High-suspended sewage treatment method and application thereof

Abstract

The application provides a high-suspension sewage treatment method and application thereof, wherein the method comprises the following steps: 1) hydrolytic phase separation treatment is performed on the feed sewage to obtain turbid-phase sewage and clear-phase sewage; 2) the turbid-phase sewage is subjected to turbid-phase anaerobic sequencing batch digestion treatment to obtain turbid-phase sludge, turbid-phase biogas slurry and turbid-phase biogas; the clear-phase sewage is subjected to clear-phase anaerobic sequencing batch digestion treatment to obtain clear-phase sludge, clear-phase biogas and clear-phase anaerobic sequencing batch digestion effluent. The high-suspension sewage treatment method provided by the application can adapt to the decomposition and conversion rate difference of soluble organic matter and insoluble organic matter, and can also adapt to the characteristics of feed sewage with large water quantity and water quality fluctuation.

Description

TECHNICAL FIELD

[0001] The present application relates to a high-suspended sewage treatment method, in particular to a high-suspended sewage treatment method and its application, and belongs to the technical field of environmental engineering. BACKGROUND

[0002] With the continuous intensification of livestock and poultry farms, the tightening of environmental protection policies and the strengthening of environmental protection supervision, the large amount of high-suspended sewage and the high cost of high-suspended sewage treatment are one of the major problems faced by pig enterprises. The practical and feasible livestock and poultry high-suspended sewage treatment and resource utilization technology is paid more and more attention. According to the different situations of local environmental protection policy, geographical location, available land quantity, adjacent water system environment, etc., there are currently several modes for high-suspended sewage treatment process, which are anaerobic digestion and then field application of biogas slurry, anaerobic black film pool storage and then field application, and anaerobic digestion and then discharge or irrigation of standard treatment effluent. However, no matter which mode, anaerobic digestion is one of the core technology units. At present, the common anaerobic digestion forms of high-suspended sewage treatment mainly include continuous stirred tank reactor (CSTR) and upflow anaerobic sludge bed reactor (UASB), etc. However, the organic matter in high-suspended sewage still exists in solid form. About 57% to 80% of the volatile solids in high-suspended sewage exist in the form of suspended (insoluble) volatile solids. The decomposition and conversion rates of dissolved and insoluble organic matter are different. The design and operation of many existing anaerobic reactors cannot guarantee the sufficient conversion of insoluble organic matter.

[0003] In addition, the water quality and quantity of high-suspended sewage fluctuate greatly due to different digestion and metabolism of different pigs and changes in water use and pollution during the breeding process. The water content of high-suspended sewage fluctuates greatly. However, the commonly used anaerobic digestion reactor cannot well adapt to such fluctuations, and the decomposition and conversion efficiency is low. Moreover, when the drainage capacity of the pig house suddenly increases, the hydraulic retention time of anaerobic digestion will instantaneously become very small, causing a large number of anaerobic microorganisms to be washed out of the fermentation tank, thereby seriously affecting the stability and fermentation efficiency of anaerobic digestion.

[0004] Under the standard discharge mode, the activated sludge method based on the anoxic / oxic (A / O) process is currently used to further remove nitrogen, phosphorus and organic matter from the anaerobically digested wastewater. However, this process produces a large amount of excess sludge, resulting in high dewatering agent costs and difficult sludge treatment and disposal. The low degree of sludge homogeneity caused by the segmented production and multiple flocculation of sludge in the existing high-suspended sewage treatment system also increases the difficulty of flocculation and dewatering in the final sludge dewatering process.

[0005] The livestock and poultry high-suspended substance sewage harmless treatment and resource utilization-based planting and breeding combined mode is one of the important trends at present, however, the connection of the current high-suspended substance sewage treatment and field application is single, which cannot well follow the nutrient and water demand rules in the planting process. In addition, in some cases, the high-suspended substance sewage is mixed with more inorganic substances such as sand, which not only increases the risk of equipment and facility blockage and wear, but also increases the overall sludge yield of the high-suspended substance sewage treatment system, reduces the volume efficiency of the treatment system, increases the maintenance cost, and makes the sludge treatment more difficult.

[0006] In summary, the current commonly used high-suspended substance sewage treatment process system has the following deficiencies: the anaerobic unit cannot well adapt to the difference in the decomposition and conversion rates of soluble and insoluble organic matters, thereby leading to insufficient degradation of insoluble organic matters; the anaerobic unit cannot well adapt to the fluctuation of the water content and water quantity of high-suspended substance sewage.

[0007] Therefore, developing a sewage treatment method that can adapt to the difference in the decomposition and conversion rates of soluble and insoluble organic matters and also adapt to the fluctuation of the water quantity and quality of the feed sewage has become the research direction at present. SUMMARY

[0008] The present application provides a high-suspended substance sewage treatment method, which has the characteristics of being able to adapt to the difference in the decomposition and conversion rates of soluble and insoluble organic matters and also adapt to the fluctuation of the water quantity and quality of the feed sewage.

[0009] The present application also provides a high-suspended substance sewage treatment system, which has the characteristics of being able to adapt to the difference in the decomposition and conversion rates of soluble and insoluble organic matters and also adapt to the fluctuation of the water quantity and quality of the feed sewage.

[0010] The present application provides a high-suspended substance sewage treatment method, which comprises the following steps:

[0011] 1) hydrolyzing and separating the feed sewage to obtain turbid-phase sewage and clear-phase sewage;

[0012] 2) performing turbid-phase anaerobic sequencing batch digestion treatment on the turbid-phase sewage to obtain turbid-phase sludge, turbid-phase biogas slurry and turbid-phase biogas, and performing clear-phase anaerobic sequencing batch digestion treatment on the clear-phase sewage to obtain clear-phase sludge, clear-phase biogas and clear-phase anaerobic sequencing batch digestion effluent.

[0013] The method described above further comprises sequentially performing short-cut nitrification treatment and anaerobic ammonia oxidation treatment on the clear-phase anaerobic sequencing batch digestion effluent to obtain short-cut nitrification sludge and anaerobic ammonia oxidation effluent.

[0014] The method as described above, wherein, before the step of performing the short-cut nitrification treatment on the effluent of the clear-phase anaerobic sequencing batch reactor treatment, the method further comprises sequentially performing a primary coagulation and flocculation treatment and a primary sedimentation treatment on the effluent of the clear-phase anaerobic sequencing batch reactor treatment to obtain primary sedimentation sludge.

[0015] The method as described above, wherein the method further comprises sequentially performing a secondary sedimentation treatment and a Fenton treatment on the effluent of the anaerobic ammonia oxidation treatment to obtain secondary sedimentation sludge and Fenton-treated effluent.

[0016] The method as described above, wherein the method further comprises sequentially performing a secondary coagulation and flocculation treatment, a final sedimentation treatment and a disinfection treatment on the Fenton-treated effluent to obtain final sedimentation sludge and disinfected effluent.

[0017] The method as described above, wherein the method further comprises performing a hydrolytic fractionation treatment on the short-cut nitrification sludge, the primary sedimentation sludge, the secondary sedimentation sludge and the final sedimentation sludge.

[0018] The method as described above, wherein the method further comprises performing a sludge dewatering treatment on the turbid-phase sludge and the clear-phase sludge to obtain dewatered sludge and dewatered biogas slurry, and performing an aging treatment on the dewatered biogas slurry to obtain aged biogas slurry; and / or,

[0019] The method as described above, wherein the method further comprises performing a biogas slurry aging treatment on the turbid-phase biogas slurry to obtain aged biogas slurry.

[0020] The present application also provides a high-suspended solid wastewater treatment system, which can perform any of the above high-suspended solid wastewater treatment methods. The system comprises a hydrolytic fractionation tank, a turbid-phase anaerobic sequencing batch reactor tank, a clear-phase anaerobic sequencing batch reactor tank,

[0021] The turbid-phase wastewater outlet of the hydrolytic fractionation tank is in communication with the turbid-phase wastewater inlet of the turbid-phase anaerobic sequencing batch reactor tank;

[0022] The clear-phase wastewater outlet of the hydrolytic fractionation tank is in communication with the clear-phase wastewater inlet of the clear-phase anaerobic sequencing batch reactor tank.

[0023] The system as described above, wherein the system further comprises a primary coagulation and flocculation tank, a primary sedimentation tank, a short-cut nitrification tank, an anaerobic ammonia oxidation tank, a secondary sedimentation tank, a Fenton reaction tank, a secondary coagulation and flocculation tank, a final sedimentation tank, a disinfection tank, and a clear water tank.

