CN105417777B - Sewage Coagulation, Adsorption, Sedimentation and Separation—Separation Anaerobic Biogas Regeneration Treatment Method - Google Patents

Abstract

The invention belongs to the technical field of sewage treatment in environmental engineering, and relates to a technology for recycling sewage through coagulation, adsorption, precipitation and separation and separator anaerobic biogas gasification regeneration. A part of biogas generated by the anaerobic reaction is used for the heat preservation of the anaerobic reactor, so that the anaerobic treatment efficiency is improved, and the effective treatment can be ensured all the year round. The anaerobic treatment is also a regeneration process of the flocculant adsorbent, and anaerobic biochemical residues can return to an adsorption flocculation sedimentation process to be used as an adsorption flocculant for the second time. And (3) dehydrating a part of redundant anaerobic residues losing the adsorption capacity periodically, then incinerating the dehydrated part of the anaerobic residues by using part of biogas, and discharging the dehydrated part of the anaerobic residues after thorough harmless treatment. Meanwhile, the process also incinerates the persistent pollutants adsorbed on the residues.

Description

Sewage Coagulation, Adsorption, Sedimentation and Separation—Separation Anaerobic Biogas Regeneration Treatment Method

technical field

The invention belongs to the technical field of sewage treatment in environmental engineering, and relates to a sewage coagulation, adsorption, sedimentation separation-separation anaerobic biogasification regeneration treatment method.

Background technique

At present, the contradiction between economic development and environmental pollution seriously restricts the development speed of our country and the world economy. We are faced with two major problems: serious water pollution and shortage of water resources. As a cost-effective environmental engineering technology, biological treatment technology has been widely used for more than 100 years, and has played a very important role in environmental protection. However, the large area and high operating costs are still the Achilles heel of biological treatment. People are committed to developing more efficient and energy-saving sewage treatment technologies. Recently, zero-energy resource-based sewage treatment technology has attracted people's attention and has been criticized. The core of sewage biological treatment is the biodegradation and harmlessness of pollutants in sewage, which can be divided into two steps: one is the transfer of pollutants from the water phase to the biological phase; the other is the biochemical process of pollutants in the biological phase. transform. In the first process, it is mainly a physical diffusion process. The higher the concentration of pollutants around the biophase, the faster the diffusion speed and the greater the speed of entering the biophase. For medium and high concentration sewage treatment, the pollutants in the raw water have already If it is high enough, the diffusion transfer rate is basically compatible with the biodegradation rate. For low-concentration sewage treatment, it is necessary to use an appropriate method to concentrate the pollutant concentration so that it can quickly diffuse into the biological phase and perform rapid biodegradation. In the second process, one is to use aerobic microorganisms to carry out the aerobic conversion of pollutants. For hydrocarbon pollutants, the target products are carbon dioxide and water. Although the pollutants are completely transformed in this process, a large amount of molecular oxygen is consumed. , become the largest energy consumption of sewage treatment, the heat generated by the biochemical process is directly taken away by the wastewater, which is difficult to recover; the second is to use anaerobic microorganisms to transform pollutants. For hydrocarbon pollutants, the target products are methane and a small amount of hydrogen Carbon dioxide and water, the key is not to provide molecular oxygen, which reduces energy consumption, and there is energy output during the treatment process, and the higher the concentration of pollutants, the greater the production capacity. More importantly, anaerobic treatment can be achieved due to the limitation of no oxygen supply capacity. Accommodates very high organic concentrations, either raw or enriched. At the same time, a lot of research work has shown that due to the difference between anaerobic and aerobic biochemical processes, the ability and types of pollutants are also very different. Although anaerobic organisms grow slowly and the transformation speed of pollutants is slow, they can There are many types of pollutants and a high tolerance to toxic and harmful pollutants, so that a large number of pollutants can be anaerobically transformed within a long enough pollutant-biological contact time.

