CN215403731U - Utilize sewage treatment system of sewage plant mud hydrolytic acidification formation carbon source - Google Patents
Utilize sewage treatment system of sewage plant mud hydrolytic acidification formation carbon source Download PDFInfo
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Abstract
The utility model discloses a sewage treatment system for generating a carbon source by utilizing hydrolytic acidification of sludge in a sewage plant, wherein a main stream system comprises a main stream biological denitrification and dephosphorization system and a biochemical sludge separation and interception system which are sequentially connected through a pipeline, a side stream system comprises a pretreatment reaction tank, a primary side stream hydrolytic acidification tank and a secondary side stream anaerobic fermentation tank which are sequentially connected through a pipeline, a sludge outlet of the biochemical sludge separation and interception system is respectively connected with a sludge concentration tank, the main stream biological nitrogen and phosphorus removal system is connected with the pretreatment reaction tank, an anoxic tank of the main stream biological nitrogen and phosphorus removal system is connected with the secondary sidestream anaerobic fermentation tank, sludge in the anoxic tank in the main stream biological nitrogen and phosphorus removal system flows back to the secondary sidestream anaerobic fermentation tank, an outlet of the secondary sidestream anaerobic fermentation tank is connected with the main stream biological nitrogen and phosphorus removal system, and a medicine adding system for adding a medicine is arranged on an inlet of the pretreatment reaction tank. The utility model promotes the effect of biological nitrogen and phosphorus removal and realizes the consumption reduction of carbon source and drug consumption.
Description
Technical Field
The utility model relates to the field of sludge treatment and sewage treatment of sewage plants, in particular to a sewage treatment system for generating a carbon source by hydrolyzing and acidifying sludge of a sewage plant.
Background
In order to realize the stable standard reaching of the total nitrogen and the total phosphorus of the effluent, the sewage plant needs to effectively remove the total nitrogen and the total phosphorus through a biological nitrogen and phosphorus removal system. Biological nitrogen and phosphorus removal generally recommends that the COD/TN of the influent water is not less than 6 and the readily biochemical COD rCOD/TP is not less than 18. However, many domestic sewage plants face the problem of low carbon-nitrogen ratio of inlet water, so that the biological nitrogen and phosphorus removal efficiency is low, and therefore, many sewage plants often need to add carbon sources to realize effective biological nitrogen and phosphorus removal, and the common carbon sources comprise glucose, sodium acetate, methanol or other synthetic carbon sources; this greatly increases the operating costs of the sewage plant. So far, an economic and effective method for effectively removing total nitrogen and total phosphorus and reducing the consumption of carbon source and chemical consumption is urgently needed by sewage plants.
The main components of the biochemical sludge of the sewage plant are macromolecular compounds such as protein, carbohydrate and the like. The sludge can firstly hydrolyze macromolecular compounds into micromolecular substances by using hydrolytic enzymes through an anaerobic hydrolysis process, and the micromolecular substances can be further acidified to generate organic volatile acid. The acetic acid, the propionic acid and the butyric acid are main products of the hydrolytic acidification of the sludge, so the hydrolytic acidification product of the sludge can be effectively utilized as a carbon source by a biological nitrogen and phosphorus removal system.
