogas generated in the anaerobic digestion tank 4 enters the incinerator through a biogas conveying pipeline 11 to be used as a heating source. After detection, the SCOD content of the sludge in the sludge storage tank 3 is 24000mg/L, the VSS content is 33.5 percent, and the gas production rate of the unit sludge (sludge in the sludge storage tank) in the anaerobic digestion tank 4 is 18.5Nm3/t，The pH value of the digested sludge is 7.85, and CH is contained in the methane465.4% of H2S was 68 ppm.
Application example two
The method comprises the following steps of firstly enabling primary sludge (with the VSS content of 40%) to enter a slurrying tank 1, enabling the temperature to be 80 ℃ and the retention time to be 1h, enabling the slurried sludge to enter a thermal hydrolysis tank 2, enabling the thermal hydrolysis operation temperature to be 165 ℃ and the heating time to be 30min, enabling thermal hydrolysis release steam to enter the slurrying tank 1 and then enabling tail gas to enter an incinerator after waste heat recovery, enabling the incinerator temperature to be 800 ℃ and the retention time to be 2s, enabling the incinerated tail gas to be sprayed and cooled to 60 ℃ and then conveyed to a sludge storage tank 3 through a conveying fan, and enabling tail gas cooling spray water to enter the sludge storage tank 3 at the same time. The sludge in the thermal hydrolysis tank 2 enters the rear sludge storage tank 3, the solid content is adjusted to 10%, the retention time is 5 hours, then the sludge enters the anaerobic digestion tank 4, the operation is carried out by adopting a high-temperature anaerobic digestion process, the operation temperature is 55 ℃, and the retention time is 20 days. Biogas generated in the anaerobic digestion tank 4 enters the incinerator through a biogas conveying pipeline 11 to be used as a heating source. Wherein the SCOD content of the sludge in the sludge storage tank 3 is 23100mg/L, the VSS content is 34.2 percent, and the gas production rate of the unit sludge (sludge in the sludge storage tank) in the anaerobic digestion tank 4 is 17.8Nm3T, pH of the digested sludge is 7.88, CH in the biogas465.2% of H2S was 66 ppm.
Comparative example
The sludge treatment plant adopts a thermal hydrolysis and high-temperature anaerobic digestion operation process, wherein the VSS (volatile suspended solids) content in the primary sludge accounts for 40%, the primary sludge firstly enters a slurrying tank, the temperature is 80 ℃, the retention time is 1h, the slurried sludge enters the thermal hydrolysis tank, the thermal hydrolysis operation temperature is 165 ℃, the heating time is 30min, the thermal hydrolysis pressure-relief steam enters the slurrying tank for waste heat recovery, the tail gas enters a subsequent deodorization facility for treatment and discharge, the sludge in the thermal hydrolysis tank enters a rear sludge storage tank, the solid content is adjusted to 10%, the retention time is 7h, the sludge enters an anaerobic digestion tank, the high-temperature anaerobic digestion process is adopted for operation, the operation temperature is 55 ℃, and the retention time is 20 d. After detection, the content of SCOD (soluble chemical organic matter) in the sludge storage tank is 21500mg/L, the content of VSS is 35.1 percent, and the sludge yield per ton of the sludge storage tank is 16Nm3T, pH of the digested sludge is 8.15, CH in the biogas465.0% of H2S was 62 ppm.
By caseCompared with the traditional process of thermal hydrolysis and anaerobic digestion, the method can improve the SCOD dissolution rate of the sludge pretreatment link by about 10 percent and increase the gas production of an anaerobic digestion system by about 10 to 15 percent. Simultaneously can reduce the pH value of the anaerobic digestion system to a certain extent, is favorable for adjusting the stability of the sludge anaerobic digestion system, and can remove CH from the methane4And H2For S content, the technical scheme is that CH is treated4Content has no influence, H2The S content slightly rises, but the influence is not great. Meanwhile, through cost accounting, the links of increasing the operation cost of the technical scheme mainly lie in the links of burning and deodorizing methane consumption, and the methane consumption in the links of burning and deodorizing is about 1Nm3T, essentially negligible increase in gas production relative to the example.