[0024] The effluent outlet of the primary coagulation and flocculation tank is in communication with the supernatant outlet of the clear-phase anaerobic sequencing batch reactor tank;

[0025] The effluent outlet of the primary coagulation and flocculation tank is in communication with the effluent inlet of the primary sedimentation tank;

[0026] The supernatant outlet of the primary sedimentation tank is in communication with the effluent inlet of the short-cut nitrification tank;

[0027] the supernatant outlet of the short-cut nitrification tank is in communication with the stream inlet of the anammox tank;

[0028] the supernatant outlet of the anammox tank is in communication with the stream inlet of the secondary sedimentation tank;

[0029] the supernatant outlet of the secondary sedimentation tank is in communication with the stream inlet of the Fenton reaction tank;

[0030] the stream outlet of the Fenton reaction tank is in communication with the stream inlet of the secondary coagulation and flocculation tank;

[0031] the stream outlet of the secondary coagulation and flocculation tank is in communication with the stream inlet of the final sedimentation tank;

[0032] the supernatant outlet of the final sedimentation tank is in communication with the stream inlet of the disinfection tank;

[0033] the stream outlet of the disinfection tank is in communication with the stream inlet of the clear water tank.

[0034] The system as described above, wherein, further comprising a grating machine, a grit chamber, a cyclone sand remover, a conditioning tank, a biogas heat and electricity utilization device, a biogas slurry aging pond, a water and fertilizer mixing tank, a sludge dewatering machine, a sludge tank;

[0035] The grating machine, the grit chamber, the cyclone sand remover, and the conditioning tank are sequentially communicated, and the stream outlet of the conditioning tank is in communication with the stream inlet of the hydrolysis and phase separation tank;

[0036] The biogas inlets of the biogas heat and electricity utilization device are respectively in communication with the biogas outlets of the hydrolysis and phase separation tank, the turbid-phase anaerobic sequencing batch reactor, and the clear-phase anaerobic sequencing batch reactor;

[0037] The sludge inlets of the sludge tank are respectively in communication with the sludge outlets of the short-cut nitrification tank, the primary sedimentation tank, the secondary sedimentation tank, and the final sedimentation tank;

[0038] The sludge outlet of the sludge tank is in communication with the sludge inlet of the conditioning tank;

[0039] The sludge outlet of the turbid-phase anaerobic sequencing batch reactor is in communication with the sludge inlet of the sludge dewatering machine;

[0040] The biogas slurry inlets of the biogas slurry aging pond are respectively in communication with the biogas slurry outlets of the sludge dewatering machine and the turbid-phase anaerobic sequencing batch reactor;

[0041] The aged biogas slurry outlet of the biogas slurry aging pond and the clear water outlet of the clear water tank are respectively in communication with the water and fertilizer mixing tank;

[0042] The sludge outlet of the anaerobic ammonia oxidation tank is communicated with the sludge outlet of the secondary sedimentation tank.

[0043] The sludge outlet of the biogas slurry aging pond is communicated with the sludge inlet of the sludge dewatering machine.

[0044] The high-suspended sewage treatment method provided by the application has the characteristics of being adaptable to the decomposition and conversion rate difference of soluble and insoluble organic matters and being adaptable to large water quantity and water quality fluctuation of the feed sewage. BRIEF DESCRIPTION OF DRAWINGS

[0045] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings required to be used in the embodiments or the prior art description will be simply introduced one by one below, and obviously, the drawings in the following description are some embodiments of the present application, and for those skilled in the art, other drawings can also be obtained without creative labor.

[0046] Figure 1 The device connection schematic diagram of the sewage treatment system provided by the application.

[0047] MARK NUMBER EXPLANATION:

[0048] 1 - grating machine; 2 - grit chamber; 3 - cyclone grit remover; 4 - regulating tank; 5 - hydrolysis phase separation tank; 6 - turbid phase anaerobic sequencing batch digester; 7 - clear phase anaerobic sequencing batch digester; 8 - biogas heat and electricity utilization device; 9 - primary coagulation and flocculation tank; 10 - primary sedimentation tank; 11 - short-cut nitrification tank; 12 - anaerobic ammonia oxidation tank, 13 - secondary sedimentation tank, 14 - Fenton reaction tank; 15 - secondary coagulation and flocculation tank; 16 - final sedimentation tank, 17 - disinfection tank; 18 - clear water tank; 19. biogas slurry aging pond; 20 - water and fertilizer mixing tank; 21 - sludge dewatering machine; 22 - sludge tank; A - high-suspended sewage; B - sand and gravel utilization disposal; C - sludge disposal treatment; D - biogas slurry field return or water and fertilizer integration. DETAILED DESCRIPTION

[0049] In order to make those skilled in the art better understand the technical solutions of the present application, the present application will be further described in detail below. The following specific embodiments are only used to describe the principles and characteristics of the present application, and the examples are used to explain the present application, but not to limit the scope of the present application. Based on the embodiments of the present application, all other embodiments obtained by those skilled in the art without creative labor are within the scope of protection of the present application.

[0050] The first aspect of the present application provides a high-suspended sewage treatment method, which comprises the following steps:

[0051] 1) hydrolysis phase separation treatment is performed on the feed sewage to obtain turbid phase sewage and clear phase sewage;

[0052] 2) the turbid-phase wastewater is subjected to turbid-phase anaerobic sequencing batch digestion to obtain turbid-phase sludge, turbid-phase biogas slurry and turbid-phase biogas; and the clear-phase wastewater is subjected to clear-phase anaerobic sequencing batch digestion to obtain clear-phase sludge, clear-phase biogas, and clear-phase anaerobic sequencing batch digestion effluent.

[0053] The hydrolysis and phase separation treatment is used for dissolving, hydrolyzing and small-moleculeizing the organic matter in an anaerobic state, and forming a clear-phase wastewater with low suspended solid content in the upper part of the tank and a turbid-phase wastewater with high suspended solid content in the lower part of the tank through natural sedimentation of the suspended matter in the sedimentation time sequence phase. The turbid-phase wastewater is subjected to turbid-phase anaerobic sequencing batch digestion to obtain turbid-phase sludge (bottom sediment), turbid-phase biogas slurry (liquid above the sediment) and turbid-phase biogas; and the clear-phase wastewater is subjected to clear-phase anaerobic sequencing batch digestion to obtain clear-phase sludge (bottom sediment), clear-phase biogas, and clear-phase anaerobic sequencing batch digestion effluent (liquid above the sediment, overflow effluent).

[0054] The turbid-phase anaerobic sequencing batch digestion and the clear-phase anaerobic sequencing batch digestion are both used for further dissolving, hydrolyzing and small-moleculeizing the organic matter in the treated matter in an anaerobic condition, and the difference lies in that the two have different hydraulic retention times. Since the organic matter content in the treated matter of the turbid-phase anaerobic sequencing batch digestion is higher, the hydraulic retention time of the treated matter in the turbid-phase anaerobic sequencing batch digestion is higher. In the high-suspended wastewater treatment method provided by the present application, the hydraulic retention time of the treated matter in the turbid-phase anaerobic sequencing batch digestion is 10-12 d, and the hydraulic retention time of the treated matter in the clear-phase anaerobic sequencing batch digestion is 2-4 d.

[0055] The above-mentioned treatment of the clear-phase and the turbid-phase respectively obtains biogas, biogas slurry, sludge and clear-phase anaerobic sequencing batch digestion effluent. The biogas, the biogas slurry and the sludge can be recycled and reused by using the common technology in the field, and the clear-phase anaerobic sequencing batch digestion effluent can be used as needed or further treated to further improve the water quality.

[0056] In an embodiment, the hydraulic retention time of the treated matter in the hydrolysis and phase separation treatment is 3-5 d.

[0057] The high-suspended wastewater treatment method provided by the present application realizes turbid-clear phase separation of the solid organic matter and the soluble organic matter of the high-suspended wastewater through the sedimentation process in the hydrolysis and phase separation tank, so that different anaerobic digestion forms can be better matched according to the characteristics of different materials, which can adapt to the decomposition and conversion rate difference of the soluble organic matter and the insoluble organic matter, and can also adapt to the characteristics of the large water quantity and water quality fluctuation of the feed wastewater.

[0058] In an embodiment, the high-suspended sludge treatment method provided by the present application further comprises sequentially performing short-cut nitrification treatment and anaerobic ammonia oxidation treatment on the effluent of the clear-phase anaerobic sequencing batch digestion to obtain short-cut nitrification sludge and anaerobic ammonia oxidation effluent.