The hydrolysis process of the sludge is a speed-limited step, and the hydrolysis degree of the sludge determines the effect of the hydrolytic acidification of the sludge on generating a carbon source. The hydrolysis of the sludge requires a longer residence time to be maintained due to the slow hydrolysis process. The hydrolysis effect of the sludge can be enhanced through sludge pretreatment, and common methods for sludge pretreatment include adding an oxidant, adding acid to reduce the pH value, adding alkali to increase the pH value, heating, pressurizing or using ultrasonic waves to break the wall of sludge cells. In actual production practice, the pretreatment of the sludge is generally utilized in the anaerobic digestion process of the sludge, and the pretreated sludge directly enters an anaerobic digestion tank to promote the anaerobic digestion of the sludge and the yield of the biogas. Sludge pretreatment is also being used to promote hydrolytic acidification of sludge to produce carbon sources. In the disclosed patents, the methods disclosed in CN107265806A and CN110282841A both add liquid alkali to raise the pH of sludge to 10, and then perform anaerobic alkaline fermentation to generate organic volatile acid, and the method mainly uses high-dose liquid alkali to perform the processes of intensified wall breaking of sludge cells and biochemical acidification. In the method disclosed in CN104118971B, the main stream hydrolysis fermentation is performed after mixing and concentrating the sludge in the primary sedimentation tank and the biochemical sludge returned from the secondary sedimentation tank. Envidan corporation of Denmark also discloses a method of ASP/SSH (activated sludge recirculation/sidestream sludge hydrolysis) to effect the production of carbon source by the sludge in sidestream hydrolysis to promote denitrification and phosphorus removal in biochemical systems. The patent CN104118971B and the method disclosed by EnviDan corporation of denmark both control hydrolysis and fermentation in a single-stage hydrolysis acidification tank by alternately performing aeration and stirring to control micro-aerobic and anaerobic conditions, and are not strict anaerobic conditions. So far, how to generate more carbon sources through hydrolytic acidification by effective and economic sludge pretreatment and then coupling hydrolytic acidification process has great market prospect.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem of providing a sewage treatment system for generating a carbon source by hydrolyzing and acidifying sludge in a sewage plant, carrying out sludge pretreatment to realize the initial wall breaking of sludge cells, and further optimizing the hydrolysis and acidification process in the subsequent hydrolysis and acidification to realize the generation of the carbon source by hydrolyzing and acidifying sludge.
In order to solve the technical problems, the utility model adopts the technical scheme that: a sewage treatment system for generating a carbon source by utilizing hydrolytic acidification of sludge in a sewage plant comprises a main stream system, a side stream system and a sludge concentration tank, wherein the main stream system comprises a main stream biological nitrogen and phosphorus removal system and a biochemical sludge separation and interception system which are sequentially connected through a pipeline, the main stream biological nitrogen and phosphorus removal system is connected with a sewage inlet, the biochemical sludge separation and interception system is connected with a sewage outlet, the side stream system comprises a pretreatment reaction tank, a primary side stream hydrolytic acidification tank and a secondary side stream anaerobic fermentation tank which are sequentially connected through a pipeline, a sludge outlet of the biochemical sludge separation and interception system is respectively connected with the sludge concentration tank, the main stream biological nitrogen and phosphorus removal system and the pretreatment reaction tank, an anoxic tank of the main stream biological nitrogen and phosphorus removal system is connected with the secondary side stream anaerobic fermentation tank, so that the anoxic tank in the main stream biological nitrogen and phosphorus removal system flows back to the secondary side stream anaerobic fermentation tank, the outlet of the second-stage side-stream anaerobic fermentation tank is connected with the main stream biological nitrogen and phosphorus removal system, the first-stage side-stream hydrolysis acidification tank is a hydrolysis acidification tank adopting a continuous stirring mixing mode, the second-stage side-stream anaerobic fermentation tank is a static anaerobic fermentation tank adopting an intermittent stirring mode, a chemical adding system for adding chemicals is arranged on the inlet of the pretreatment reaction tank, and a sludge discharge port is arranged on the sludge concentration tank.
The biochemical sludge separation and interception system is a secondary sedimentation tank or a membrane tank.
The outlet of the secondary side-stream anaerobic fermentation tank is connected with the first tank or the water inlet end of the main-stream biological nitrogen and phosphorus removal system.
The sludge concentration tank is also connected with the inlet of the pretreatment reaction tank.
And the pretreatment reaction tank is provided with a mechanical stirrer and an online pH monitor.
The medicine feeding system is a pipeline mixer or a medicine feeding pump.
And a mechanical stirrer is arranged in the primary side-stream hydrolysis acidification tank. .
An online pH meter or an oxidation-reduction potentiometer ORP is arranged in the primary side-stream hydrolysis acidification tank.
The pretreatment reaction tank, the primary side flow hydrolysis acidification tank and the secondary side flow anaerobic fermentation tank are made into integrated equipment, and the middle of the integrated equipment is separated by a partition wall or a partition plate.
The second-stage side flow anaerobic fermentation tank is provided with a stirrer.