Contents of the invention

Based on the above idea, and aiming at the deficiencies in the existing sewage treatment technology, the present invention adopts coagulation and adsorption materials to enrich and separate the pollutants in the sewage, and the separation goal is to make the sewage meet the discharge and reuse standards. Firstly, the sewage is turned into a resource, and the separated pollutants are sent to an anaerobic bioreactor to convert the pollutants into biogas, and then the pollutants are turned into resources. Part of the biogas generated by anaerobic is used for the heat preservation of the anaerobic reactor to improve the anaerobic treatment efficiency and ensure effective treatment throughout the year. Anaerobic treatment is also the regeneration process of flocculant and adsorbent, and the anaerobic biochemical residue can be returned to the adsorption, flocculation and sedimentation process, and used as an adsorption flocculant for the second time. Regularly dehydrate a part of the excess anaerobic residue that has lost its adsorption capacity, then incinerate with part of the biogas, and discharge it after being completely harmless. At the same time, the process also incinerates the persistent pollutants adsorbed on the residue.

The technical solution of the present invention is: sewage coagulation, adsorption, sedimentation and separation-separation anaerobic biogasification regeneration treatment technology, the process flow is: collect domestic and various industrial wastewater in the sewage collection pool, and send the sewage to the sewage collection tank by the sewage lifting pump Go to the coagulation and adsorption comprehensive reaction tank for coagulation and adsorption reaction, coagulate the pollutants in the water into flocs, and at the same time adsorb the water-soluble pollutants on the adsorbent, and the sewage containing flocs and granular adsorbents enters the sedimentation tank The supernatant after sedimentation and separation enters the chemical precipitation recovery nitrogen and phosphorus compound fertilizer reaction tank, and the sewage after precipitation and separation in the sedimentation recovery tank is discharged or reused after disinfection, and the sewage containing suspended solids and adsorbents that is precipitated and separated in the sedimentation tank The sludge is transported to the anaerobic reactor with a sludge pump for anaerobic biogas treatment of the sludge. The biogas generated in the anaerobic reactor is discharged from the top of the reactor and enters the desulfurizer. After hydrogen sulfide is removed, the biogas enters the biogas The boiler burner burns, and the hot water produced is recycled as the heating heat source of the anaerobic reactor. In the anaerobic reactor, biodegraded biogas residues, regenerated adsorbents and flocculants that degrade organic matter are mixed. After dehydration, most of the biogas residue is returned to the coagulation adsorption reaction tank, and is reused to adsorb coagulation pollutants; after repeated use of the remaining coagulation adsorbent loses its removal function, it is dehydrated by the dehydrator and used The exhaust gas is burned by the biogas combustion boiler and dehydrated in the exhaust gas dryer. The dehydrated dry mud enters the second-stage solid waste combustion section of the biogas combustion furnace for incineration, which is completely harmless. , The washing water is returned to the sewage treatment system for secondary treatment.

The anaerobic reactor is composed of sludge dryer, biogas storage area, solid-liquid separation area, circulating water outlet, internal circulation pump, circulating liquid inlet, circulating liquid distributor, biogas residue sedimentation area, slag accumulation hopper, slag discharge control valve and The sludge pump is composed of a mud pump, and the sludge dryer is composed of a steel container, which is coated with anti-corrosion materials. The top of the equipment is equipped with a sedimentation separation area. The upper part of the sedimentation separation area is a biogas storage area, and the lower part is a solid-liquid separation area. There is an internal circulating water outlet at the bottom, and the two ends of the internal circulating pump are respectively connected with the internal circulating water outlet and the circulating fluid inlet. The anaerobic equipment is equipped with a circulating fluid distributor, and the bottom of the anaerobic reactor is equipped with a biogas residue sedimentation area. And the slag hopper, the bottom of the biogas slag sedimentation area is provided with a slagging control valve, and the slag hopper is connected with the mud pump; the concentration of the wastewater pollutants treated by the present invention is 50-50000 mg/liter, and the flocculant It is aluminum salt, iron salt, silicon salt, starch base and cellulose base, methyl ketone base, biological flocculant, polyacrylic acid series, polyacrylamide series, the adsorbent is activated carbon, fly ash, diatomaceous earth, zeolite, Macroporous resin or ion exchange resin. The coagulation adsorption reaction pool can be designed as one-stage or multi-stage. The number of sedimentation tanks is determined by the number of coagulation adsorption tanks, and the two are in a corresponding relationship. The design of the residence time of the sedimentation tank varies according to the properties of the selected coagulant and adsorbent, in order to achieve a good sedimentation effect, and the suspended solid concentration of the supernatant does not exceed the sewage discharge standard and does not exceed the reuse standard for reuse.