[0059] The short-cut nitrification treatment on the effluent of the clear-phase anaerobic sequencing batch digestion can oxidize ammonia nitrogen in the effluent to nitrite nitrogen to obtain short-cut nitrification effluent; the short-cut nitrification effluent is subjected to anaerobic ammonia oxidation treatment to obtain anaerobic ammonia oxidation effluent. Specifically, the anaerobic ammonia oxidation treatment uses ammonia as an electron donor and nitrite as an electron acceptor to generate nitrogen to achieve denitrification; the denitrification process of short-cut nitrification-anaerobic ammonia oxidation does not need to consume carbon source, and the energy consumption of aeration is saved by about 60%, and the denitrification sludge is reduced by about 85%, so that the energy consumption, sludge production and dewatering agent cost of the high-suspended sludge treatment system can be reduced.

[0060] In an embodiment, the effluent of the clear-phase anaerobic sequencing batch digestion can also be divided into two parts, the first part is sequentially subjected to short-cut nitrification treatment and anaerobic ammonia oxidation treatment, and the other part is not subjected to short-cut nitrification treatment but is subjected to anaerobic ammonia oxidation treatment after being mixed with the short-cut nitrification effluent. This method can provide more sufficient carbon source and further reduce the energy consumption and operating cost of the system.

[0061] In an embodiment, the high-suspended sludge treatment method provided by the present application further comprises sequentially performing primary coagulation and flocculation treatment and primary sedimentation treatment on the effluent of the clear-phase anaerobic sequencing batch digestion to obtain primary sedimentation sludge before the short-cut nitrification treatment on the effluent of the clear-phase anaerobic sequencing batch digestion.

[0062] The primary coagulation and flocculation treatment adds lime and cationic polyacrylamide flocculants to the effluent of the clear-phase anaerobic sequencing batch digestion to make the suspended substances in the effluent gather into precipitates by the principle of net capture and sweeping, and the precipitates are removed in the primary sedimentation treatment. The primary coagulation and flocculation treatment and the primary sedimentation treatment on the effluent of the clear-phase anaerobic sequencing batch digestion before the short-cut nitrification treatment can help reduce the load of the subsequent treatment process such as the short-cut nitrification treatment, and further reduce the energy consumption and operating cost of the system.

[0063] In an embodiment, the high-suspended sludge treatment method provided by the present application further comprises sequentially performing secondary sedimentation treatment and Fenton treatment on the anaerobic ammonia oxidation effluent to obtain secondary sedimentation sludge and Fenton treatment effluent.

[0064] Secondary sedimentation treatment is a second sedimentation treatment after primary sedimentation treatment, which can remove the suspended solids in the effluent of anaerobic ammonia oxidation treatment by gravity sedimentation; Fenton treatment generates hydroxyl radicals by chain reaction between divalent iron ions and hydrogen peroxide, and further oxidizes and degrades the organic matters in the effluent of secondary sedimentation treatment, which helps to further improve the water quality of the effluent.

[0065] The present application does not limit the treatment conditions of Fenton treatment, and the conditions commonly used in the art can be used. In an embodiment, the pH of Fenton treatment is 3-5, the mass ratio of hydrogen peroxide to chemical oxygen demand is 1-2:1, the molar ratio of hydrogen peroxide to ferrous sulfate is 1-10:1, the hydraulic retention time is 2.0-8.0 h, and the content of suspended solids in the effluent of secondary sedimentation treatment is less than 200 mg / L.

[0066] In an embodiment, the high-suspended sewage treatment method provided by the present application further comprises sequentially performing secondary coagulation and flocculation treatment, final sedimentation treatment and disinfection treatment on the effluent of Fenton treatment to obtain final sedimentation sludge and disinfection effluent.

[0067] The secondary coagulation and flocculation treatment adds lime and cationic polyacrylamide flocculants to the effluent of Fenton treatment, and the suspended solids in the treated material are aggregated into precipitates by the principle of net capture and sweeping, and are removed in the final sedimentation treatment. The effluent of final sedimentation treatment is subjected to disinfection treatment to meet the discharge or use standard.

[0068] The present application does not limit the treatment conditions of disinfection treatment, and the conditions commonly used in the art can be used. In an embodiment, the disinfection treatment is ultraviolet disinfection, and a channel type ultraviolet disinfection system is used, the cleaning method adopts online mechanical and chemical cleaning method, the effective dose of ultraviolet disinfection is preferably 15-25 mJ / cm according to test data, the channel water flow is uniformly irradiated, and the channel length before and after the lamp is 1-3 m; in another embodiment, the disinfection treatment is chlorine dioxide, sodium hypochlorite and liquid chlorine disinfection, and the chlorine dosage is determined according to test data, when there is no test data, 5-15 mg / L is used, and the chlorine dioxide, sodium hypochlorite or chlorine should be mixed and contacted after disinfection, and the contact time should not be less than 30 min.

[0069] In an embodiment, the high-suspended sewage treatment method provided by the present application further comprises hydrolysis and phase separation treatment on the sludge of short-cut nitrification treatment, primary sedimentation treatment, secondary sedimentation treatment and final sedimentation treatment.

[0070] The sludge of the primary settling tank, the short distance nitrification tank, the secondary settling tank and the final settling tank is mixed with the high-suspended substance sewage in the adjusting tank, and then is subjected to hydrolysis and phase separation treatment, so that the suspended substance is dissolved, hydrolyzed and settled, and then is subjected to turbid phase anaerobic sequencing batch digestion treatment with the turbid phase sewage, so as to degrade the organic matter in the sludge into biogas and anaerobic sludge with uniform properties, thereby reducing the sludge yield of the high-suspended substance sewage treatment system, reducing the flocculation difficulty and saving the dewatering agent cost.

[0071] In an embodiment, the high-suspended substance sewage treatment method provided by the application further comprises subjecting the turbid phase sludge and the clear phase sludge to sludge dewatering treatment to obtain dewatered sludge and dewatered biogas liquid, and subjecting the dewatered biogas liquid to aging treatment to obtain aged biogas liquid.

[0072] The sludge dewatering process produces biogas liquid, which contains a large amount of organic matter, and the part of the biogas liquid can be subjected to aging treatment together with the turbid phase biogas liquid, so that the organic matter in the biogas liquid is decomposed into small molecular substances, which are convenient for reuse, so as to improve the energy utilization rate of the system.

[0073] The second aspect of the application provides a high-suspended substance sewage treatment system for executing any one of the high-suspended substance sewage treatment methods described above, which comprises a hydrolysis and phase separation tank, a turbid phase anaerobic sequencing batch digestion tank and a clear phase anaerobic sequencing batch digestion tank.

[0074] The turbid phase sewage outlet of the hydrolysis and phase separation tank is in communication with the turbid phase sewage inlet of the turbid phase anaerobic sequencing batch digestion tank.

[0075] The clear phase sewage outlet of the hydrolysis and phase separation tank is in communication with the clear phase sewage inlet of the clear phase anaerobic sequencing batch digestion tank.

[0076] The hydrolysis and phase separation tank is used for executing hydrolysis and phase separation treatment on the feed sewage. The meaning of the hydrolysis and phase separation treatment is the same as described above, and will not be described herein again.

[0077] In the system provided by the application, the hydrolysis and phase separation tank is a circular cement tank, an enamel steel tank or a stainless steel assembled tank provided with a mechanical stirring device, the hydraulic retention time is 3-5 days, the temperature range at normal temperature operation is 20-25℃, the temperature range at medium temperature operation is 30-37℃, and the temperature range at high temperature operation is 50-55℃, and the operation time sequence of "feeding-reaction-settling-discharging" is consistent, the feeding time is set to 16-22 hours, the reaction time is set to 1.0-6.0 hours, and the settling time is set to 0.5-2.0 hours.

[0078] The hydrolysis and phase separation tank is provided with a turbid phase sewage outlet and a clear phase sewage outlet, and the elevation of the turbid phase sewage outlet is lower than that of the clear phase sewage outlet. The turbid phase sewage outlet is communicated with a turbid phase sewage inlet of the turbid phase anaerobic sequencing tank, and the clear phase sewage outlet is communicated with a clear phase sewage inlet of the clear phase anaerobic sequencing tank. The turbid phase sewage and the clear phase sewage obtained by hydrolysis and phase separation treatment of the feed sewage are respectively introduced into the turbid phase anaerobic sequencing tank and the clear phase anaerobic sequencing tank for further treatment.

