CN214881022U - Utilize sewage treatment system of sewage plant mud resourceization generation carbon source - Google Patents
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Abstract
The utility model discloses a sewage treatment system for generating carbon source by utilizing sludge resource of a sewage plant, which comprises a main stream system, a side stream system and a sludge concentration tank, wherein the main stream system comprises a main stream mixed liquid fermentation tank, a biological denitrification dephosphorization system and a secondary sedimentation tank which are sequentially connected through pipelines, the main stream mixed liquid fermentation tank is connected with a sewage inlet, the secondary sedimentation tank is connected with a sewage outlet, the side stream system comprises a side stream pretreatment reaction tank and a side stream hydrolysis acidification tank which are sequentially connected through pipelines, the sludge outlet of the secondary sedimentation tank is respectively connected with the sludge concentration tank, the water inlet end of the main stream mixed liquid fermentation tank, the biological denitrification dephosphorization system and the side stream pretreatment reaction tank, the outlet of the side stream hydrolysis acidification tank is connected with the main stream mixed liquid fermentation tank, a drug adding system for adding drugs is arranged on the inlet of the side flow pretreatment reaction tank, and a sludge outlet is arranged on the sludge concentration tank. The treatment system of the utility model not only promotes the effect of biological nitrogen and phosphorus removal, but also realizes the consumption reduction of carbon sources.
Description
Technical Field
The utility model relates to a sewage plant sludge treatment and sewage treatment field specifically are an utilize sewage treatment system of sewage plant mud resourceful generation carbon source.
Background
The biological denitrification mainly comprises the steps of oxidizing ammonia nitrogen into nitrate nitrogen or nitrite nitrogen in an aerobic tank by nitrifying bacteria, then refluxing muddy water mixed liquor in the aerobic tank to a front-end anoxic tank through an internal reflux pump, and converting the nitrate nitrogen or nitrite nitrogen into nitrogen through a denitrification process so as to realize effective removal of total nitrogen. The biological phosphorus removal is realized by phosphorus-accumulating bacteria releasing phosphorus in an anaerobic tank by using a carbon source, and then absorbing phosphorus in an aerobic tank and discharging excess sludge. In order to realize effective biological nitrogen and phosphorus removal, the COD/TN of the inlet water is generally recommended to be not less than 6, and the COD rCOD/TP of the easy biochemical water is not less than 18. And the sewage plant in China generally faces the problem of low carbon-nitrogen ratio of inlet water, so that the nitrogen and phosphorus removal efficiency of a biological system is low. In order to discharge the effluent total nitrogen and total phosphorus after reaching the standard, a sewage plant usually needs to add carbon sources such as glucose, sodium acetate and methanol to promote the biological nitrogen and phosphorus removal effect, so that the medicament cost of the operation of the sewage plant is greatly increased, and the sludge yield and the treatment cost of the sewage plant are increased. Therefore, how to reduce the consumption of carbon source and drug consumption while ensuring effective removal of total nitrogen and total phosphorus is an urgent need of many sewage plants.