In order to more strictly control the discharge of nutrient elements nitrogen and phosphorus, the sewage that has been coagulated and adsorbed is then chemically precipitated to remove soluble nitrogen and phosphorus. According to the nitrogen and phosphorus content and existing state of the sewage, the composite precipitation method can be used. Magnesium ammonium phosphate Breakpoint chlorination to remove nitrogen and precipitate phosphorus at the same time, and separate precipitation method calcium, aluminum, iron and other inorganic salts.

After the biogas produced by the anaerobic reactor is discharged from the top of the reactor, it enters the desulfurization unit. After the hydrogen sulfide is removed, the biogas enters the biogas boiler burner for combustion, and the hot water generated is recycled as the heating source of the anaerobic reactor. Wet sodium hydroxide is used to remove hydrogen sulfide, and the resulting sodium sulfide is crystallized and sold as a by-product. This system is included in the desulfurization system.

The drying of biogas residue after dehydration uses the biogas combustion furnace to directly burn the tail gas. On the one hand, the moisture in the biogas residue is evaporated, and on the other hand, the harmful substances in the tail gas of biogas combustion are also absorbed, and then the biogas residue enters the second stage of the biogas combustion furnace for incineration. Harmless, realize the self-purification process of exhaust gas, this part is included in the biogas boiler burner.

The beneficial effect of the present invention is: the present invention can handle the waste water of the inorganic pollutant of the concentration COD of low, middle and high concentration pollutant from 50 to 50000 mg/liter, especially for the treatment of low and middle concentration waste water. The volume of the adsorption coagulant after anaerobic treatment after coagulation adsorption concentration is greatly reduced, which not only saves the volume of the biochemical reactor, increases the gas production per unit volume, but also reduces the loss of biogas and heat loss.

Description of drawings

Fig. 1 is a process flow diagram of the present invention

Fig. 2 is the structural representation of anaerobic reactor of the present invention

In the figure: 1. Sewage collection tank, 2. Sewage lifting pump, 3. Coagulation and adsorption comprehensive reaction tank, 4. Settling tank, 5. Reaction tank, 6. Sedimentation recovery tank, 7. Sludge pump, 8. Anaerobic Reactor, 9. Desulfurizer, 10. Biogas boiler burner, 11. Sludge dehydrator, 12. Tail gas scrubber, 13. Sludge dryer, 14. Sedimentation separation area, 15. Biogas storage area, 16. Solid Liquid separation area, 17, circulating water outlet, 18, internal circulation pump, 19, circulating liquid inlet, 20, circulating liquid distributor, 21, biogas residue sedimentation area, 22, slag accumulation hopper, 23, slag discharge control valve, 24 , Mud pump.

Detailed ways

Below in conjunction with Fig. 1, Fig. 2 and embodiment the present invention will be further described:

The technical solution of the present invention is: sewage coagulation, adsorption, sedimentation and separation-separation anaerobic biogasification regeneration treatment technology, and its process flow is: collecting domestic and various industrial wastewater in sewage collection pool 1, and sewage lifting pump 2 Sewage is sent to coagulation and adsorption comprehensive reaction tank 3 for coagulation and adsorption reaction, the pollutants in the water are coagulated into flocs, and water-soluble pollutants are adsorbed on the adsorbent at the same time, and the sewage containing flocs and particle adsorbents enters the In the sedimentation tank 4, the supernatant after sedimentation and separation enters the reaction tank 5 for chemical precipitation and recovery of nitrogen and phosphorus compound fertilizers. After sedimentation and separation in the sedimentation recovery tank 6, the sewage is discharged or sterilized and reused. The sludge of suspended matter and adsorbent is transported to the anaerobic bioreactor 8 by the sludge pump 7, and the anaerobic biogas treatment of the sludge is performed. The anaerobic biogas is sent to the biogas boiler burner 10 after the hydrogen sulfide is removed by the desulfurizer 9, and the hot water generated by combustion is used for heating and heat preservation of the anaerobic reactor 8, and undergoes biodegradation in the anaerobic reactor 8 After dehydration, most of the mixed biogas residues are returned to the coagulation and adsorption comprehensive reaction tank 3, and are used again to adsorb coagulation pollutants; After the recycled residual coagulation adsorbent loses its removal function, it is dehydrated by the dehydrator 11, and the combustion tail gas of the biogas boiler burner 10 is dehydrated in the tail gas dryer 13, and the dehydrated dry mud enters the biogas boiler burner 10 again. The second-stage solid waste combustion section is incinerated and completely harmless. The dry and dehydrated tail gas is discharged after being deodorized by the tail gas scrubber 12, and the washing water is returned to the sewage treatment system for secondary treatment.