[0079] The turbid phase anaerobic sequencing tank is used for turbid phase anaerobic sequencing treatment of the turbid phase sewage. The turbid phase anaerobic sequencing treatment has the same meaning as above, and will not be repeated here.

[0080] In the system provided by the application, the turbid phase anaerobic sequencing tank is a circular cement pool, an enamel steel tank or a stainless steel assembled tank provided with a mechanical stirring device, the hydraulic retention time is 10-12 d, the temperature range during normal temperature operation is 20-25 DEG C, the temperature range during medium temperature operation is 30-37 DEG C, the temperature range during high temperature operation is 50-55 DEG C, the time sequence operation of "feeding-reaction-settling-discharging" is adopted, the time sequences of the three are consistent, the feeding time is set to 16-22 h, the reaction time is set to 1.0-6.0 h, the settling time is set to 0.5-2.0 h, the bottom sludge discharge pump discharges turbid phase sludge once every 1-7 d, and the discharge amount is 0.1-1.0 times of the daily water inflow.

[0081] In addition, the turbid phase anaerobic sequencing tank also produces turbid phase biogas and turbid phase biogas slurry, which can be recycled according to requirements.

[0082] The clear phase anaerobic sequencing tank is used for clear phase anaerobic sequencing treatment of the clear phase sewage. The clear phase anaerobic sequencing treatment has the same meaning as above, and will not be repeated here.

[0083] In the system provided by the application, the clear phase anaerobic sequencing tank is a circular cement pool, an enamel steel tank or a stainless steel assembled tank provided with a hydraulic circulating stirring device, the hydraulic retention time is 2-4 d, the temperature range during normal temperature operation is 20-25 DEG C, the temperature range during medium temperature operation is 30-37 DEG C, the temperature range during high temperature operation is 50-55 DEG C, the time sequence operation of "feeding-reaction-settling-discharging" is adopted, the time sequences of the three are consistent, the feeding time is set to 16-22 h, the reaction time is set to 1.0-6.0 h, and the settling time is set to 0.5-2.0 h. The bottom sludge discharge pump discharges clear phase sludge once every 1-20 d, and the discharge amount is 0.1-1.0 times of the daily water inflow.

[0084] In addition, the clear-phase anaerobic sequencing tank also produces clear-phase biogas and clear-phase anaerobic sequencing treatment effluent, wherein the clear-phase biogas can be recycled according to the requirement, and the clear-phase anaerobic sequencing treatment effluent can be directly used or further treated.

[0085] Further, in an embodiment, the feeding and discharging of the hydrolysis and phase separation tank are simultaneously performed, the feeding is performed by a hydrolysis and phase separation tank feeding pump, the discharging is performed by feeding pumps of the turbid-phase anaerobic sequencing tank and the clear-phase anaerobic sequencing tank, the feeding pumps of the turbid-phase anaerobic sequencing tank and the clear-phase anaerobic sequencing tank are started and stopped in linkage with the hydrolysis and phase separation tank feeding pump, the flow rate thereof is determined according to the residence time of the corresponding tank and the turbid-phase / clear-phase split ratio, and the sum of the flow rates of the two pumps should be consistent with the flow rate of the hydrolysis and phase separation tank feeding pump;

[0086] The feeding of the turbid-phase anaerobic sequencing tank and the clear-phase anaerobic sequencing tank is completed by respective feeding pumps, and the discharging mode is overflow effluent;

[0087] The stirring devices of the hydrolysis and phase separation tank, the turbid-phase anaerobic sequencing tank and the clear-phase anaerobic sequencing tank are only operated in the reaction time sequence section, the stirring is started after the feeding is completed, and the stirring is stopped after the reaction time is completed, the stirring can be continuous or intermittent, when the intermittent stirring is adopted, the stirring is performed for 0.5-1.0 h, and then stopped for 10-30 min; the pump flow rate of the hydraulic circulation stirring is 1.0-3.0 times of the feeding pump flow rate.

[0088] The turbid phase anaerobic sequencing tank and the clear phase anaerobic sequencing tank respectively receive the turbid phase and the clear phase of the hydrolysis separation tank, and different hydraulic retention times and stirring forms are set according to the characteristics of the materials; the sequencing digestion mode adopted by the two digestion tanks can retain most of the suspended solids and microorganisms in the tank due to the setting of the sedimentation process, so that only supernatant with low organic matter, low suspended solid content and low microorganism content is overflowed out of the tank body in the water inflow stage, the insoluble organic matter contained in the suspended solids can obtain a solid retention time significantly greater than the hydraulic retention time to continue decomposition and conversion; the retention of microorganisms can also maintain a high concentration of anaerobic microorganisms in the tank, and the full contact of organic matter and microorganisms brought by the stirring in the reaction stage can further improve the decomposition and conversion efficiency of the insoluble organic matter; the retention of the insoluble organic matter and the microorganisms in the anaerobic sequencing digestion mode can obtain a larger solid retention time and a microorganism retention time with a lower hydraulic retention time, so that it can adapt to the characteristics that the soluble organic matter and the insoluble organic matter in the high-suspended matter sewage exist at the same time and have different degradation rates, and can maintain good anaerobic digestion and decomposition and conversion performance even in the case that the water content and the water volume of the high-suspended matter sewage fluctuate greatly; the improvement of the degradation degree of the insoluble organic matter can effectively reduce the amount of suspended solids finally converted into sludge, thereby reducing the sludge production amount and the dewatering agent cost; the reduction of the suspended matter in the overflow water of the clear phase anaerobic sequencing tank can also reduce the agent cost of the primary coagulation and flocculation.

[0089] The high-suspended sewage treatment system provided by the application realizes the turbid and clear separation of the solid organic matter and the soluble organic matter in the high-suspended sewage in the hydrolysis separation tank through the sedimentation process, so that different subsequent anaerobic digestion forms can be better matched according to different material characteristics.

[0090] In one embodiment, the high-suspended sewage treatment system provided by the application further comprises a primary coagulation and flocculation tank, a primary sedimentation tank, a short-cut nitrification tank, an anaerobic ammonia oxidation tank, a secondary sedimentation tank, a Fenton reaction tank, a secondary coagulation and flocculation tank, a final sedimentation tank, a disinfection tank and a clear water tank.

[0091] The supernatant outlet of the primary coagulation and flocculation tank is in communication with the supernatant inlet of the primary sedimentation tank.

[0092] The supernatant outlet of the primary coagulation and flocculation tank is in communication with the supernatant inlet of the primary sedimentation tank.

[0093] The supernatant outlet of the primary coagulation and flocculation tank is in communication with the supernatant inlet of the primary sedimentation tank.

[0094] The supernatant outlet of the primary coagulation and flocculation tank is in communication with the supernatant inlet of the primary sedimentation tank.

[0095] The supernatant outlet of the primary coagulation and flocculation tank is in communication with the supernatant inlet of the primary sedimentation tank.

[0096] The supernatant outlet of the primary coagulation and flocculation tank is in communication with the supernatant inlet of the primary sedimentation tank.

[0097] The effluent outlet of the Fenton reaction tank is communicated with the influent inlet of the secondary coagulation and flocculation tank;

[0098] The effluent outlet of the secondary coagulation and flocculation tank is communicated with the influent inlet of the final sedimentation tank;

[0099] The supernatant outlet of the final sedimentation tank is communicated with the influent inlet of the disinfection tank;

[0100] The effluent outlet of the disinfection tank is communicated with the influent inlet of the clear water tank.

[0101] The primary coagulation and flocculation tank is used for primary coagulation and flocculation treatment of the effluent of the clear-phase anaerobic sequencing batch digestion.

[0102] In the system provided by the application, the primary coagulation and flocculation tank is a flat-bottomed square tank provided with a mechanical stirring device and a flocculating agent feeding device, the flocculating agent used is lime and cationic polyacrylamide, the concentration of the lime is 0.5% to 1%, the feeding ratio is 3% to 15% of the dry matter of the flocculation object, the concentration of the cationic polyacrylamide is 0.1% to 0.2%, and the feeding ratio is 0.3% to 0.5% of the dry matter of the flocculation object.

[0103] Further, the dosing equipment of the primary coagulation and flocculation tank is linked with the feed pump of the clear-phase anaerobic sequencing batch digestion tank to start and stop together.

[0104] The primary coagulation and flocculation tank is used for primary coagulation and flocculation treatment of the effluent of the clear-phase anaerobic sequencing batch digestion, and the primary flocculation and coagulation treatment effluent obtained is introduced into the primary sedimentation tank through the effluent outlet of the primary coagulation and flocculation tank and the influent inlet of the primary sedimentation tank.