The utility model has the beneficial effects that:
the sewage treatment system of the utility model utilizes that partial return sludge of the secondary sedimentation tank or the return sludge of the membrane tank is pretreated in the sidestream and then enters the primary sidestream hydrolysis acidification tank for hydrolysis acidification, then enters the secondary sidestream anaerobic fermentation tank for further fermentation, and simultaneously, part of sludge of the anoxic tank of the mainstream biological nitrogen and phosphorus removal system is directly discharged into the secondary sidestream anaerobic fermentation tank for fermentation, and simultaneously, carbon source generated in the fermentation tank is directly utilized for denitrification reaction. And finally, discharging the sludge subjected to side stream pretreatment, primary side stream hydrolytic acidification and secondary side stream anaerobic fermentation into a mainstream biological nitrogen and phosphorus removal system to provide a carbon source.
The sewage treatment system of the utility model adds the medicament in the sludge pretreatment only for realizing the preliminary wall breaking of the sludge cells, and the carbon source generation by the sludge hydrolytic acidification is mainly realized by the subsequent primary side-stream hydrolytic acidification and secondary side-stream anaerobic fermentation; the dosage of the chemical agent added in the pretreatment process section is mild, so that the operation cost of the sludge pretreatment process section is optimized, the economic benefit of generating the carbon source by recycling the sludge is realized to the maximum extent, and the utility model has wide market application prospect.
The hydrolytic acidification in the sewage treatment system adopts a method of primary side-stream hydrolytic acidification and secondary side-stream anaerobic fermentation, respectively optimizes the operating conditions of the two-stage hydrolytic acidification, and realizes the optimal effect of the hydrolytic acidification. Moreover, the sludge pretreatment and the two-stage hydrolysis acidification are both established on the side stream of the sewage plant, so that the method can be directly installed and modified without influencing the operation of the water plant and then combined with the original process of the sewage plant.
The secondary side flow anaerobic fermentation tank in the method not only performs sludge fermentation to generate a carbon source, but also can directly utilize the generated carbon source to remove nitrate nitrogen and nitrite nitrogen brought back by sludge flowing back from an anoxic tank of a main flow biological denitrification system; moreover, because the sludge concentration of the secondary side flow anaerobic fermentation tank of the side flow is higher, the denitrification speed is correspondingly higher than that of the main flow anoxic tank, and the impact resistance of the main flow biological nitrogen and phosphorus removal system is greatly improved.
In the sewage treatment system, part of organic matters in the sludge are changed into carbon sources to be utilized due to hydrolytic acidification, so that the effect of biological nitrogen and phosphorus removal is promoted, and the consumption reduction of the carbon sources and the partial reduction of biochemical sludge can be realized.
The utility model is not only suitable for municipal wastewater, but also suitable for non-municipal wastewater, in particular to sewage plants which need to add carbon sources to realize the standard of total nitrogen of effluent or sewage plants which need to additionally add chemical phosphorus removal agents because the biological phosphorus removal effect is not ideal due to insufficient carbon sources.
Drawings
FIG. 1 is a block diagram showing the construction of a sewage treatment system for producing a carbon source by hydrolytic acidification of sludge from a sewage plant according to the present invention.