The anaerobic reactor 8 is composed of a sludge dryer 13, a biogas storage area 15, a solid-liquid separation area 16, a circulating water outlet 17, an internal circulation pump 18, a circulating liquid inlet 19, a circulating liquid distributor 20, a biogas residue sedimentation area 21, The slagging hopper 22, the slagging control valve 23 and the mud pump 24 are composed. The sludge dryer 13 is composed of a steel container, which is coated with anti-corrosion materials. The top of the equipment is equipped with a sedimentation separation area 14, and the upper part of the sedimentation separation area 14 is used for biogas storage. District 15, the bottom is a solid-liquid separation zone 16, the lower half of the solid-liquid separation zone 16 is provided with an internal circulation water outlet 17, and the two ends of the internal circulation pump 18 are connected with the internal circulation water outlet 17 and the circulation liquid inlet 19 respectively, Oxygen equipment 8 is provided with a circulating liquid distributor 20, the bottom of the anaerobic reactor 8 is provided with a biogas residue sedimentation area 21 and a slag accumulation hopper 22, and the lower part of the biogas residue sedimentation area 21 is equipped with a slag discharge control valve 23, and a slag accumulation hopper 22 is connected with the mud pump 24; the mud pump 24 returns most of the mud to the coagulation and adsorption comprehensive reaction tank 3 for secondary use, and a small amount is discharged to the sludge dehydrator 11, and then enters the sludge dryer 13, and then the dried sludge Enter the biogas boiler burner 10, and discharge the inorganic residue after incineration. The anaerobic reactor 8 is the key equipment of this technology, it receives the flocculation and sedimentation products from the sedimentation tank 6 and the adsorbent that adsorbs the pollutants, the anaerobic reactor 8 is a combination of an anaerobic fluidized bed with external circulation and a packed bed In the reactor, the feed port is at the upper middle, and the discharge port is at the bottom. The material enters from the upper middle and then slowly descends to the bottom. At the same time, the internal circulation power continuously promotes the material to move upward, forming a fluidized state, improving the mass transfer effect, and increasing the biogas. The process also facilitates the suspension of the material. The generated biogas is collected at the top of the reactor and automatically enters the biogas storage tank and subsequent desulfurization combustion system.

The key design parameters of the anaerobic reactor volume load and effective volume design parameters are shown in Table 1.

Table 1

The present invention can treat waste water of inorganic pollutants with low, medium and high concentration pollutants whose concentration COD is from 50 to 50,000 mg/liter, especially for low and medium concentration wastewater treatment, because it is directly used at this time For anaerobic treatment of this type of sewage, due to the low concentration of pollutants, the amount of biogas produced is small, and the biogas is dissolved in water and entrained by water and part of it is lost. Heating a large amount of low-concentration sewage requires more energy, and the heat taken away by drainage also lost to the environment. However, the volume of the adsorption coagulant after anaerobic treatment after coagulation adsorption concentration is greatly reduced, which not only saves the volume of the biochemical reactor, increases the gas production per unit volume, but also reduces the loss of biogas and heat loss.

The range of sewage water quality defined by the present invention is shown in Table 2.

Table 2

The flocculants described in the present invention include: commonly used aluminum salts, iron salts, silicon salts and other small molecules and polymer flocculants, commonly used natural and synthetic organic polymer flocculants such as starch-based, cellulose-based, methyl gram Su-based, biological flocculants, polyacrylic acid series, polyacrylamide series, etc., the basic principle of selection is to effectively flocculate and remove colloids, polymer compounds and other types of pollutants in water, regardless of their biodegradable Both biodegradable and non-biodegradable can be used. The biodegradable can be reused many times, and the biodegradable can be converted into biogas for recycling. It is determined through experimental selection when specifically treating sewage of different types and concentrations.