[0105] The primary sedimentation tank is used for primary sedimentation treatment of the primary flocculation and coagulation treatment effluent. The meaning of the primary sedimentation treatment is the same as above, and will not be repeated here.

[0106] In the system provided by the application, the primary sedimentation tank is a conical-bottomed square tank provided with a sludge discharge port, the hydraulic retention time is 8 to 16 hours, and the effective water depth is 2.0 to 4.0 meters.

[0107] The primary sedimentation tank is used for primary sedimentation treatment of the primary flocculation and coagulation treatment effluent. The meaning of the primary sedimentation treatment is the same as above, and will not be repeated here.

[0108] The short-cut nitrification tank is used for short-cut nitrification treatment of the primary sedimentation treatment effluent. The meaning of the short-cut nitrification treatment is the same as above, and will not be repeated here.

[0109] The system provided by the application has a short-range nitrification tank which is a square tank with a conical bottom and is provided with a sludge discharge port and an aeration device, the hydraulic retention time is 1.5-3.5 days, the pH is controlled in the range of 7.0-8.5, the dissolved oxygen is controlled in the range of 0.5-1.0 mg / L through frequency conversion control, and the water temperature is 20-30℃.

[0110] The short-range nitrification tank is used for short-range nitrification treatment of the primary sedimentation effluent, and the short-range nitrification treatment effluent obtained is introduced into the ANAMMOX tank through the supernatant outlet of the short-range nitrification tank and the material flow inlet of the ANAMMOX tank.

[0111] The ANAMMOX tank is used for ANAMMOX treatment of the short-range nitrification treatment effluent. The meaning of ANAMMOX treatment is the same as above, and will not be repeated here.

[0112] The system provided by the application has an ANAMMOX tank which is a square tank with a conical bottom and is provided with fillers, the fillers are porous fillers, and the material is polyurethane, polyethylene or polypropylene, the concentration ratio of ammonia nitrogen to nitrite nitrogen is about 1:1.0-1.2 by controlling the inflow of the primary sedimentation effluent and the short-range nitrification tank effluent, the hydraulic retention time is 0.5-2.0 days, the pH is controlled in the range of 7.0-8.0, and the water temperature is 20-30℃.

[0113] The ANAMMOX tank is used for ANAMMOX treatment of the short-range nitrification treatment effluent, and the ANAMMOX treatment effluent obtained is introduced into the secondary sedimentation tank through the supernatant outlet of the ANAMMOX tank and the material flow inlet of the secondary sedimentation tank.

[0114] In an embodiment, the clear-phase anaerobic sequencing batch digestion effluent can also be divided into two parts, the first part is sequentially subjected to short-range nitrification treatment and ANAMMOX treatment, and the other part is not subjected to short-range nitrification treatment but is subjected to ANAMMOX treatment after being mixed with the short-range nitrification treatment effluent. This kind of mode can provide more sufficient carbon source, and further reduce the energy consumption and operation cost of the system.

[0115] The secondary sedimentation tank is used for secondary sedimentation treatment of the ANAMMOX treatment effluent. The meaning of secondary sedimentation treatment is the same as above, and will not be repeated here.

[0116] The system provided by the application has a secondary sedimentation tank which is a square tank with a conical bottom and is provided with a sludge discharge port, the hydraulic retention time is 4-16 hours, and the effective water depth is 2.0-4.0 m. In an embodiment, the secondary sedimentation tank is further provided with a sludge return pipeline leading to the ANAMMOX tank as needed.

[0117] The secondary sedimentation tank is used for secondary sedimentation treatment of the ANAMMOX treatment effluent. The secondary sedimentation treatment effluent obtained is introduced into the Fenton reaction tank through the supernatant outlet of the secondary sedimentation tank and the material flow inlet of the Fenton reaction tank.

[0118] The Fenton reaction tank is used for Fenton treatment of the secondary sedimentation effluent. The meaning of Fenton treatment is the same as above, and will not be repeated here.

[0119] In the system, the Fenton reaction tank is a flat-bottomed square tank provided with a mechanical stirring device, a hydrogen peroxide and ferrous sulfate medicament feeding device, the hydraulic retention time is 2.0-8.0 h, the suspended solids content in the influent is less than 200 mg / L, the pH is controlled at 3-5, the mass ratio of hydrogen peroxide to chemical oxygen demand is 1-2:1, and the molar ratio of hydrogen peroxide to ferrous sulfate is 1-10:1.

[0120] The Fenton reaction tank is used for Fenton treatment of the secondary sedimentation effluent. The meaning of Fenton treatment is the same as above, and will not be repeated here.

[0121] The secondary coagulation and flocculation tank is used for secondary coagulation and flocculation treatment of the Fenton-treated effluent. The meaning of secondary coagulation and flocculation treatment is the same as above, and will not be repeated here.

[0122] In the system, the secondary coagulation and flocculation tank is a flat-bottomed square tank provided with a mechanical stirring device and a flocculating agent feeding device, the pH is adjusted to 5.5-8.5 by adding lime in the dosing equipment, the dosing concentration of lime is 0.5%-1%, the coagulant is polyaluminum chloride, and the dosage is 100-200 mg / L, and the coagulant aid is anionic polyacrylamide, and the dosage is 15-35 mg / L.

[0123] Further, the dosing equipment of the secondary coagulation and flocculation tank is linked to the feed pump of the clear-phase anaerobic sequencing batch digester for starting and stopping.

[0124] The secondary coagulation and flocculation tank is used for secondary coagulation and flocculation treatment of the Fenton-treated effluent. The meaning of secondary coagulation and flocculation treatment is the same as above, and will not be repeated here.

[0125] The secondary coagulation and flocculation tank is used for secondary coagulation and flocculation treatment of the Fenton-treated effluent. The meaning of secondary coagulation and flocculation treatment is the same as above, and will not be repeated here.

[0126] In the system, the secondary coagulation and flocculation tank is a flat-bottomed square tank provided with a mechanical stirring device and a flocculating agent feeding device, the pH is adjusted to 5.5-8.5 by adding lime in the dosing equipment, the dosing concentration of lime is 0.5%-1%, the coagulant is polyaluminum chloride, and the dosage is 100-200 mg / L, and the coagulant aid is anionic polyacrylamide, and the dosage is 15-35 mg / L.

[0127] The secondary coagulation and flocculation tank is used for secondary coagulation and flocculation treatment of the Fenton-treated effluent. The meaning of secondary coagulation and flocculation treatment is the same as above, and will not be repeated here.

[0128] The disinfection tank is used for disinfection treatment of the secondary coagulation and flocculation-treated effluent. The meaning of disinfection treatment is the same as above, and will not be repeated here.

[0129] In the system provided by this invention, the disinfection pool is a flat-bottomed square pool equipped with a disinfection device. When the disinfection device is an ultraviolet disinfection device, an open channel ultraviolet disinfection system is adopted. The cleaning method is online mechanical and chemical cleaning. The effective dose of ultraviolet disinfection is preferably 15-25 mJ / cm based on experimental data. The water flow in the irradiation channel is uniform, and the channel length before and after the lamp is 1-3m. When the disinfection device is chlorine dioxide, sodium hypochlorite, or liquid chlorine, the chlorine dosage should be determined based on experimental data. When no experimental data is available, 5-15 mg / L is used. After disinfection with chlorine dioxide, sodium hypochlorite, or chlorine, they should be mixed and contacted, and the contact time should not be less than 30 minutes.

[0130] The disinfection tank disinfects the effluent from the final sedimentation treatment. The disinfected effluent then flows from the disinfection tank's outlet to the clear water tank's inlet, where it is stored for later use. The clear water tank is a flat-bottomed square tank with a hydraulic retention time of 4–16 hours and an effective water depth of 2.0–4.0 meters.

[0131] In one embodiment, the system provided by the present invention further includes a bar screen, a sedimentation tank, a cyclone separator, a regulating tank, a biogas thermal power utilization device, a biogas slurry aging pond, a water-fertilizer mixing tank, a sludge dewatering machine, and a sludge tank.

[0132] The bar screen, grit chamber, cyclone separator, and equalization tank are connected in sequence, and the material outlet of the equalization tank is connected to the material inlet of the hydrolysis phase separation tank.

[0133] The biogas inlet of the biogas power generation equipment is connected to the biogas outlet of the hydrolysis phase separation tank, the biogas outlet of the turbid phase anaerobic sequencing batch digester, and the biogas outlet of the clear phase anaerobic sequencing batch digester, respectively.