It should be noted that although the present invention has been described with reference to the preferred embodiments, the present invention is not limited thereto. Those skilled in the art can make numerous possible variations and modifications to the present invention, or modify equivalent embodiments to equivalent variations, without departing from the scope of the invention, using the teachings disclosed above. Therefore, any simple modification, equivalent change and modification made to the above embodiments according to the technical spirit of the present invention should fall within the protection scope of the technical scheme of the present invention, unless the technical spirit of the present invention departs from the content of the technical scheme of the present invention.
Claims (8)
1. The utility model provides a mud pyrohydrolysis system, includes pulp jar (1), pyrohydrolysis jar (2) and storage mud jar (3), and each treatment tank communicates its characterized in that in proper order through mud pipeline (5): the sludge pyrohydrolysis system further comprises a high-temperature oxidation device (6), a cooling device (7) and a conveying fan (8), wherein the pyrohydrolysis tank (2), the slurrying tank (1), the high-temperature oxidation device (6), the cooling device (7), the conveying fan (8) and the sludge storage tank (3) are sequentially communicated through a tail gas conveying pipeline (9).
2. The sludge pyrohydrolysis system of claim 1, wherein: the thermal hydrolysis tank (2) adopts a sequencing batch reactor.
3. The sludge pyrohydrolysis system of claim 1, wherein: the sludge storage tank (3) adopts a complete mixing type reactor.
4. The sludge pyrohydrolysis system of claim 1, wherein: the high-temperature oxidation device (6) comprises an incinerator.
5. The sludge pyrohydrolysis system according to any one of claims 1 to 4, wherein: the cooling device (7) is a spraying cooling device which is communicated with the sludge storage tank (3) through a spraying water conveying pipeline (10).
6. The sludge pyrohydrolysis system of claim 5, wherein: and at least three tail gas conveying pipelines (9) are uniformly arranged at the bottom of the sludge storage tank (3).
7. A sludge anaerobic digestion system comprises an anaerobic digestion tank (4), and is characterized in that: the sludge pyrohydrolysis system as claimed in any one of claims 1 to 6, wherein the sludge storage tank (3) is in communication with the anaerobic digestion tank (4) via a sludge transfer pipe (5), and the anaerobic digestion tank (4) is in communication with the high temperature oxidation device (6) via a biogas transfer pipe (11).
8. The sludge anaerobic digestion system as claimed in claim 7, wherein: the anaerobic digestion tank (4) adopts a complete mixing type reactor.
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| CN105561778A (en) * | 2016-03-09 | 2016-05-11 | 深圳市兴能保环境科技有限公司 | Method and device for treating high-concentration odor produced by sludge thermal hydrolysis process |
| CN206435049U (en) * | 2016-12-29 | 2017-08-25 | 湖南军信环保股份有限公司 | A kind of device for the high concentration foul gas processing that sludge pyrohydrolysis is produced |
| CN106621791B (en) * | 2016-12-29 | 2022-11-29 | 湖南军信环保股份有限公司 | Method and device for treating high-concentration malodorous gas generated by sludge pyrohydrolysis |
| CN108423959A (en) * | 2018-02-11 | 2018-08-21 | 浙江合泽环境科技股份有限公司 | A kind of Sludge resource utilization method based on pyrohydrolysis-pyrolysis charring |
| CN108773992A (en) * | 2018-04-02 | 2018-11-09 | 苏伊士水务工程有限责任公司 | Sludge treatment system and method for treating sludge by using same |
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| CN209065710U (en) * | 2018-09-06 | 2019-07-05 | 昆山绿威环保科技有限公司 | Quick processing system is combined in sludge pyrohydrolysis solar low-temperature film anaerobic digestion |
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