FIG. 2 is a block diagram showing another embodiment of the sewage treatment system for generating a carbon source by hydrolysis and acidification of sludge from a sewage plant according to the present invention.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention; it is obvious that 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.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", "top/bottom", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "disposed," "sleeved/connected," "connected," and the like are to be construed broadly, e.g., "connected," which may be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in figure 1, the sewage treatment system for generating carbon source by utilizing hydrolytic acidification of sludge in a sewage plant comprises a main stream system, a side stream system and a sludge concentration tank, wherein the main stream system comprises a main stream biological nitrogen and phosphorus removal system 1 and a biochemical sludge separation and interception system 2 which are sequentially connected through a pipeline, the main stream biological nitrogen and phosphorus removal system 1 is connected with a sewage inlet, the biochemical sludge separation and interception system 2 is connected with a sewage outlet, the side stream system comprises a pretreatment reaction tank 4, a primary side stream hydrolytic acidification tank 5 and a secondary side stream anaerobic fermentation tank 6 which are sequentially connected through a pipeline, the sludge outlet of the biochemical sludge separation and interception system 2 is respectively connected with the sludge concentration tank 3, the main stream biological nitrogen and phosphorus removal system 1 and the pretreatment reaction tank 4, the anoxic tank of the main stream biological nitrogen and phosphorus removal system 1 is connected with the secondary side stream anaerobic fermentation tank 6, so that sludge in the anoxic tank in the main stream biological nitrogen and phosphorus removal system flows back to the secondary side stream anaerobic fermentation tank 6, the outlet of the second-stage side-stream anaerobic fermentation tank 6 is connected with the main stream biological nitrogen and phosphorus removal system 1, the first-stage side-stream hydrolysis acidification tank 5 is a hydrolysis acidification tank adopting a continuous stirring mixed mode, the second-stage side-stream anaerobic fermentation tank 6 is a static anaerobic fermentation tank adopting an intermittent stirring mode, a chemical adding system 7 for adding chemicals is arranged at the inlet of the pretreatment reaction tank 4, and a sludge discharge port is arranged on the sludge concentration tank 3.
The biochemical sludge separation and interception system 2 is a secondary sedimentation tank or a membrane tank.
The outlet of the secondary side-stream anaerobic fermentation tank 6 is connected with the first tank or the water inlet end of the main-stream biological nitrogen and phosphorus removal system 1.
As shown in fig. 2, the sludge concentrating tank 3 is also connected to an inlet of the pretreatment reaction tank 4.
And a mechanical stirrer and an online pH monitor are arranged on the pretreatment reaction tank 4.
The medicine adding system 7 is a pipeline mixer or a medicine adding pump.
And a mechanical stirrer is arranged in the primary side-stream hydrolysis acidification tank 5. .
An online pH meter or an oxidation-reduction potentiometer ORP is arranged in the primary side-stream hydrolysis acidification tank 5.
The pretreatment reaction tank 4, the primary side-stream hydrolysis acidification tank 5 and the secondary side-stream anaerobic fermentation tank 6 are made into integrated equipment, and the middle parts of the equipment are separated by partition walls or partition plates.
The second-stage side-stream anaerobic fermentation tank 6 is provided with a stirrer.
The sewage treatment system of the utility model divides return sludge of the secondary sedimentation tank or return sludge of the membrane tank into partial sludge to a sidestream sludge pretreatment process section for pretreatment to realize the preliminary wall breaking of sludge cells, and then enters a two-stage hydrolysis acidification process of a sidestream, wherein the first-stage sidestream hydrolysis acidification tank operates in a continuous stirring and mixing mode, the second-stage hydrolysis acidification tank operates in a static anaerobic fermentation mode, and a stirrer of the second-stage sidestream anaerobic fermentation tank only operates in an intermittent mode. And the sludge in the anoxic tank of the main stream biological nitrogen and phosphorus removal system also flows back to a secondary side stream anaerobic fermentation tank of the side stream for anaerobic fermentation to generate a carbon source and simultaneously remove nitrate nitrogen and nitrite nitrogen through denitrification reaction. The sludge is discharged into the front end of the main stream biological denitrification system after being subjected to side stream pretreatment and two-stage hydrolytic acidification so as to provide a carbon source to promote the main stream biological denitrification and dephosphorization effect, and simultaneously, the consumption reduction of the carbon source is realized.