The relationship between the amount of different types of flocculants used in the present invention and the water quality is shown in Table 3.

table 3

The adsorbents selected in the present invention include: general adsorbents such as activated carbon, fly ash, diatomaceous earth, etc., specific adsorbents such as zeolite for adsorbing ammonia nitrogen, macroporous resin for adsorbing organic matter, ion exchange resin for adsorbing heavy metals, etc. Wait. The choice of adsorbent is to be able to adsorb and remove dissolved organic matter, inorganic heavy metal ions and nitrogen and phosphorus nutrients in sewage to a certain discharge standard. It is determined through experimental selection when specifically treating sewage with different properties and concentrations.

The relation between the adsorbent used in the present invention and usage amount and water quality is shown in Table 4.

Table 4

The coagulation adsorption reaction pool 3 can be designed as one-stage or multi-stage. It is determined according to the type and concentration of sewage. High-concentration multi-component sewage adopts multi-stage coagulation adsorption, and low-concentration simple components adopts one-stage coagulation adsorption. The determination of technology is determined by experimentation.

In the present invention, the relationship between the residence time and the series of the coagulation reaction and the water quality is set in Table 5.

table 5

The number of sedimentation tanks 4 is designed according to the number of coagulation adsorption tanks 3, and the two are in a one-to-one correspondence. The design of the residence time of the sedimentation tank varies according to the properties of the selected coagulant and adsorbent. In order to achieve a good sedimentation effect, the SS concentration of the suspended solids in the supernatant does not exceed the sewage discharge standard and does not exceed the reuse standard for reuse.

In order to more strictly control the discharge of nutrient elements nitrogen and phosphorus, the sewage that has been coagulated and adsorbed is then chemically precipitated to remove soluble nitrogen and phosphorus. According to the nitrogen and phosphorus content and existing state of the sewage, the composite precipitation method can be used. Magnesium ammonium phosphate Breakpoint chlorination to remove nitrogen and precipitate phosphorus at the same time, and separate precipitation method calcium, aluminum, iron and other inorganic salts.

The biogas produced by the anaerobic reactor 8 is discharged from the top of the reactor and enters the desulfurizer 9. After the hydrogen sulfide is removed, the biogas enters the biogas boiler burner 10 for combustion, and the hot water generated is recycled as a heating source for the anaerobic reactor 8. . Wet sodium hydroxide is used to remove hydrogen sulfide, and the resulting sodium sulfide is crystallized and sold as a by-product. This system is included in the desulfurization system.

The drying of biogas residue after dehydration uses the biogas combustion furnace to directly burn the tail gas. On the one hand, the moisture in the biogas residue is evaporated, and on the other hand, the harmful substances in the tail gas of biogas combustion are also absorbed, and then the biogas residue enters the second stage of the biogas combustion furnace for incineration. Harmless, to realize the self-purification process of tail gas, this part is included in the burner 10 of the biogas boiler.

Example 1

When the sewage treatment capacity is 420 tons/hour or about 10,000 tons/day, the concentration of organic matter expressed in COD is 300 mg/liter, the concentration of organic matter after treatment is expressed in COD at 50 mg/liter, and the amount of COD removed per ton of water It is 0.25 kg, and the daily removal of COD is 2500 kg. The COD removed during the coagulation adsorption process is calculated as 0.8 g COD/g flocculation adsorbent dry basis, then the amount of flocculation adsorbent is: 3.13 tons/day, 1.30 tons/hour; The base coagulation adsorbent is 26 tons/hour. When the adsorption equilibrium time is designed to be 1 hour, the effective volume of the coagulation adsorption tank is 420 cubic meters, the dry basis coagulation adsorption amount is 1.30 tons, and the suspended solids concentration of the coagulation adsorption comprehensive reaction tank 3 is 0.3% 3000 mg/liter. The residence time of the settling tank 4 is 3 hours, the effective volume is 1260 cubic meters, the water content of the settled sludge is 95%, and the total volume of the settled sludge is 26 tons/hour. The hydraulic retention time of the flocculated and adsorbed sludge in the anaerobic reactor 8 is designed to be 96 hours, and the effective volume of the anaerobic reactor 8 is 26 tons/hour X 96 hours=2496 cubic meters. The removal volume load of the anaerobic reactor 8 is 2500 kg COD/day/2496 cubic meters = 1.00 kg COD/m3, day. Calculated on the basis of 0.4 cubic meters of biogas for every 1 kg of COD removed, the daily biogas production is 1,000 cubic meters. The methane content in biogas is calculated as 60%, the calorific value of biogas per cubic meter is: 21000-25000KJ/cubic meter, and the theoretical daily energy production is: 21-25MJ/day. The recycling rate of biogas residue is calculated as 96.7%, and 104 kg of residual biogas residue is discharged every day on a dry basis. The moisture content after dehydration by the sludge dewatering machine 11 is calculated as 80%, and 520 kg of wet residue is discharged every day, including 416 kg of water. According to the calculation of removing water at 30 degrees by evaporation, sensible heat of 20-100 degrees 139110KJ/day 0.139MJ/day is required to remove 416 kg of water, and latent heat of 100 degrees 973772.8KJ/day 0.974MJ/day is required to remove 416 kg of water. The amount of newly added biogas residue entering the anaerobic reactor 8 every day is: 21 tons/hour X 24 hours = 504 tons/day; the heat required to heat 520 tons of biogas residue from 20 degrees to 30 degrees is: 21736000KJ/day 21.736MJ /day, the sum of energy required by the three is: 22848882.8KJ/day 22.848 MJ/day. The heat is basically the same, without considering the heat released by incinerating 10% of the residue and the heat lost.