The main components of the sludge are macromolecular compounds such as protein, carbohydrate and the like, under the anaerobic condition, the sludge can realize cell wall breaking through hydrolysis, the macromolecular protein and carbohydrate can be hydrolyzed into simple micromolecular substances by using hydrolase, the micromolecular substances are further acidified to generate volatile organic acid, and the volatile organic acid generated by sludge hydrolysis acidification is mainly acetic acid, propionic acid and butyric acid generally; the organic volatile acid can be used as a carbon source for biological nitrogen and phosphorus removal. However, the hydrolysis process of sludge is a slow biochemical process, so in order to achieve effective hydrolysis of sludge, it is generally necessary to construct a large hydrolysis tank to maintain a long residence time, which increases the floor space and investment. In order to effectively perform the processes of breaking cell walls and promoting hydrolysis of sludge, the sludge can be pretreated, and the commonly used pretreatment of the sludge can be performed by adding an oxidant, adding acid to reduce pH, adding alkali to increase pH, heating to raise temperature, pressurizing or performing cell wall breaking by using ultrasonic waves; at present, the measures are mainly applied to the process of generating the biogas by anaerobic sludge digestion, and the sludge is pretreated and then directly enters an anaerobic digestion tank to promote the digestion of the sludge and the yield of the biogas. Some of the published patent processes have begun to attempt to produce carbon sources by alkaline fermentation after increasing the pH of the sludge by adding liquid alkali, and patent CN107265806A discloses pretreatment by raising the pH of the excess sludge to 10 with liquid alkali while maintaining the sludge at a temperature of 90 ℃ for 2 hours, followed by feeding into a hydrolytic acidification tank, and hydrolytic acidification by an alkaline fermentation process of acclimatizing from the initial pH 6 to pH10 by gradually raising the pH from 6 to 10. The patent CN110282841A discloses a method for alkaline fermentation of sludge by adjusting the hydrolytic acidification tank to pH 10. The method disclosed by the patent also utilizes ultrasonic waves to break the wall of sludge to generate a carbon source, and the method disclosed by the patent CN108439741A is characterized in that 30-50% of sludge is shunted from residual sludge to an ultrasonic wall breaking device, the sludge is conveyed to a hydrolysis tank for hydrolysis after wall breaking pretreatment, and the sludge after wall breaking hydrolysis is returned to a sewage biochemical treatment system for treatment. In addition, a method for directly hydrolyzing sludge by a biological method to generate a carbon source is disclosed in the patent, and the method disclosed in CN104118971B is to reflux part of secondary sedimentation backflow sludge to a primary sedimentation tank, perform hydrolytic fermentation after the primary sedimentation tank and the primary sedimentation sludge are mixed and concentrated, and realize sludge fermentation to provide the carbon source by adopting aeration and stirring to alternately control micro-aerobic and anaerobic conditions during fermentation. In addition, Envidan corporation of Denmark also proposed ASP/SSH (activated sludge recirculation/sidestream sludge hydrolysis) process to realize the carbon source generation of sludge in sidestream hydrolysis to promote the denitrification and dephosphorization of biochemical system, wherein aeration and stirring are used to alternately control the micro-aerobic and anaerobic conditions in the hydrolysis acidification tank to realize the sludge fermentation to provide carbon source.
The condition of sludge alkaline fermentation needs to be controlled to 10, and the drug consumption of liquid caustic soda is higher. The method for breaking the wall of the sludge by ultrasonic waves has higher power consumption. The method for mixing the sludge in the secondary sedimentation tank and the primary sedimentation sludge in the primary sedimentation tank for fermentation is mainly a mainstream anaerobic fermentation process, and can limit the market popularization of the method because of the need of the primary sedimentation tank. The method of the EnviDan company is a process of sidestream sludge hydrolysis. The latter two biological hydrolysis processes both utilize an aeration and agitation alternating mode of operation.
So far, how to effectively combine efficient and economical sludge pretreatment, side stream sludge hydrolytic acidification and mainstream mixed liquor fermentation to realize the maximum resource utilization of sludge to generate carbon source is a new topic.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide an utilize sewage treatment system of sewage plant mud resourceful generation carbon source, through the hydrolysis of the mud preliminary treatment promotion mud of high-efficient economy to and combine together the preliminary treatment of mud, the hydrolytic acidification of sidestream and the hydrolysis fermentation of mainstream effectively and realize mud through hydrolytic acidification generation carbon source in order to reach the resourceful and the purpose that reduces biological nitrogen and phosphorus removal's medicament cost of mud.
In order to solve the technical problem, the utility model discloses a technical scheme is: the utility model provides an utilize sewage treatment system of sewage factory mud resourceization generation carbon source, including mainstream system, sidestream system and sludge concentration tank, the mainstream system includes the mixed liquid fermentation vat of mainstream, biological nitrogen and phosphorus removal system and the secondary sedimentation tank that connect gradually through the pipeline, the mixed liquid fermentation vat of mainstream links to each other with the water inlet of sewage, be connected with the sewage delivery port on the secondary sedimentation tank, the sidestream system includes sidestream preliminary treatment reaction tank and the hydrolysis acidification tank of sidestream that connects gradually through the pipeline, the mud export of secondary sedimentation tank respectively with sludge concentration tank, the end of intaking of the mixed liquid fermentation vat of mainstream, biological nitrogen and phosphorus removal system, the pretreatment reaction tank of sidestream links to each other, the export of hydrolysis acidification tank of sidestream links to each other with the mainstream fermentation vat, be provided with the medicine system that adds the medicament on the mixed liquid preliminary treatment reaction tank of sidestream, be provided with the mud discharge port on the sludge concentration tank.