The utility model mainly comprises 3 steps:
step 1 is the pretreatment of sludge to achieve local wall breaking of sludge cells. Leading out (1-90%) Q (Q is the inflow flow of a sewage plant) from the return sludge of the secondary sedimentation tank to a side-stream sludge pretreatment process section for pretreatment; if the biochemical system of the sewage plant is operated by an MBR process, Q is led out (1-100 percent) from return sludge of the MBR to a side-stream sludge pretreatment process section for pretreatment. If the sewage plant is a municipal sewage plant or a non-municipal sewage plant but a large amount of chemical agents such as iron salt, aluminum salt or fenton agent are not added in the pretreatment process section before the biochemical system or the advanced treatment process section after the biochemical system, the residual sludge which is prepared to be sent to dehydration after being concentrated in the sludge concentration tank can be further divided into 1-90% of the residual sludge to be sent to the sludge pretreatment process section. The sludge concentration of the sludge pretreatment process section can be 0.2-12%. If the sludge concentration of the return sludge of the secondary sedimentation tank or the membrane tank is low, the sludge concentration can be firstly improved and then enters the pretreatment process section, the method for improving the sludge concentration can utilize sludge concentration, or utilize a screw stacking machine or a centrifugal machine to carry out partial dehydration, and the sludge does not need to be added with chemical agents to carry out sludge conditioning before the dehydration
The sludge pretreatment can adopt the reaction by adding an oxidant, wherein the oxidant can be sodium hypochlorite, hydrogen peroxide or ozone, and the dosage of the oxidant is 50-5000 mg/L. The pretreatment process section can also control the pH value to be 2-7 by adding acid, or control the pH value to be 7-12 by adding alkali, or respectively add oxidant and acid, or respectively add oxidant and alkali to carry out the primary wall breaking of sludge cells. The sludge pretreatment reaction tank can be operated in a continuous operation fully mixed CSTR mode or a continuous operation plug-flow PFR mode; it is also possible to run an in-order batch SBR mode, preferably a CSTR mode or a PFR mode operating continuously. The hydraulic retention time of the pretreatment reaction tank is 0.1-24 hours, the pretreatment reaction tank adopts a mechanical stirring mode, and the power of a stirrer is 3-25KW/1000m3An effective volume. The pretreatment reaction tank is arranged on an on-line pH meterThe pH was monitored. The oxidant, acid or alkali required by the pretreatment process section can be directly added into the reaction tank through a dosing pump, or can be added into a pipeline and mixed by a pipeline mixer and then enters the pretreatment reaction tank.
And step 3, a side flow secondary side flow anaerobic fermentation tank which is used for not only performing sludge fermentation to generate a carbon source, but also removing nitrate nitrogen and nitrite nitrogen through denitrification by directly utilizing the carbon source generated by the fermentation tank. And discharging the sludge in the primary side-stream hydrolysis acidification tank into a secondary fermentation tank for further fermentation. In addition, the sludge is directly returned from the anoxic tank of the main stream biological nitrogen and phosphorus removal system to the secondary side stream anaerobic fermentation tank of the side stream for synchronous anaerobic fermentation and denitrification. The reflux quantity from the anoxic tank of the main stream biological nitrogen and phosphorus removal system to the side stream secondary side stream anaerobic fermentation tank is (1-100%) Q. When the main flow biological nitrogen and phosphorus removal system operates in a primary anaerobic/anoxic/aerobic, or secondary anoxic/aerobic/anoxic/aerobic, or anaerobic/anoxic/aerobic state, the sludge can flow back from the primary anoxic tank to the lateral flow secondary anaerobic fermentation tank; if the biological nitrogen and phosphorus removal system operates in more than two stages or multi-stage anoxic/aerobic or anaerobic + multi-stage anoxic/aerobic systems, the sludge can flow back from the anoxic tank of the last stage to the secondary fermentation tank of the side stream.
The side-stream secondary side-stream anaerobic fermentation tank can run at room temperature, and the secondary side-stream anaerobic fermentation tank runs in a static fermentation mode. When the secondary side-stream anaerobic fermentation tank is started, anaerobic mud or hydrolytic acidification mud does not need to be additionally inoculated; can be directly introduced into the sludge after pretreatment and side stream first-stage side stream hydrolytic acidification treatment for operation. The second-stage fermentation tank is provided with a stirrer with the power of 3-25KW/1000m3Effective volume, the stirrer of the anaerobic fermentation tank is only intermittently operated to control the sludge age of the fermentation tank to be 2-72 hours. The sludge is directly discharged into a first tank of the mainstream biological nitrogen and phosphorus removal system or a water inlet end of the mainstream biological nitrogen and phosphorus removal system to provide a carbon source for the mainstream biological nitrogen and phosphorus removal system after being subjected to side flow pretreatment, primary side flow hydrolysis acidification and secondary side flow anaerobic fermentation tanks so as to promote biological nitrogen and phosphorus removal and realize carbon source consumption reduction.
