CN214829754U - Sewage treatment system for generating carbon source by utilizing hydrolytic acidification of sludge in sewage plant - Google Patents
Sewage treatment system for generating carbon source by utilizing hydrolytic acidification of sludge in sewage plant Download PDFInfo
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Abstract
The utility model discloses a sewage treatment system for generating carbon source by utilizing sludge hydrolysis acidification of a sewage plant, a main stream system comprises a main stream biological denitrification and dephosphorization system and a biochemical sludge separation interception system which are connected in sequence through pipelines, the main stream biological denitrification and dephosphorization system is connected with a water inlet of sewage, the biochemical sludge separation interception system is connected with a sewage outlet, the side stream system comprises a pretreatment reaction tank, a primary side stream hydrolysis acidification tank and a secondary side stream anaerobic fermentation tank which are connected in sequence through pipelines, the sludge outlet of the biochemical sludge separation interception system is respectively connected with a sludge concentration tank, the main stream biological denitrification and dephosphorization system, the pretreatment reaction tank is connected with the secondary side stream anaerobic fermentation tank, the outlet of the secondary side stream anaerobic fermentation tank is connected with the main stream biological denitrification and dephosphorization system, the primary side stream hydrolysis acidification tank adopts a continuous stirring mixing mode, the secondary side stream anaerobic fermentation tank adopts an intermittent stirring mode, the utility model promotes the effect of biological nitrogen and phosphorus removal and realizes the consumption reduction of carbon source consumption.
Description
Technical Field
The utility model relates to a sludge treatment and sewage treatment field of sewage factory, especially an utilize sewage treatment system of sewage factory sludge hydrolysis acidizing formation carbon source.
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 that a sewage treatment system that utilizes sewage plant sludge hydrolysis acidification to generate carbon source is provided, carry out the preliminary broken wall that mud preliminary treatment realized the mud cell, further optimize the process of hydrolysis acidification in order to realize utilizing sludge hydrolysis acidification to generate the carbon source in follow-up hydrolysis acidification.
In order to solve the technical problem, the utility model discloses a technical scheme is: 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, the pretreatment reaction tank and the secondary side stream anaerobic fermentation tank, an outlet of the secondary side stream anaerobic fermentation tank is connected with the main stream biological nitrogen and phosphorus removal system, the primary side stream hydrolytic acidification tank is a hydrolytic acidification tank adopting a continuous stirring mixed 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 an inlet of the pretreatment reaction tank, and a sludge outlet 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 first-stage side-stream hydrolysis acidification tank and the second-stage side-stream anaerobic fermentation tank are made into integrated equipment, and the middle of the 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 advantages that:
the utility model discloses a sewage treatment system utilizes and passes through the side stream and sink pond backward flow mud to part two, perhaps membrane pool backward flow mud gets into one-level side stream hydrolysis acidification pond after carrying out the preliminary treatment and hydrolysises the acidizing, get into the further fermentation of side stream second grade side stream anaerobic fermentation pond after that, partly two sink pond backward flow mud simultaneously, perhaps membrane pool backward flow mud also directly emits into side stream second grade side stream anaerobic fermentation pond and ferments, directly utilize the carbon source that generates at anaerobic fermentation pond simultaneously to pass through denitrification reaction denitrogenation. And finally, discharging the sludge which passes through the sidestream pretreatment reaction tank, the primary sidestream hydrolysis acidification tank and the secondary sidestream anaerobic fermentation tank 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 tank only for realizing the preliminary wall breaking of sludge cells, and the carbon source generated 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 milder, so 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 utility model discloses a hydrolytic acidification among the sewage treatment system has adopted one-level side stream hydrolytic acidification and second grade side stream anaerobic fermentation's method, optimizes the operating condition of two-stage hydrolytic acidification respectively, realizes the best effect of hydrolytic acidification. Moreover, sludge pretreatment and two-stage hydrolysis acidification are all side flows established at the sewage plant, make the utility model discloses can directly install under the state that does not influence the operation of water plant and reform transform the back and combine together with the original technology of sewage plant.
The second-stage side flow anaerobic fermentation tank in the sewage treatment system of the utility model can directly utilize the generated carbon source to remove nitrate nitrogen and nitrite nitrogen brought back by the return sludge of the secondary sedimentation tank or the return sludge of the membrane tank besides performing sludge fermentation to generate the carbon source; moreover, because the sludge concentration of the secondary anaerobic fermentation tank of the side stream is higher, the denitrification speed is correspondingly higher than that of the main stream anoxic tank, so that the impact resistance of the main stream biological nitrogen and phosphorus removal system is greatly improved.
The utility model discloses a partial organic matter in the mud among the sewage treatment system is utilized owing to the carbon source that becomes of hydrolytic acidification, so not only promote biological nitrogen and phosphorus removal's effect, can also realize the partial decrement of carbon source consumption reduction and biochemical mud.
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 a carbon source by hydrolyzing and acidifying sludge from a sewage plant.
FIG. 2 is a block diagram showing another embodiment of the sewage treatment system for generating a carbon source by hydrolyzing and acidifying sludge from 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.