The sludge concentration tank is also connected with the inlet of the side flow pretreatment reaction tank.
And a mechanical stirrer and an online pH monitor are arranged on the side flow pretreatment reaction tank.
The medicine feeding system is a pipeline mixer or a medicine feeding pump.
And a flow impeller is arranged in the side flow hydrolysis acidification tank.
The side-stream hydrolysis acidification tank and the side-stream pretreatment reaction tank are made into integrated equipment, and the middle of the equipment is separated by a partition wall or a partition plate.
The main flow mixed liquid fermentation tank is provided with a submersible water impeller.
And a sludge outlet of the secondary sedimentation tank is connected with the first tank of the biological nitrogen and phosphorus removal system or the foremost end of the biological nitrogen and phosphorus removal system.
The main stream biological nitrogen and phosphorus removal system is one of an anoxic/aerobic system, an anaerobic/anoxic/aerobic system, an oxidation ditch system with an anoxic section and an aerobic section, an oxidation ditch system with an anaerobic section/anoxic section/aerobic section, a multi-stage anoxic/aerobic system and an anaerobic + multi-stage anoxic/aerobic system.
The utility model has the advantages that:
the utility model discloses a sewage treatment system utilizes sludge pretreatment tank to carry out the preliminary broken wall back that the preliminary treatment realized sludge cell to partial backward flow mud at the sidestream and then gets into the sidestream hydrolysis acidification pond and strengthen hydrolysising and acidizing, and the muddy water mixed liquid of sidestream hydrolysis acidification discharges into the mainstream and mixes liquid fermentation tank and further ferment and generate more carbon sources. In addition, part of sludge refluxed by the secondary sedimentation tank is mixed with the inlet water of the sewage plant at the front end of the main stream fermentation tank to adsorb easily degradable organic matters in the inlet water and then enters the fermentation tank to be fermented into a carbon source, the main stream mixed liquid fermentation tank is not only fermented into the carbon source, but also can directly utilize the generated carbon source to carry out denitrification reaction to remove nitrate nitrogen and nitrite nitrogen brought back by the reflux of the sludge of the secondary sedimentation tank and contained in the inlet water of the sewage plant; and then, the residual carbon source after the nitrate nitrogen and the nitrite nitrogen are removed by the fermentation tank and the newly generated carbon source in the fermentation tank enter a subsequent biological nitrogen removal system along with the inflow water so as to provide the carbon source to promote the biological nitrogen and phosphorus removal.
The utility model discloses a sewage treatment system can couple sludge pretreatment, side stream hydrolytic acidification and mainstream and mix the liquid fermentation to realized the biggest resourceization of mud and generated more carbon sources, for the biological nitrogen and phosphorus removal system of mainstream provides the carbon source, realized carbon source consumption reduction's effect. Meanwhile, due to the hydrolysis acidification process of the sludge, organic matters in a part of the sludge are dissolved in water to become carbon sources for utilization due to hydrolysis and acidification, and thus, the effect of partial sludge reduction is realized.
The utility model discloses a preliminary broken wall of mud cell is realized to the preliminary treatment pond, and the hydrolysis of mud is accomplished by the mixed liquid fermentation vat of subsequent side flow hydrolysis acidification pool coupling mainstream mainly, and the oxidant that the mud preliminary treatment pond used or the dose of acid or alkali is more gentle, this operation cost with regard to greatly reduced mud preliminary treatment technology section to the maximize has realized the economic benefits that mud resourceization generated the carbon source, makes the utility model discloses wide market perspective has.
The utility model discloses not only be applicable to municipal waste water, also be applicable to non-municipal waste water, especially to those need throw the sewage plant that the carbon source realized that the total nitrogen of play water is up to standard, perhaps those because the carbon source is not enough to cause the unsatisfactory sewage plant that needs extra throwing chemical phosphorus removal agent of biological phosphorus removal effect.
Drawings
FIG. 1 is a block diagram of a sewage treatment system for generating carbon source by utilizing sludge resource of a sewage plant.