Example 1
The sludge concentration of a membrane tank of a municipal sewage plant is 1.1%, the sludge is added with 500mg/L sodium hypochlorite and mixed for 4 hours, and then added into a hydrolysis acidification tank which is equivalent to a side-stream first-level sludge hydrolysis acidification process section, and the hydrolysis acidification tank is kept at room temperature for 16 hours to stay for running into a continuous CSTR mode. The soluble COD SCOD of the sludge after pretreatment and primary side stream hydrolytic acidification is increased from the original 38mg/L to 655 mg/L. Then 100 ml of the mixture is added into a 1 liter anaerobic fermentation tank which is equivalent to a secondary side flow anaerobic fermentation tank and is subjected to side flow sludge pretreatment and primary side flow hydrolysisThe acidified sludge is equivalent to 10 percent Q membrane pool return sludge which is subjected to lateral flow pretreatment, then the sludge subjected to primary lateral flow hydrolytic acidification is added, 200 ml of sludge which is washed for several times by clear water and has a concentration of 0.55 percent in an anoxic pool is added, the sludge which is equivalent to 20 percent Q anoxic pool return flow of the anoxic pool of the mainstream biological nitrogen and phosphorus removal system is added into a secondary lateral flow anaerobic fermentation pool, then clear water is added to 1000 ml, and KNO is added simultaneously3The drug is dissolved to make the mixed solution contain 50mg N/L NO3 -.1 liter of secondary side flow anaerobic fermentation is maintained for 20 hours at room temperature for hydrolysis acidification to generate a carbon source, and the generated carbon source is directly utilized for denitrification to remove total nitrogen, so that the total nitrogen removal of 27.2mg N/L is realized. In actual operation, glucose is added as a carbon source if necessary in order to remove 27.2mg of N/L of total nitrogen, and the cost of carbon source consumption is 0.49 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 remove 27.2mg N/L total nitrogen, the method can help the water plant to reduce the carbon source drug consumption by 0.45 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 settled sludge in the secondary sedimentation tank of the municipal sewage plant is 2.7 percent, the sludge is added with 500mg/L sodium hypochlorite and mixed for 4 hours, and then the sludge is added into a hydrolysis acidification tank which is equivalent to a primary side flow hydrolysis acidification process section of the side flow sludge, and the hydrolysis acidification tank is kept to operate in a CSTR mode of continuous operation at room temperature for 16 hours of residence time. The soluble COD SCOD of the sludge after pretreatment and primary side stream hydrolytic acidification is increased from the original 28mg/L to 839 mg/L. Then 100 ml of sludge which is pretreated by side flow sludge and treated by primary side flow hydrolysis acidification is added into 1 liter of secondary side flow anaerobic fermentation tank which is equivalent to 10 percent Q of secondary sedimentation tank return sludge, the sludge which is pretreated by side flow and treated by primary side flow hydrolysis acidification is added, 200 ml of anoxic tank sludge which is washed for several times by clear water and has the concentration of 0.5 percent is added, the anoxic tank sludge which is equivalent to 20 percent Q of main flow biological nitrogen and phosphorus removal system return flow to the secondary side flow anaerobic fermentation tank, and clear water is addedAdding KNO to 1000 ml simultaneously3The drug is dissolved to make the mixed solution contain 50mg N/L NO3 -. A1L secondary side-stream anaerobic fermentation reactor maintains the sludge age for 24 hours at room temperature to carry out hydrolytic acidification to generate a carbon source, and simultaneously, the generated carbon source is directly utilized to carry out denitrification to remove total nitrogen, thereby realizing the removal of 32mg N/L total nitrogen. In actual operation, if glucose is added as a carbon source for removing 32mg of N/L total nitrogen, the cost of carbon source consumption is 0.57 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 32mg N/L total nitrogen, the method can help the water plant to reduce the carbon source drug consumption by 0.53 yuan/ton water after deducting the sodium hypochlorite drug consumption according to the price accounting of 700 yuan/ton sodium hypochlorite.