The sewage after flocculation and adsorption is assumed to contain 20 mg/liter of ammonia nitrogen and 3 mg/liter of phosphate, and the residual nitrogen and phosphorus are removed by oxidation-precipitation method to reach 8 mg/liter of ammonia nitrogen and 1 mg/liter of phosphate. The target of 1 liter needs to remove 12 mg/liter of ammonia nitrogen, 2 mg/liter of phosphate, and add 80 mg/liter of oxidation precipitant.

Example 2

When the sewage treatment capacity is 420 tons/hour or about 10,000 tons/day, the concentration of organic matter expressed in COD is 1000 mg/liter, and the concentration of organic matter after treatment is expressed in COD at 50 mg/liter, and the amount of COD removed per ton of water It is 0.95 kg, and the daily removal of COD is 9500 kg. The COD removed during the coagulation adsorption process is calculated as 0.8 g COD/g flocculation adsorbent dry basis, then the amount of flocculation adsorbent is: 11.875 tons/day, 0.5 tons/hour; The base coagulation adsorbent is 2.5 tons/hour. When the adsorption equilibrium time is designed to be 1 hour, the effective volume of the coagulation and adsorption comprehensive reaction tank 3 is 420 cubic meters, the dry basis coagulation and adsorption capacity is 2.5 tons, and the suspended matter concentration of the coagulation and adsorption comprehensive reaction tank 3 is 0.6% 6000 mg/liter . The residence time of the settling tank 4 is 3 hours, the effective volume is 1260 cubic meters, the moisture content of the settled sludge is 95%, and the total volume of the settled sludge is 50 tons/hour. The water residence time of the sludge after flocculation and adsorption in the anaerobic reactor 8 is designed to be 96 hours, and the effective volume of the anaerobic reactor 8 is 50 tons/hour X 96 hours = 4800 cubic meters. The removal volume load of the anaerobic reactor 8 is 9500 kg COD/day/4800 cubic meters = 1.98 kg COD/m3, day. Calculated on the basis of 0.4 cubic meters of biogas for every 1 kg of COD removed, the daily biogas production is 3,800 cubic meters. The methane content in biogas is calculated as 60%, the calorific value of biogas per cubic meter is: 21000-25000KJ/cubic meter, and the theoretical daily energy production is: 79.8-95MJ/day. The recycling rate of biogas residue is calculated as 96%, and 400 kg of residual biogas residue is discharged every day on a dry basis. The moisture content after dehydration by the sludge dewatering machine 11 is calculated as 80%, and 2,000 kg of wet residue is discharged every day, including 1,600 kg of water. According to the calculation of moisture removal at 30 degrees by evaporation, sensible heat of 20-100 degrees, 528618KJ/day and 0.529MJ/day is required to remove 1600 kg of water, and latent heat of 100 degrees, 3700336.6KJ/day and 3.70MJ/day is required to remove 1600 kg of water. The amount of newly added biogas residue entering the anaerobic reactor 8 every day is: 80 tons/hour X 24 hours = 1920 tons/day; the heat required to heat 1920 tons of biogas residue from 20 degrees to 30 degrees is: 80055360KJ/day 80.055MJ /day, the sum of energy required by the three is: 84284314.6KJ/day 84.284 MJ/day. The heat is basically the same, without considering the heat released by incinerating 10% of the residue and the heat lost.