FIG. 2 is a block diagram showing another mode of the sewage treatment system for generating carbon source by utilizing sludge resources of a sewage plant according to the present invention.
Detailed Description
The technical solution in the embodiment of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiment of the present invention; obviously, the described embodiments are only a part of the embodiments of the present invention, and not all embodiments, and all other embodiments obtained by those skilled in the art without any inventive work are within the scope of the present invention based on the embodiments of the present invention.
As shown in figure 2, the utility model discloses a utilize sewage treatment system of sewage plant mud resourceful formation carbon source, including mainstream system, sidestream system and sludge concentration tank 4, the mainstream system includes mainstream mixed liquid fermentation tank 1, biological nitrogen and phosphorus removal system 2 and two heavy ponds 3 that connect gradually through the pipeline, mainstream mixed liquid fermentation tank 1 links to each other with the water inlet of sewage, be connected with the sewage delivery port on two heavy ponds 3, the sidestream system includes sidestream preliminary treatment reaction tank 5 and sidestream hydrolysis acidification tank 6 that connect gradually through the pipeline, the sludge outlet of two heavy ponds 3 respectively with sludge concentration tank 4, the water inlet end of mainstream mixed liquid fermentation tank 1, biological nitrogen and phosphorus removal system 2, sidestream preliminary treatment reaction tank 5 links to each other, the export of sidestream hydrolysis acidification tank 6 links to each other with mainstream mixed liquid fermentation tank 1, be provided with medicine system 7 that adds the medicament on sidestream preliminary treatment reaction tank 5 import, the sludge concentration tank 4 is provided with a sludge outlet.
As shown in FIG. 1, the sludge concentration tank 4 is also connected to the inlet of the sidestream pretreatment reaction tank 5.
The side flow pretreatment reaction tank 5 is provided with a mechanical stirrer and an online pH monitor. The medicine adding system 7 is a pipeline mixer or a medicine adding pump. And a flow impeller is arranged in the side-flow hydrolysis acidification tank 6. The main flow mixed liquid fermentation tank 1 is provided with a submersible water impeller.
Preferably, the side stream hydrolysis acidification tank 6 and the side stream pretreatment reaction tank 5 are integrated into a device, and are separated by a partition wall or a partition plate.
Preferably, the sludge outlet of the secondary sedimentation tank 3 is connected with the first tank of the biological nitrogen and phosphorus removal system 2 or the foremost end of the biological nitrogen and phosphorus removal system.
The main stream biological nitrogen and phosphorus removal system 2 is one of an anoxic/aerobic system, an anaerobic/anoxic/aerobic system, an oxidation ditch system with an anoxic section and an aerobic section, an oxidation ditch system with an anaerobic section/anoxic section/aerobic section, a multi-stage anoxic/aerobic system and an anaerobic + multi-stage anoxic/aerobic system.
The utility model discloses a sewage treatment system effectively combines mud preliminary treatment and hydrolytic acidification, and hydrolytic acidification has combined side stream hydrolytic acidification and mainstream mixed liquid anaerobic fermentation again simultaneously. In the secondary sedimentation tank return sludge, firstly, a part of return sludge is pretreated to realize the preliminary cell wall breaking, then the return sludge enters a side-stream hydrolysis acidification tank to carry out efficient hydrolysis and acidification, and then the return sludge returns to a main-stream mixed liquor fermentation tank to further ferment and generate more carbon sources. And the other part of the return sludge in the secondary sedimentation tank directly returns to the water inlet end of the main stream mixed liquid fermentation tank to be mixed with the water inlet of the sewage plant so as to adsorb easily degradable organic matters in the water inlet, and then the mixture enters the main stream mixed liquid fermentation tank to be subjected to hydrolytic fermentation to generate a carbon source and is also used as a strain for removing nitrate nitrogen by denitrification in the main stream mixed liquid fermentation tank. The last part of the return sludge of the secondary sedimentation tank returns to the first tank of the biological nitrogen and phosphorus removal system or the foremost end of the biological nitrogen and phosphorus removal system. The carbon source part generated by the main flow mixed liquid fermentation tank can be directly utilized in the fermentation tank to remove nitrate nitrogen and nitrite nitrogen contained in the inlet water or brought back by the backflow of the secondary sedimentation tank, and then enters a subsequent biological nitrogen and phosphorus removal system together with the inlet water to be utilized to promote the process of biological nitrogen and phosphorus removal, and simultaneously, the carbon source consumption reduction is realized.