Example 3
The sludge concentration of a membrane tank of an industrial sewage plant is 1.2 percent, the sludge is added into 400mg/L30 percent sodium hydroxide to be mixed for 2 hours and then is added into a hydrolysis acidification tank which is equivalent to a first-stage side-stream hydrolysis acidification process section of side-stream sludge, and the first-stage hydrolysis acidification tank is maintained at 35 ℃ for 18 hours to operate in a continuous operation CSTR mode. The soluble COD SCOD of the sludge after pretreatment and first-stage hydrolytic acidification is increased from the original 24mg/L to 582 mg/L. Then adding 120 ml of sludge subjected to lateral flow pretreatment and primary lateral flow hydrolytic acidification treatment into 1 liter of secondary lateral flow anaerobic fermentation tank equivalent to the lateral flow, adding sludge subjected to lateral flow pretreatment and primary lateral flow hydrolytic acidification treatment into membrane tank return sludge equivalent to 12% Q, adding 250 ml of anoxic tank sludge with the solid content of 0.55% which is washed for several times by clear water, refluxing 25% Q of anoxic tank sludge to the secondary lateral flow anaerobic fermentation tank equivalent to the anoxic tank of the main flow biological nitrogen and phosphorus removal system, adding clear water to 1000 ml, and simultaneously adding KNO3The drug is dissolved to make the mixed solution contain 70mg N/L NO3 -. The 1 liter anaerobic fermentation reactor maintains the sludge age for 24 hours at room temperature to carry out hydrolytic acidification to generate a carbon source, and simultaneously, the generated carbon source is directly utilized to carry out denitrification to remove total nitrogen, thereby realizing the removal of the total nitrogen of 26.8mg N/L. In actual operationIf glucose is added as a carbon source in order to remove 26.8mg of N/L of total nitrogen, the cost of carbon source consumption is 0.48 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 26.8mg N/L total nitrogen, the method disclosed by the utility model can help the water plant to reduce the carbon source drug consumption by 0.44 yuan/ton water after deducting the drug consumption of the liquid alkali according to the price of the liquid alkali of 800 yuan/ton.
Example 4
The concentration of sludge in a secondary sedimentation tank of a municipal sewage plant is 1.2 percent, the sludge is added into 1500mg/L30 percent hydrogen peroxide for mixing, then added into 800 mg/L1 +1 hydrochloric acid for mixing for 4 hours, and then added into a hydrolysis acidification tank which is equivalent to a primary side flow hydrolysis acidification process section of the sludge, and the hydrolysis acidification is maintained at room temperature for 20 hours and is operated into a continuous operation CSTR mode. The soluble COD SCOD of the sludge after pretreatment and primary side stream hydrolytic acidification is increased from the original 16mg/L to 470 mg/L. Then adding 120 ml of sludge subjected to lateral flow pretreatment and primary lateral flow hydrolytic acidification treatment into 1 liter of secondary lateral flow anaerobic fermentation tank equivalent to the secondary lateral flow anaerobic fermentation tank, adding sludge subjected to primary lateral flow hydrolytic acidification after the secondary sedimentation tank equivalent to 12% Q is subjected to lateral flow pretreatment, adding 300 ml of sludge of an anoxic tank which is cleaned for several times by clear water and has the concentration of 0.6%, adding 30% Q of anoxic tank sludge to the secondary lateral flow anaerobic fermentation tank equivalent to the backflow of a main flow biological nitrogen and phosphorus removal system, adding clear water to 1000 ml, and simultaneously adding KNO3The drug is dissolved to make the mixed solution contain 50mg N/L NO3 -. The anaerobic fermentation reactor with 1 liter operates at room temperature and maintains the sludge age for 24 hours to carry out hydrolytic acidification to generate a carbon source, and simultaneously, the generated carbon source is directly utilized to carry out denitrification to remove total nitrogen, thereby realizing the removal of 30.3mg N/L total nitrogen. In actual operation, glucose is required to be added as a carbon source for removing 30.3mg of N/L of total nitrogen, and the carbon source consumption cost is 0.545 yuan/ton of water (glucose is calculated according to 3000 yuan/ton). Therefore, when the sewage plant does not have enough carbon source and needs to add glucose as the carbon source to remove 30.3mg of N/L total nitrogen, the accounting is carried out according to the hydrogen peroxide price of 1400 yuan/ton and the hydrochloric acid price of 280 yuan/tonThe method can help water plants to reduce the consumption of carbon source and drug by 0.28 yuan per ton of water.