The sewage after flocculation and adsorption is assumed to contain 60 mg/liter of ammonia nitrogen and 10 mg/liter of phosphate, and the residual nitrogen and phosphorus are removed by oxidation-precipitation method to reach 8 mg/liter of ammonia nitrogen and 1 mg/liter of phosphate. The target of 1 liter needs to remove 52 mg/liter of ammonia nitrogen, 9 mg/liter of phosphate, and add 400 mg/liter of oxidation precipitant.

Example 3

When the sewage treatment capacity is 420 tons/hour or about 10,000 tons/day, the concentration of organic matter expressed in COD is 10,000 mg/liter, and the concentration of organic matter after treatment is expressed in COD at 50 mg/liter, and the amount of COD removed per ton of water It is 9.95 kg, and the daily removal of COD is 99,500 kg. The COD removed during the coagulation adsorption process is calculated as 0.8 g COD/g flocculation adsorbent dry basis, then the amount of flocculation adsorbent is: 124 tons/day, 5.18 tons/hour; The base coagulation adsorbent is 103.6 tons/hour. When the adsorption equilibrium time is designed to be 10 hours, the effective volume of the coagulation-adsorption comprehensive reaction tank 3 is 4200 cubic meters (designed as a three-stage countercurrent flocculation adsorption, the dry basis coagulation adsorption amount is 51.8 tons, and the suspended solids in the coagulation-adsorption comprehensive reaction tank 3 Concentration 1.2% 12000 mg/liter. The residence time of settling tank 4 is 10 hours, and effective volume is 4200 cubic meters, and the moisture content of sedimentation sludge is 95%, and the total volume of sedimentation sludge is 103.6 tons/hour. Flocculation adsorption The hydraulic retention time of the final sludge in the anaerobic reactor is designed to be 96 hours, and the effective volume of the anaerobic reactor 8 is 103.6 tons/hour * 96 hours=9945.6 cubic meters. The removal volume load of the anaerobic reactor is 99,500 kg COD/day/9945.6 cubic meters = 10.00 kg COD/m3, day. Calculated on the basis of 0.4 cubic meters of biogas produced per 1 kg of COD removed, the daily biogas production is 39,800 cubic meters. The methane content in biogas is calculated as 60%. The calorific value of m3 biogas is: 21000-25000KJ/m3, and the theoretical daily energy output is: 835.8-995MJ/day. The recycling rate of biogas residue is calculated according to 97%, and 4150 kg of residual biogas residue is discharged every day on a dry basis. The dehydrator 11 The moisture content after dehydration is calculated according to 80%, and 20,750 kg of wet residue is discharged every day, including 16,600 kg of water. According to the calculation of moisture removal at 30 degrees by evaporation, the removal of 16,600 kg of water requires sensible heat of 20-100 degrees, 5488375KJ/day 5.49MJ /day, removing 16600 kg of moisture requires latent heat of 100 degrees 142140992.2KJ/day 14.21MJ/day. The amount of new biogas residue entering the anaerobic reactor 8 every day is: 829 tons/hour X 24 hours=19896 tons/day; heating The heat required to raise the temperature from 20 degrees to 30 degrees for 19896 tons of biogas residues is: 829573668KJ/day 829.573MJ/day, and the total energy required by the three is: 977203035.2KJ/day 977.203 MJ/day. The heat is basically the same, and 10% of the incineration is not considered The heat released by the residue and the heat lost.

The sewage after flocculation and adsorption is assumed to contain 500 mg/liter of ammonia nitrogen and 100 mg/liter of phosphate, and the residual nitrogen and phosphorus are removed by oxidation-precipitation method to reach 8 mg/liter of ammonia nitrogen and 1 mg/liter of phosphate. The target of 1 liter needs to remove 492 mg/liter of ammonia nitrogen, 99 mg/liter of phosphate, and add 4000 mg/liter of oxidation precipitant.