The utility model discloses a mainly contained 3 steps among sewage treatment system's the processing method:
step 1 is to carry out the pretreatment step of the side stream sludge to realize the primary wall breaking process of the sludge cells. And guiding out partial sludge from the returned sludge of the secondary sedimentation tank for sludge pretreatment, wherein the amount of the guided-out returned sludge can be (2% -80%) Q (Q is the inflow rate) for sludge pretreatment. If the excess sludge of the sewage plant is mainly biochemical sludge, the excess biochemical sludge concentrated by the sludge concentration tank and ready to be sent to the sludge dehydration treatment can be divided into 1-80% of the amount to be sent to the sludge pretreatment process section for pretreatment. The sludge concentration in the sludge pretreatment process section may be 0.2-10%.
The preliminary cell wall breaking process of the sludge pretreatment can adopt the addition of an oxidant for oxidation reaction, and the oxidant can be hydrogen peroxide, sodium hypochlorite and ozone; the dosage of these oxidizing agents is 50-5000 mg/L. The sludge pretreatment can also control the pH at 2-7 by adding hydrochloric acid or sulfuric acid or can control the pH at 7-12 by adding liquid alkali to realize the primary wall breaking of cells. The sludge pretreatment can also be to add oxidant and acid respectively or add oxidant and alkali respectively to carry out the primary wall breaking of sludge cells. The sludge pretreatment can be completed in a reaction tank, the hydraulic retention time of the reaction tank is designed to be 0.1-24 hours, the reaction tank adopts a mechanical stirring mode, and the power of a stirrer used for mechanical stirring can be 3-30kw/1000m3An effective volume. The pretreatment reaction tank needs to be equipped with an on-line pH meter to monitor the change in pH. The pretreatment process segment can be in a continuous mode of operation or in a sequential batch mode of operation, and if in the sequential batch mode, can be run at 1-12 batches/day. The oxidant, acid or alkali required by the pretreatment process section can be added into the reaction tank by a dosing pump and mixed by mechanical stirring, or can be added into a pipeline and mixed by a pipeline mixer. If the medicament is added in a pipeline and mixed by a pipeline mixer, a mixing reaction tank can be connected behind the pipeline. If only acid or alkali is added, the pipeline can be connected with the mixing reaction tank or can be directly connected with the hydrolysis acidification tank without the mixing reaction tank, and meanwhile, the pipeline is also provided with online pH to monitor the change of the pH value.
And step 3, further performing anaerobic fermentation in the main flow mixed liquid fermentation tank. The main flow mixed liquid fermentation tank is arranged at the front end of the main flow biological nitrogen and phosphorus removal system. And discharging the sludge-water mixed liquor treated by the side-stream hydrolysis acidification tank into a main-stream mixed liquor fermentation tank for further fermentation to generate more carbon sources. 2-60% of Q in the return sludge of the secondary sedimentation tank also returns to the water inlet end of the main flow mixed liquid fermentation tank to be mixed with the inlet water of the sewage plant firstly, and organic matters which are easy to degrade in the inlet water are adsorbed, and the mixed mode of the return sludge of the secondary sedimentation tank and the inlet water of the sewage plant can directly adopt a hydraulic mixed mode or a mechanical stirring mode; and mixing and then entering a main flow mixed liquid fermentation tank. In the main flow mixed liquid fermentation tank, nitrate nitrogen and nitrite nitrogen brought back by return sludge in the secondary sedimentation tank and contained in inlet water of a sewage plant are removed by directly utilizing a carbon source generated by the side flow hydrolysis acidification tank and available COD contained in the inlet water in the main flow fermentation tank. And the carbon source remained after the nitrate nitrogen and the nitrite nitrogen are removed by the main flow mixed liquid fermentation tank and the carbon source newly generated by the sludge in the fermentation tank enter a subsequent biological nitrogen and phosphorus removal system along with the inflow water, so as to provide a carbon source for biological nitrogen and phosphorus removal. The hydraulic retention time of the main flow mixed liquid fermentation tank is 0.1-8 h. The main flow mixed liquid fermentation tank is provided with a submersible water impeller with the power of 3-30kw/1000m3An effective volume. The operation mode of the flow impeller of the main flow mixed liquid fermentation tank is intermittent stirring, and the total operation time of the flow impeller is 0.1-6 h/day to control the sludge age to be 2-60And (4) hours. If the municipal sewage plant is provided with the primary sedimentation tank, the primary sedimentation tank can be directly transformed into the main flow mixed liquid fermentation tank. For a newly-built sewage plant, if the sewage plant for treating non-municipal wastewater needs to remove some difficultly-degraded COD by using a pre-coagulation process section, a main-flow mixed liquid fermentation tank needs to be newly built behind a primary settling tank and in front of a biological nitrogen and phosphorus removal system in the sewage plant; in the case of municipal water and sewage plants, a mixed liquid fermentation tank can be directly built to replace a primary sedimentation tank, and the primary sedimentation sludge, secondary sedimentation tank sludge and sludge after side stream hydrolysis and acidification are directly mixed in a main mixed liquid fermentation tank for fermentation to generate a carbon source. If the existing sewage plant does not have redundant empty space to build the main flow mixed liquid fermentation tank, a section of tank can be isolated from the anaerobic tank or the anoxic tank to transform into the main flow mixed liquid fermentation tank.