In summary, the disclosure of the present invention is not limited to the above-mentioned embodiments, and persons skilled in the art can easily set forth other embodiments within the technical teaching of the present invention, but such embodiments are included in the scope of the present invention.
Claims (8)
1. A sewage treatment system for generating a carbon source by utilizing hydrolytic acidification of sludge in a sewage plant comprises a main stream system, a side stream system and a sludge concentration tank, and is characterized in that the main stream system comprises a main stream biological nitrogen and phosphorus removal system (1) and a biochemical sludge separation and interception system (2) which are sequentially connected through pipelines, the main stream biological nitrogen and phosphorus removal system (1) is connected with a water inlet of sewage, the biochemical sludge separation and interception system (2) is connected with a sewage outlet, the side stream system comprises a pretreatment reaction tank (4), a primary side stream hydrolytic acidification tank (5) and a secondary side stream anaerobic fermentation tank (6) which are sequentially connected through pipelines, a sludge outlet of the biochemical sludge separation and interception system (2) is respectively connected with the sludge concentration tank (3), the main stream biological nitrogen and phosphorus removal system (1) and the pretreatment reaction tank (4), and an anoxic tank of the main stream biological nitrogen and phosphorus removal system (1) is connected with the secondary side stream anaerobic fermentation tank (6), making sludge in an anoxic tank in a main stream biological nitrogen and phosphorus removal system flow back to a secondary side stream anaerobic fermentation tank (6), wherein an outlet of the secondary side stream anaerobic fermentation tank (6) is connected with the main stream biological nitrogen and phosphorus removal system (1), a primary side stream hydrolysis acidification tank (5) is a hydrolysis acidification tank adopting a continuous stirring and mixing mode, the secondary side stream anaerobic fermentation tank (6) is a static anaerobic fermentation tank adopting an intermittent stirring mode, a chemical adding system (7) for adding a medicament is arranged at an inlet of a pretreatment reaction tank (4), and a sludge discharge port is arranged on a sludge concentration tank (3); the biochemical sludge separation and interception system (2) is a secondary sedimentation tank or a membrane tank; the outlet of the secondary side flow anaerobic fermentation tank (6) is connected with the first tank or the water inlet end of the main flow biological nitrogen and phosphorus removal system (1).
2. The sewage treatment system for generating a carbon source by hydrolysis and acidification of sludge from a sewage plant according to claim 1, wherein the sludge concentration tank (3) is further connected to an inlet of the pretreatment reaction tank (4).
3. The sewage treatment system for generating a carbon source by utilizing hydrolytic acidification of sewage plant sludge as claimed in claim 1, wherein the pretreatment reaction tank (4) is provided with a mechanical stirrer and an online pH monitor.
4. The sewage treatment system for generating a carbon source by hydrolysis and acidification of sludge from a sewage plant according to claim 1, wherein the dosing system (7) is a pipeline mixer or a dosing pump.
5. The sewage treatment system for generating a carbon source by hydrolysis and acidification of sewage plant sludge as claimed in claim 1, wherein a mechanical stirrer is installed in the primary side-stream hydrolysis and acidification tank (5).
6. The sewage treatment system for generating a carbon source by hydrolysis and acidification of sewage plant sludge according to claim 1, wherein an on-line pH meter or an oxidation-reduction potentiometer ORP is installed in the primary side-stream hydrolysis and acidification tank (5).
7. The sewage treatment system for generating a carbon source by hydrolysis and acidification of sludge from a sewage plant according to claim 1, wherein the pretreatment reaction tank (4), the primary side-stream hydrolysis and acidification tank (5) and the secondary side-stream anaerobic fermentation tank (6) are integrated into a single device, and are separated by a partition wall or a partition plate.
8. The sewage treatment system for generating a carbon source by hydrolysis and acidification of sludge from a sewage plant according to claim 1, wherein the secondary side-stream anaerobic fermentation tank (6) is equipped with a stirrer.
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