[0134] The sludge inlet of the sludge tank is connected to the sludge outlet of the short-cut nitrification tank, the sludge outlet of the primary sedimentation tank, the sludge outlet of the secondary sedimentation tank, and the sludge outlet of the final sedimentation tank, respectively.

[0135] The sludge outlet of the sludge tank is connected to the sludge inlet of the equalization tank.

[0136] The sludge outlet of the turbid phase anaerobic sequencing batch digester is connected to the sludge inlet of the sludge dewatering machine.

[0137] The biogas slurry inlet of the biogas slurry aging pond is connected to the biogas slurry outlet of the sludge dewatering machine and the biogas slurry outlet of the turbid phase anaerobic sequencing batch digester, respectively.

[0138] The biogas slurry outlet of the biogas slurry aging pond and the clear water outlet of the clear water pond are respectively connected to the water-fertilizer mixing tank;

[0139] The sludge outlet of the anaerobic ammonia oxidation tank is connected to the sludge outlet of the secondary sedimentation tank.

[0140] The sludge outlet of the biogas slurry aging pond is connected to the sludge inlet of the sludge dewatering machine.

[0141] The grid is used to remove sundries in the influent sewage, to avoid wear and tear of the treatment equipment, to remove large specific gravity in the sewage by the sand trap and the cyclone sand remover, and to reduce the pipe wear and tear. The adjusting tank is used to temporarily store the influent sewage, so that the system provided by the present application has stronger effect of resisting water quantity fluctuation.

[0142] The density difference of the sand and the high-suspended substance organic matter in the sewage is used to effectively remove the sand in the high-suspended substance sewage by gravity sedimentation and cyclone separation, so as to reduce the clogging and wear and tear of the equipment and facilities of the high-suspended substance sewage treatment system, reduce the maintenance cost, and reduce the sludge production of the high-suspended substance sewage treatment system by the early separation and removal of the sand.

[0143] The biogas heat and power equipment collects the biogas from the hydrolysis and phase separation tank, the turbid phase anaerobic sequencing batch reactor and the clear phase anaerobic sequencing batch reactor, and uses the biogas to generate electricity to realize energy recycling. The above-mentioned equipment is connected to the biogas heat and power utilization equipment by a pipeline; in one embodiment, the biogas heat and power utilization equipment includes auxiliary devices such as biogas dehydration and desulfurization and biogas storage devices.

[0144] Further, the heat and power utilization equipment reduces the water content of the biogas to below 1% and the hydrogen sulfide content to less than 100 ppm through the auxiliary biogas dehydration equipment, buffers the biogas through the biogas storage cabinet and balances the pressure of the gas production end and the gas use end, the volume of the biogas storage cabinet is 0.2-0.5 times the daily biogas production; the biogas generator or the biogas boiler is determined according to the daily biogas production, the sewage treatment system preferentially uses the electric energy generated by the biogas generator, automatically switches to the mains power supply when the power generation of the biogas generator is insufficient, and realizes the uninterrupted operation of the electric equipment through the uninterruptible power supply; the heat energy produced by the biogas boiler is preferentially supplied to the turbid phase anaerobic sequencing batch reactor, then to the clear phase anaerobic sequencing batch reactor, and then to the hydrolysis and phase separation tank, to maintain the appropriate fermentation temperature and reduce the temperature fluctuation as much as possible, and the fermentation temperature fluctuation of the digestion tank is not more than 1℃ per day; when the biogas production speed and the consumption speed do not match instantaneously, the biogas is fully combusted and discharged through the biogas burner.

[0145] The sludge tank collects the sludge from the short-cut nitrification tank, the primary sedimentation tank, the secondary sedimentation tank and the final sedimentation tank, discharges the above-mentioned sludge to the adjusting tank, and realizes the circulation of the sludge.

[0146] The sludge dewatering machine collects sludge from the turbid-phase anaerobic sequencing batch digester, and the biogas slurry aging pond collects biogas slurry from the sludge dewatering machine and from the turbid-phase anaerobic sequencing batch digester. In an embodiment, a sludge buffer tank is provided before the sludge dewatering machine, the sludge buffer tank is provided with high and low liquid level meters, the high liquid level meter controls the start and stop of the turbid-phase anaerobic sequencing batch digester discharge pump, the clear-phase anaerobic sequencing batch digester sludge discharge pump and the biogas slurry aging pond sludge discharge pump, and the low liquid level meter controls the start and stop of the sludge dewatering machine feed pump; when the sludge dewatering machine fails, the sludge enters the biogas slurry aging pond from the sludge buffer tank, bypassing the sludge dewatering machine.

[0147] The aging biogas slurry outlet of the biogas slurry aging pond and the clear water outlet of the clear water pool are respectively communicated with the water and fertilizer mixing tank, and the two can be mixed in the water and fertilizer mixing tank to realize biogas slurry field application or water and fertilizer integration.

[0148] In an embodiment, the sludge outlet of the anaerobic ammonia oxidation tank is communicated with the sludge outlet of the secondary sedimentation tank to realize sludge reflux, and the sludge outlet of the biogas slurry aging pond is communicated with the sludge inlet of the sludge dewatering machine to dewater the sludge generated by the aging pond.

[0149] The high-suspended wastewater treatment system provided by the application integrates organic and inorganic separation, hydrolysis and phase separation, anaerobic sequencing batch digestion, short-cut nitrification and anaerobic ammonia oxidation, sludge anaerobic digestion, and water and fertilizer allocation, effectively harmless, stabilizes and reduces high-suspended wastewater, and flexibly realizes the resource utilization of nutrients and water.

[0150] The high-suspended wastewater treatment system provided by the application separates sand and gravel from high-suspended wastewater, reduces the wear and siltation risk of subsequent pipes, pumps, valves and tank bodies, improves the volume efficiency of the fermentation tank, and reduces the maintenance cost of equipment and facilities.

[0151] The high-suspended wastewater treatment system provided by the application realizes turbid and clear phase separation of solid organic matter and soluble organic matter in high-suspended wastewater in the hydrolysis and phase separation tank through the settlement process, so that different anaerobic digestion forms are better matched according to the characteristics of different materials.

[0152] The high-suspended wastewater treatment system provided by the application respectively performs anaerobic sequencing batch digestion on turbid-phase and clear-phase materials, better adapts to the different water content characteristics of materials, and the characteristics that soluble organic matter and insoluble organic matter exist at the same time and have different degradation rates, effectively intercepts microorganisms and undegraded insoluble organic matter, makes the solid retention time and the microorganism retention time several times of the hydraulic retention time, improves the organic matter degradation rate, and reduces the investment in fermentation tanks.

[0153] The present application provides a high-suspended sewage treatment system, which adopts short-cut nitrification and anaerobic ammonia oxidation reaction to reduce the yield of biochemical sludge, introduces sludge of each process section into a turbid-phase anaerobic sequencing tank for anaerobic decomposition and conversion, further reduces the sludge production and the amount of dewatering agent of the overall treatment system to reduce the cost, and after the sludge of each unit is mixed and then subjected to anaerobic degradation, it is beneficial to form highly homogenized sludge and thus beneficial to efficient flocculation in the dewatering process.

[0154] The high-suspended sewage treatment system provided by the present application proportionally adjusts biogas slurry and standard water in a water and fertilizer mixing tank, flexibly carries out biogas slurry field returning, water and fertilizer integration and clean water irrigation and other planting and breeding integration operations, according to the fertilizer and water requirement law of crops, uses biogas slurry as base fertilizer before planting, uses water and fertilizer as topdressing during the growth of crops, and uses standard water for irrigation when the crops need water.

[0155] In one embodiment, the system further comprises a central control system, all flow meters, liquid level meters, stirring devices, dosing devices, pump groups and valves are connected to the central control system, and the pump groups, valves, stirring and dosing are started or stopped according to the clock setting; the regulating tank is provided with high and low liquid level meters, the high liquid level meter controls the start and stop of the grit chamber discharge pump, and the low liquid level meter controls the start and stop of the hydrolysis and phase separation tank feed pump; the inlet of the regulating tank, the inlet of the hydrolysis and phase separation tank, the inlets of the turbid-phase anaerobic sequencing tank and the clear-phase anaerobic sequencing tank, the dosing equipment, the inlet of the short-cut nitrification tank, the inlet of the anaerobic ammonia oxidation tank and the inlet of the water and fertilizer mixing tank are all provided with flow meters connected to the central control system, the central control system controls the flow of each device, the short-cut nitrification tank is provided with a dissolved oxygen monitoring device connected to the central control system to assist in frequency conversion control of the aeration air volume, and the operation state checking, operation data statistics and operation parameter setting of all devices are operated through the central control system on the computer end and the mobile phone end.