The main stream of biological nitrogen and phosphorus removal system can be an anoxic/aerobic system, or an anaerobic/anoxic/aerobic system, or an oxidation ditch system with an anoxic section and an aerobic section, or an oxidation ditch system with an anaerobic section/anoxic section/aerobic section, or a multi-stage anoxic/aerobic system, or an anaerobic + multi-stage anoxic/aerobic system. The sludge reflowing from the secondary sedimentation tank is divided into a side stream pretreatment part, a hydrolysis acidification part and a part reflowing to the water inlet end of the main stream mixed liquid fermentation tank, and the rest reflowing sludge is reflowed to the first tank or the foremost end of the biological nitrogen and phosphorus removal tank to maintain the sludge concentration of a biochemical system.
Example 1
The concentration of sludge in a secondary sedimentation tank of a municipal sewage plant is 1.7 percent, the sludge is added with 1000mg/L sodium hypochlorite and mixed for 8 hours, then the mixture is added into a hydrolysis acidification tank which is equivalent to a side-stream sludge hydrolysis acidification process section, and the hydrolysis acidification tank is kept at room temperature for 12 hours to stay for running in a continuous CSTR mode. The soluble COD SCOD of the sludge after pretreatment and hydrolytic acidification is increased from the original 28mg/L to 898 mg/L. Then 100 ml of sludge-water mixed liquor which is pretreated by side-stream sludge and is subjected to hydrolytic acidification treatment is added into a 1L fermentation tank which is equivalent to a main mixed liquor, return sludge which is equivalent to 10 percent Q of a secondary sedimentation tank is added with sludge which is subjected to side-stream hydrolytic acidification after being pretreated by side-stream,adding 100 ml of secondary sedimentation tank sludge with the concentration of 1.7 percent which is cleaned for several times by clear water, namely refluxing 10 percent Q of refluxing sludge in the secondary sedimentation tank to a main flow mixed liquid fermentation tank, then adding the clear water to 1000 ml, and simultaneously adding KNO3The agent is dissolved so that the mixed solution contains 50mgN/L NO3 -. The 1L mainstream fermentation reactor maintains the sludge age for 20 hours to carry out mainstream hydrolytic acidification to generate a carbon source, and simultaneously, the generated carbon source is directly utilized to carry out denitrification to remove the total nitrogen, thereby realizing the removal of the total nitrogen of 27 mgN/L. In actual operation, if glucose is added as a carbon source for removing 27mgN/L of total nitrogen, the cost of carbon source consumption is 0.486 yuan/ton of water (glucose is calculated according to 3000 yuan/ton). Therefore, if the sewage plant does not have enough carbon source and needs to add glucose as the carbon source to realize the removal of 27mg N/L total nitrogen, the utility model discloses a method can help the water plant to realize the carbon source drug consumption reduction of 0.41 yuan/ton water after deducting the sodium hypochlorite drug consumption according to the price accounting of 700 yuan/ton sodium hypochlorite.