Claims (7)

1. sewage Coagulation and Adsorption precipitates separation-isolate anaerobic methane regeneration treating method, it is characterised in that its technique stream Cheng Shi：It will live and all types of industries wastewater collection is in sewage collecting pool（1）In, by sewage pump（2）Sewage is delivered into coagulation Adsorb combined reaction pond（3）Coagulation and Adsorption reaction is carried out, by water pollutant coagulation into floccule, while by water soluble contaminants It is adsorbed onto on adsorbent, the sewage containing flocculate and granule adsorbent enters settling tank（4）In, the supernatant after sedimentation separation Liquid enters chemical precipitation recovery compound nitrogen phosphate fertilizer reaction tank（5）, by precipitating recovery pond（6）Sewage discharge after precipitation separation Or reuse after sterilization, in settling tank（4）The sludge sludge pump containing suspension and adsorbent of middle precipitation separation（7）It is transported to Anaerobic reactor（8）In, carry out the anaerobic methaneization processing of sludge, anaerobic reactor（8）Caused biogas is from reactor head After discharge, into devulcanizer（9）, after removing hydrogen sulfide, biogas enters methane boiler burner（10）Burning, caused hot water are made For anaerobic reactor（8）Heat source recycle, in anaerobic reactor（8）Middle biogas residue after biodegradation, contain Adsorbent and the flocculant for degrading organic matter after regeneration, are largely returned to Coagulation and Adsorption synthesis after mixing biogas residue dehydration Reaction tank（3）In, reuse in absorption and coagulation pollutant；It is de- that it is lost by the remaining Coagulation and Adsorption agent being recycled for multiple times After function, then by dewaterer（11）After dehydration, with methane boiler burner（10）Combustion tail gas, in tail gas drying machine (13) Dehydration, the dry mud after dehydration enter back into methane boiler burner（10）Second level solid waste burning zone burn, it is thoroughly innoxious, do The tail gas of dry dehydration passes through exhaust scrubber（12）Discharged after taste removal, washings return to sewage disposal system after-treatment.

2. sewage Coagulation and Adsorption according to claim 1 precipitates separation-isolate anaerobic methane regeneration treating method, Characterized in that, described anaerobic reactor（8）Include sludge drier（13）, biogas storage area（15）, solid-liquid displacement zone （16）, circulating water outlet（17）, internal circulation pump（18）, circulation fluid import（19）, recycle liquid distributor（20）, biogas residue settling zone （21）, accumulated slag bucket（22）, letting cinder control valve（23）And slush pump（24）, equipment body is made up of steel vessel, and inside scribbles Anti-corrosion material, equipment top are provided with sedimentation separation area（14）, sedimentation separation area（14）Top is biogas storage area（15）, bottom For solid-liquid displacement zone（16）, solid-liquid displacement zone（16）Lower half is provided with interior circulating water outlet（17）, internal circulation pump（18）Both ends Respectively with interior circulating water outlet（17）With circulation fluid import（19）It is connected, anaerobic reactor（8）Inside is provided with circulation fluid and is distributed Device（20）, anaerobic reactor（8）Bottom be provided with biogas residue settling zone（21）With accumulated slag bucket（22）, biogas residue settling zone（21）Bottom Provided with letting cinder control valve（23）, accumulated slag bucket（22）With slush pump（24）It is connected.

3. sewage Coagulation and Adsorption according to claim 1 precipitates separation-isolate anaerobic methane regeneration treating method, Characterized in that, the COD of described Wastewater Pollutant concentration is 50-50000 mg/litres.

4. sewage Coagulation and Adsorption according to claim 1 precipitates separation-isolate anaerobic methane regeneration treating method, Characterized in that, described flocculant is aluminium salt, and molysite, silicon salt, starch-based flocculant, cellulose base flocculant, chitin base Flocculant, biological flocculant, polyacrylic acid series flocculant or polyacrylamide series flocculant.

5. sewage Coagulation and Adsorption according to claim 1 precipitates separation-isolate anaerobic methane regeneration treating method, Characterized in that, described adsorbent is activated carbon, flyash, diatomite, zeolite, macroreticular resin or ion exchange resin.

6. sewage Coagulation and Adsorption according to claim 1 precipitates separation-isolate anaerobic methane regeneration treating method, Characterized in that, described Coagulation and Adsorption combined reaction pond（3）One-level or multistage can be designed to.

7. sewage Coagulation and Adsorption according to claim 1 precipitates separation-isolate anaerobic methane regeneration treating method, Characterized in that, described settling tank（4）Quantity by Coagulation and Adsorption combined reaction pond（3）Quantity determine, both for pair It should be related to.