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 the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to 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 is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted", "provided", "sleeved/connected", "connected", and the like are to be understood in a broad sense, such as "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 meaning 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 utility model discloses an utilize sewage treatment system of sewage plant's sludge hydrolysis acidizing formation carbon source, including mainstream system, sidestream system and sludge thickening tank, the mainstream system includes mainstream biological nitrogen and phosphorus removal system 1 and biochemical sludge separation and interception system 2 that connect gradually through the pipeline, mainstream biological nitrogen and phosphorus removal system 1 links to each other with the water inlet of sewage, be connected with the sewage delivery port on biochemical sludge separation and interception system 2, the sidestream system includes pretreatment reaction tank 4, one-level sidestream hydrolysis acidizing pond 5 and second grade sidestream anaerobic fermentation pond 6 that connect gradually through the pipeline, the sludge outlet of biochemical sludge separation and interception system 2 respectively with sludge thickening tank 3, mainstream biological nitrogen and phosphorus removal system 1, pretreatment reaction tank 4 and second grade sidestream anaerobic fermentation pond 6 link to each other, the export of second grade sidestream anaerobic fermentation pond 6 links to each other with mainstream biological nitrogen and phosphorus removal system 1, the 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 chemicals is arranged on an 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 first-stage side-stream hydrolysis acidification tank 5 and the second-stage side-stream anaerobic fermentation tank 6 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-stream anaerobic fermentation tank 6 is provided with a stirrer.
The utility model discloses a sewage treatment system, the backward flow mud that sinks the pond backward flow mud to two, perhaps the backward flow mud in membrane pool divides partial mud to carry out the preliminary broken wall that preliminary treatment realized the mud cell to the sidestream mud preliminary treatment technology section, gets into the two-stage hydrolysis acidification process of sidestream after that, and one-level sidestream hydrolysis acidification pond moves into the mode that the continuous stirring mixes, and the second grade hydrolysis acidification moves into static anaerobic fermentation mode, and the agitator in second grade sidestream anaerobic fermentation pond is the intermittent type formula operation only. And refluxing sludge of the secondary sedimentation tank or refluxing sludge of the membrane tank to a secondary sidestream anaerobic fermentation tank of the sidestream 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 discloses a mainly contained 3 steps in the method:
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 was equipped with an on-line pH meter to monitor pH. 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 to be mixed by using a pipelineThe reactor is mixed and then enters a 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 return sludge of the secondary sedimentation tank or the return sludge of the membrane tank also flows out (1-50%) Q to the secondary side-flow anaerobic fermentation tank for fermentation to generate a carbon source for synchronous anaerobic fermentation and denitrification. 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 concentration of sludge in a secondary sedimentation tank of a municipal sewage plant is 1.1 percent, the sludge is added with 500mg/L sodium hypochlorite and mixed for 4 hours, then the mixture is added into a hydrolysis acidification tank which is equivalent to a lateral flow primary 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 operation 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 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 the secondary side flow anaerobic fermentation tank, return sludge which is equivalent to 10 percent Q is pretreated by side flow and then added with sludge which is treated by primary side flow hydrolysis acidification, 100 ml of secondary sedimentation sludge which is washed for several times by clear water and has the concentration of 1.1 percent is added, return sludge which is equivalent to 10 percent Q is returned into the secondary side flow anaerobic fermentation tank by the secondary sedimentation tank, and clear water is added into 1000 ml of return sludgeWhile adding KNO3The 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 sludge age 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 26.2mg N/L. In actual operation, if glucose is added as a carbon source for removing 26.2mg of N/L of total nitrogen, the cost of carbon source consumption is 0.471 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 26.2mg N/L total nitrogen, the method of the utility model can help the water plant to reduce the consumption of carbon source and drug by 0.43 yuan/ton water after deducting the consumption of sodium hypochlorite according to the price accounting of 700 yuan/ton sodium hypochlorite.
Example 2
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 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 150 ml of membrane tank sludge subjected to lateral flow pretreatment and lateral flow primary lateral flow hydrolytic acidification, washing with clear water for several times, adding return sludge equivalent to membrane tank return 15% Q into the secondary lateral flow anaerobic fermentation tank, 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 28mg N/L. In actual operation, glucose is added as a carbon source if necessary to remove 28mg of N/L total nitrogen,the cost of carbon source consumption is 0.504 yuan/ton water (calculated by glucose 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 total nitrogen of 28mg N/L, the method disclosed by the utility model can help the water plant to reduce the consumption of carbon source and drug by 0.46 yuan/ton of water after deducting the drug consumption of the liquid caustic according to the price of the liquid caustic of 800 yuan/ton.
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 (10)
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), the pretreatment reaction tank (4) and 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 an 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).
2. The sewage treatment system for generating carbon source by utilizing sewage plant sludge hydrolytic acidification according to claim 1, wherein the biochemical sludge separation and interception system (2) is a secondary sedimentation tank or a membrane tank.
3. The sewage treatment system for generating a carbon source by utilizing hydrolytic acidification of sludge from a sewage plant as claimed in claim 1, wherein 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).
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 sludge concentration tank (3) is further connected to an inlet of the pretreatment reaction tank (4).
5. 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.
6. 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.
7. 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).
8. 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).
9. 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 primary side-stream hydrolysis and acidification tank (5) and the secondary side-stream anaerobic fermentation tank (6) are formed as an integrated device, and are separated by a partition wall or a partition plate.
10. 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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