Example 2
The concentration of the sludge in the secondary sedimentation tank of the industrial sewage plant is 1.2 percent, the sludge is added into 400mg/L30 percent sodium hydroxide to be mixed for 1 hour and then is added into a hydrolysis acidification tank which is equivalent to a side stream sludge hydrolysis acidification process section, and the hydrolysis acidification tank maintains the retention time of 19 hours at room temperature and operates in a continuous CSTR mode. The SCOD of the pretreated and hydrolyzed and acidified sludge is increased from 14mg/L to 661 mg/L. Then 100 ml of muddy water mixed liquor which is subjected to lateral flow pretreatment and hydrolytic acidification treatment is added into a 1L fermentation tank which is equivalent to main mixed liquor, return sludge which is equivalent to 10% Q of a secondary sedimentation tank is subjected to lateral flow pretreatment, then sludge which is subjected to lateral flow hydrolytic acidification is added, 200 ml of secondary sedimentation tank sludge which is washed for several times by clear water and has the concentration of 1.2% is added, return sludge which is equivalent to 20% Q of return sludge of the secondary sedimentation tank is added into the main mixed liquor fermentation tank, clear water is added into the main mixed liquor fermentation tank, and KNO is added into the main mixed liquor fermentation tank at the same time3The agent is dissolved so that the mixed solution contains 70mgN/L NO3 -. The 1 liter main stream fermentation reactor maintains the sludge age for 22 hours to carry out main stream hydrolytic acidification to generate a carbon source, and simultaneously, the generated carbon source is directly utilized to carry out denitrification to remove the total nitrogen, thereby realizing 28.5 mgN-And removing total nitrogen of the L. In actual operation, glucose is added as a carbon source if necessary in order to remove 28.5mg of N/L of total nitrogen, and the cost of carbon source consumption is 0.51 yuan/ton of water (glucose is calculated according to 3000 yuan/ton). Therefore, if the sewage plant does not have enough carbon source and needs to add glucose as the carbon source to remove the 28.5mg N/L total nitrogen, the method disclosed by the utility model can help the water plant to reduce the consumption of the carbon source by 0.478 yuan/ton of water after deducting the consumption of the liquid caustic soda according to the price of the liquid caustic soda of 800 yuan/ton.
Example 3
The concentration of the sludge after further sedimentation in the secondary sedimentation tank of the municipal sewage plant is 2%, the sludge is added into 2000 mg/L30% hydrogen peroxide for mixing, then added with 1000 mg/L1 +1 hydrochloric acid for mixing for 3 hours, and then added into a hydrolysis acidification tank which is equivalent to a lateral flow sludge hydrolysis acidification process section, and the hydrolysis acidification is maintained at room temperature for 22 hours, and the sludge is operated in a continuous CSTR mode. The SCOD of the pretreated and hydrolyzed and acidified sludge is increased from the original 14mg/L to 590 mg/L. Then adding 100 ml of sludge-water mixed liquor which is subjected to lateral flow pretreatment and hydrolytic acidification treatment into a 1-liter main flow mixed liquor fermentation tank equivalent to main flow mixed liquor, adding sludge which is subjected to lateral flow hydrolysis acidification after the lateral flow pretreatment of return sludge of a secondary sedimentation tank equivalent to 10% Q, adding 150 ml of secondary sedimentation tank sludge which is washed for several times by clear water and has the concentration of 1-2%, adding return sludge which is subjected to 15% Q return by the secondary sedimentation tank into the main flow mixed liquor fermentation tank, adding clear water to 1000 ml, and simultaneously adding KNO3The drug is dissolved to make the mixed solution contain 60mg N/L NO3 -. The fermentation reactor of the 1L mainstream mixed liquid maintains the sludge age for 24 hours to carry out mainstream hydrolytic acidification to generate a carbon source, and simultaneously, the generated carbon source is directly utilized to carry out denitrification to remove the total nitrogen, thereby realizing the removal of the total nitrogen of 32mg N/L. In actual operation, glucose is required to be added as a carbon source for removing 32mg of N/L total nitrogen, and the cost of carbon source consumption is 0.57 yuan per ton of water (glucose is calculated according to 3000 yuan per ton). Therefore, if the sewage plant does not have enough carbon source and needs to add glucose as the carbon source to realize the removal of 32mg N/L total nitrogen, the method can be utilized to carry out accounting according to the price of 1400 yuan/ton of hydrogen peroxide and the price of 280 yuan/ton of hydrochloric acidSo as to help the water plant to reduce the consumption of carbon source and drug by 0.27 yuan/ton water.