[0156] The high-suspended sewage treatment method and application provided by the present application are explained in detail through specific examples.

[0157] Embodiment

[0158] The present embodiment uses Figure 1 the sewage treatment system shown in the figure to treat high-suspended sewage.

[0159] As Figure 1 shown, the system comprises a grating machine 1, a grit chamber 2, a cyclone sand remover 3, a regulating tank 4, a hydrolysis and phase separation tank 5, a turbid-phase anaerobic sequencing tank 6, a clear-phase anaerobic sequencing tank 7, a biogas heat and electricity utilization equipment 8, a primary coagulation and flocculation tank 9, a primary sedimentation tank 10, a short-cut nitrification tank 11, an anaerobic ammonia oxidation tank 12, a secondary sedimentation tank 13, a Fenton reaction tank 14, a secondary coagulation and flocculation tank 15, a final sedimentation tank 16, a disinfection tank 17, a clean water tank 18, a biogas slurry aging pond 19, a water and fertilizer mixing tank 20, a sludge dewatering machine 21 and a sludge tank 22.

[0160] The grid machine 1 is installed on the inlet channel of the grit chamber, the screen mesh aperture of the grid machine is 3-10 mm, the outlet water of the grid machine 1 enters the grit chamber 2 through the channel; the grid machine 1 is mainly used for removing the pig hair, ear tags, gloves, plastic bottles and other sundries mixed in the high-suspended substance sewage; the grit chamber 2 is used for depositing most of the silt in the high-suspended substance sewage.

[0161] The grit chamber is a square pool with a conical bottom, the bottom of the grit chamber 2 is connected with the cyclone sand remover 3 through a pump and a pipeline; the sand and gravel separated from the cyclone sand remover 3 is separated from the lower end and enters the temporary storage facility, the water outlet at the upper end of the cyclone sand remover 3 is connected with the inlet at the upper end of the adjusting pool 4 through a pipeline; wherein, the function of the cyclone sand remover is to remove the sand and gravel in the high-suspended substance sewage.

[0162] The adjusting pool 4 is a square or circular pool with a flat bottom, the adjusting pool 4 is provided with a timing stirring device, the outlet at the bottom of the adjusting pool 4 is connected with the bottom inlet of the hydrolysis phase separation tank 5 through a pump and a pipeline; the adjusting pool is used for adjusting the high-suspended substance sewage after removing the sand and gravel and the sludge pumped from the sludge pool to form a homogeneous material.

[0163] The hydrolysis and separation tank 5 is a circular cement pool, which is provided with a timing stirring device, a water outlet at the bottom, a biogas outlet and an upper water outlet at the upper end; the water outlet at the bottom of the hydrolysis and separation tank 5 is connected with the turbid-phase anaerobic sequencing batch digester 6 through a pump and a pipeline, the upper water outlet of the hydrolysis and separation tank 5 is connected with the clear-phase anaerobic sequencing batch digester 7 through a pump and a pipeline, and the biogas outlet of the hydrolysis and separation tank 5 is connected with the biogas heat and electricity utilization equipment 8 through a pipeline; the hydrolysis and separation tank makes the organic matter of the material dissolved, hydrolyzed and small-molecule under anaerobic condition, and the insoluble organic matter is dissolved into soluble organic matter, and the soluble organic matter is further hydrolyzed and small-molecule; no medicament needs to be added in the tank; a heating coil is arranged in the tank, water in the tank is heated in a biogas boiler and then is used to heat the material in the tank through heat exchange, the heat energy produced by the biogas boiler is preferentially supplied to the turbid-phase anaerobic sequencing batch digester, then to the clear-phase anaerobic sequencing batch digester, and then to the hydrolysis and separation tank, so that the suitable fermentation temperature is maintained and the temperature fluctuation is reduced as much as possible; the hydrolysis and separation tank is provided with a water retention time according to material hydrolysis acidification, the time is short, and the dissolution, hydrolysis and small-molecule of the organic matter mainly occur, the insoluble organic matter is decomposed and converted into soluble protein, soluble sugar and fatty acid and the like, the turbid-phase anaerobic sequencing batch digester mainly matches the water retention time of the methanogenesis process, and further degrades the organic matter with a slow decomposition and conversion rate by using a long retention time, which is the main process of converting the organic matter into biogas; the stirring of the hydrolysis and separation tank is to make the material mixed in the tank again, so that the material and microorganisms are fully contacted, and the turbid-phase and clear-phase are separated mainly by gravity sedimentation of the sedimentation timing process, the insoluble organic matter is mainly concentrated in the turbid-phase by gravity sedimentation, and the clear-phase is mainly composed of soluble organic matter; the organic matter in the clear liquid has a fast degradation rate, so that the water retention time can be set to be short, thereby saving the reactor volume and reducing the investment, the insoluble organic matter in the turbid-phase has a slow degradation rate, and needs to match a long water retention time, because of the separation of the clear-phase and turbid-phase, the clear-phase does not need to match the long retention time of the turbid-phase, so that the reactor volume is not wasted;

[0164] The turbid-phase anaerobic sequencing batch digester 6 is an enamel steel tank, which is provided with a timing stirring device, a sludge discharge port at the bottom, and a biogas outlet at the upper end; the sludge discharge port is connected with the sludge dewatering machine 21 through a pump and a pipeline, and the biogas outlet is connected with the biogas heat and electricity utilization equipment 8 through a pipeline;

[0165] The clear-phase anaerobic sequencing batch digester 7 is provided with a sludge discharge port at the bottom, a water outlet at the upper end, and a biogas outlet at the upper end; the sludge discharge port is connected with the inlet of the sludge dewatering machine 21 through a pump and a pipeline, the water outlet is connected with the inlet of the primary coagulation and flocculation tank 9 through a pipeline, and the biogas outlet is connected with the biogas heat and electricity utilization equipment 8 through a pipeline;

[0166] The biogas heat and electricity utilization equipment 8 comprises auxiliary devices such as biogas dehydration and desulfurization and biogas storage. Water vapor in the biogas is condensed and removed through a gravel filter or an empty tank, then enters a wet or dry desulfurization device (both are mature equipment, which can be directly selected according to the processing scale) to remove hydrogen sulfide in the biogas, and then enters a biogas storage cabinet for temporary storage. The biogas storage cabinet is mainly used to buffer and balance the flow of the biogas generation end and the biogas consumption end. According to the on-site heat and electricity demand and the biogas production, a biogas generator, a biogas boiler or other combined heat and power equipment is selected and matched.

[0167] The first-stage coagulation and flocculation tank 9 is a flat-bottomed square tank. The outlet of the tank is provided with an inlet of coagulation and an inlet of flocculation agent. Each agent is prepared in a dosing tank (or a barrel) according to a suitable concentration in advance, and is added according to the required flow under the control of the central control system. The flocculation agent is lime or cationic polyacrylamide. The first-stage coagulation and flocculation tank 9 is provided with a continuous stirring device. The outlet of the first-stage coagulation and flocculation tank 9 is connected to the inlet of the primary sedimentation tank 10 through a channel or a pipeline. The first-stage coagulation and flocculation tank serves to mix the agent and the sewage under stirring, and to form flocculation under the action of the agent, and then to enter the primary sedimentation tank to be separated from the water under the action of gravity.

[0168] The primary sedimentation tank 10 is a flat-bottomed square tank. The outlet of the primary sedimentation tank 10 is connected to the inlet of the short-cut nitrification tank 11 and the inlet of the anammox tank 12 through a channel or a pump and a pipeline. The bottom of the primary sedimentation tank 10 is provided with a sludge outlet, which is connected to the inlet of the sludge tank 22 through a pump and a pipeline. The suspended solids in the sewage form flocculation under the action of the agent, and the flocculation is separated from the water under the action of gravity in the primary sedimentation tank, and then is collected at the bottom of the tank, and then is pumped into the sludge tank.