In summary, the present invention is not limited to the above embodiments, and other embodiments can be easily proposed by those skilled in the art within the technical teaching of the present invention, but all such embodiments are included in the scope of the present invention.
Claims (9)
1. A sewage treatment system for generating a carbon source by utilizing sludge resource of a sewage plant comprises a main stream system, a side stream system and a sludge concentration tank (4), and is characterized in that the main stream system comprises a main stream mixed liquid fermentation tank (1), a biological nitrogen and phosphorus removal system (2) and a secondary sedimentation tank (3) which are sequentially connected through pipelines, the main stream mixed liquid fermentation tank (1) is connected with a sewage inlet, the secondary sedimentation tank (3) is connected with a sewage outlet, the side stream system comprises a side stream pretreatment reaction tank (5) and a side stream hydrolysis acidification tank (6) which are sequentially connected through pipelines, a sludge outlet of the secondary sedimentation tank (3) is respectively connected with the sludge concentration tank (4), a mixed liquid inlet end of the main stream fermentation tank (1), the biological nitrogen and phosphorus removal system (2) and the side stream pretreatment reaction tank (5), and an outlet of the side stream hydrolysis acidification tank (6) is connected with the main stream mixed liquid fermentation tank (1), a drug adding system (7) for adding drugs is arranged on the inlet of the side flow pretreatment reaction tank (5), and a sludge discharge port is arranged on the sludge concentration tank (4).
2. The sewage treatment system for generating carbon source by utilizing sewage plant sludge resource as claimed in claim 1, wherein the sludge concentration tank (4) is further connected with an inlet of the side stream pretreatment reaction tank (5).
3. The sewage treatment system for generating a carbon source by utilizing sewage plant sludge resource as claimed in claim 1, wherein the side stream pretreatment reaction tank (5) is provided with a mechanical stirrer and an online pH monitor.
4. The sewage treatment system for generating the carbon source by utilizing the sludge resource of the sewage plant as claimed in claim 1, wherein the dosing system (7) is a pipeline mixer or a dosing pump.
5. The sewage treatment system for generating carbon source by utilizing sewage plant sludge resource as claimed in claim 1, wherein a flow impeller is installed in the side-stream hydrolysis acidification tank (6).
6. The sewage treatment system for generating a carbon source by utilizing sewage plant sludge resource as claimed in claim 1, wherein the sidestream hydrolysis acidification tank (6) and the sidestream pretreatment reaction tank (5) are made into an integrated device, and are separated by a partition wall or a partition plate.
7. The sewage treatment system for generating the carbon source by utilizing the sludge resource of the sewage plant as claimed in claim 1, wherein the main flow mixed liquid fermentation tank (1) is provided with a submersible water impeller.
8. The sewage treatment system for generating carbon source by utilizing sewage plant sludge resource as claimed in claim 1, wherein the sludge outlet of the secondary sedimentation tank (3) is connected with the first tank of the biological nitrogen and phosphorus removal system (2) or the foremost end of the biological nitrogen and phosphorus removal system.
9. The sewage treatment system for generating a carbon source by utilizing the sludge resource of the sewage plant as claimed in claim 1, wherein the mainstream biological nitrogen and phosphorus removal system (2) is one of an anoxic/aerobic system, an anaerobic/anoxic/aerobic system, an oxidation ditch system having an anoxic section and an aerobic section, an oxidation ditch system having an anaerobic section/anoxic section/aerobic section, a multi-stage anoxic/aerobic system, and an anaerobic + multi-stage anoxic/aerobic system.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116730565A (en) * | 2023-08-11 | 2023-09-12 | 福建省永建皮革科技股份有限公司 | System and method for treating tanning wastewater |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116730565A (en) * | 2023-08-11 | 2023-09-12 | 福建省永建皮革科技股份有限公司 | System and method for treating tanning wastewater |
| CN116730565B (en) * | 2023-08-11 | 2023-11-21 | 福建省永建皮革科技股份有限公司 | System and method for treating tanning wastewater |
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