[0169] The short-cut nitrification tank 11 is a square tank with a conical bottom, and an aeration device is arranged in the tank and assisted by suitable fillers (such as polyurethane, polyethylene or polypropylene fillers) and support devices for guaranteeing the growth and reproduction of microorganisms. The outlet of the short-cut nitrification tank 11 is connected to the inlet of the anammox tank 12 through a channel or a pump and a pipeline, and the bottom sludge discharge port of the short-cut nitrification tank 11 is connected to the inlet of the sludge tank 22 through a pump and a pipeline. The short-cut nitrification tank oxidizes ammonia nitrogen into nitrite nitrogen, and the microorganisms are cultured and enriched from the self-borne microorganisms in the sewage. If it is necessary to speed up the debugging time, the microorganisms can also be purchased externally. The nitrite bacteria include bacteria in the genera of Nitrosomonas, Nitrosococcus, Nitrosospira and Nitrosolobus. The anammox tank 12 is a square tank with a conical bottom, and suitable fillers (such as polyurethane, polyethylene or polypropylene fillers) and support devices are arranged in the anammox tank 12 for guaranteeing the growth and reproduction of microorganisms. The anammox tank 12 is connected to the inlet of the secondary sedimentation tank 13 through a channel or a pump and a pipeline. The short-cut nitrification effluent rich in nitrite nitrogen enters the anammox tank and is mixed with another branch of sewage rich in ammonia nitrogen to perform an anammox reaction. The anammox bacteria take ammonia as an electron donor and nitrite as an electron acceptor to generate nitrogen gas to achieve denitrification. The anammox bacteria do not need to be added externally, but are cultured and enriched by adjusting various parameters on site. If it is necessary to speed up the debugging time, the anammox bacteria can also be purchased externally.

[0170] The secondary sedimentation tank 13 is a square tank with a conical bottom, and the upper end outlet thereof is connected to the inlet of the Fenton reaction tank 14 through a channel or a pump and a pipeline. The bottom of the secondary sedimentation tank 13 is provided with a sludge discharge port, and the sludge discharge port is connected to the bottom inlet of the anammox tank 12 and the inlet of the sludge tank 22 through a channel or a pump and a pipeline. The secondary sedimentation tank collects the microorganisms flowing out of the anammox tank by gravity sedimentation, and the microorganisms are returned to the anammox tank as needed or discharged into the sludge tank. After the gravity sedimentation of the suspended matter and the microorganisms, the suspended matter entering the Fenton reaction tank can be reduced, thereby saving the cost of Fenton reagents.

[0171] The Fenton reaction tank 14 is a square tank with a flat bottom, and the Fenton reaction tank 14 is provided with hydrogen peroxide and ferrous sulfate reagent feeding ports. The reagents used are respectively prepared in a reagent preparation tank (or a barrel) in advance according to a suitable concentration, and are fed at a required flow rate under the control of a central control system. A continuous stirring device is arranged in the Fenton reaction tank. The outlet of the Fenton reaction tank 14 is connected to the inlet of the secondary coagulation and flocculation tank 15 through a channel or a pump and a pipeline.

[0172] The secondary coagulation and flocculation tank 15 is a flat-bottomed square tank. The dosing pipe of the secondary coagulation and flocculation tank 15 adds drugs, including lime, polyaluminum chloride, and anionic polyacrylamide. Each of the drugs is prepared in a drug preparation tank (or barrel) according to a suitable concentration in advance, and is added in a required flow under the control of the central control system. The dosing pipe of the secondary coagulation and flocculation tank 15 is linked to the feed pump of the clear-phase anaerobic sequencing batch digester 7 to start and stop together. The dosing equipment is provided with a flow meter connected to the central control system. The secondary coagulation and flocculation tank is also provided with a mechanical stirring device. The outlet of the secondary coagulation and flocculation tank 15 is connected to the inlet of the final settling tank 16. The secondary coagulation and flocculation tank forms sludge flocs by adding drugs generated by the Fenton reaction, and then the flocs are separated from water by gravity settling in the final settling tank, so that the suspended solid content of the water entering the disinfection tank and the clear water tank meets the design discharge requirements.

[0173] The final settling tank 16 is a conical-bottomed square tank. The bottom of the final settling tank is provided with a sludge pump, which is connected to the sludge tank 22 and can be started and stopped according to the clock setting time. The upper end of the final settling tank 16 is connected to the disinfection tank 17 through a pump and a pipeline.

[0174] The disinfection tank 17 is a flat-bottomed square tank. Its disinfection equipment is directly selected according to the selected disinfection process. The disinfection process can be ultraviolet disinfection, or chlorine dioxide, sodium hypochlorite, and liquid chlorine disinfection. The disinfection tank 17 is linked to the feed pump of the clear-phase anaerobic sequencing batch digester to start and stop together. The outlet of the disinfection tank 17 is connected to the inlet of the clear water tank 18, and the outlet of the clear water tank 18 is connected to the clear water inlet of the water and fertilizer mixing tank 20.

[0175] The biogas slurry aging pond 19 is a conical-bottomed square tank covered with a top membrane. The biogas slurry outlet end of the biogas slurry aging pond 19 is connected to the biogas slurry inlet of the water and fertilizer mixing tank 20. The biogas slurry aging pond further degrades the residual organic matter in the biogas slurry, and further makes inorganic nutrients such as nitrogen, phosphorus, and potassium and organic nutrients such as humic acid enter a stable state. The biogas slurry obtained by the water and fertilizer mixing tank 20 can be used for biogas slurry field application or water and fertilizer integration (D).

[0176] The front end of the sludge dewatering machine 21 is also provided with a sludge buffer tank, which is provided with high and low liquid level meters. The high liquid level meter controls the start and stop of the discharge pumps of the turbid-phase anaerobic sequencing batch digester 6, the discharge pumps of the clear-phase anaerobic sequencing batch digester 7 and the sludge discharge pump of the biogas slurry aging pond 19. The low liquid level meter controls the start and stop of the sludge dewatering machine feed pump. When the sludge dewatering machine fails, the sludge can bypass the sludge dewatering machine and enter the biogas slurry aging pond 19 from the sludge buffer tank of the sludge dewatering machine 21. The sludge dewatering machine is preferably a stacked screw machine, a centrifuge or a belt dewatering machine. The sludge dewatering machine is provided with a dosing barrel and a dosing device. The equipment is provided with a dosing control program. The operator only needs to select the type of dewatering agent according to the site conditions, optimize the concentration and flow rate of the agent. The dewatering agent selected for sludge dewatering is polyacrylamide. However, there are many manufacturers of polyacrylamide, and the effective ingredients also differ, and the prices are different, so the dosage and dosage flow rate need to be selected. At present, there are also other types of dewatering agents that can be selected. The sludge produced by the sludge dewatering machine 21 is treated and disposed of (C).

[0177] The water and fertilizer mixing tank 20 is a stainless steel tank. The inlet is also provided with a flow meter and a flow control valve connected to the central control system, which can control the mixing ratio of biogas slurry and water as needed.

[0178] The sludge tank 22 can be a conical bottom square tank. The sludge tank discharge pump can be started and stopped according to the clock setting time.

[0179] The flow meters, liquid level meters, stirring devices, dosing devices, pump sets and valves of all equipment are connected to the central control system, and the pump sets, valves, stirring and dosing are started or stopped according to the clock setting; the conditioning tank is provided with high and low liquid level meters. The high liquid level meter controls the start and stop of the sand discharge pump. The low liquid level meter controls the start and stop of the phase separation hydrolysis tank feed pump. The inlets of the conditioning tank, the phase separation hydrolysis tank, the turbid-phase anaerobic sequencing batch digester, the clear-phase anaerobic sequencing batch digester, the dosing equipment, the short-cut nitrification tank, the anaerobic ammonia oxidation tank and the water and fertilizer mixing tank are all provided with flow meters connected to the central control system. The central control system controls the flow of each device. The short-cut nitrification tank is provided with a dissolved oxygen monitoring device connected to the central control system to assist in frequency control of the aeration air volume. The operation status, operation data statistics and operation parameter setting of all equipment are operated through the central control system on the computer and mobile phone.

[0180] Manual operation and automatic operation can be achieved by connecting to the central control system. The stirring speed of all mechanical stirring devices can be set. The flow rate of hydraulic stirring devices can be set. The operation status, operation data statistics and operation parameter setting of all equipment can be performed on the computer and mobile phone. The statistics of sewage treatment capacity, power consumption, agent consumption of each process section and ton of water treatment cost, as well as online monitoring data such as pH, ammonia nitrogen and COD form daily, monthly and annual reports for real-time updating.

[0181] The method for using the system comprises the following steps:

[0182] The high-suspended substance sewage such as high-suspended substance sewage (A) from the pig house is discharged to the grating machine 1 for removing slag and impurities, and the grating machine 1 is used to remove the impurities such as pig hair, ear tags, gloves and plastic bottles mixed in the high-suspended substance sewage.

[0183] The high-suspended substance sewage after the impurities are removed by the grating flows into the grit chamber 2, the flow rate of the grit chamber 2 is 0.15-0.30 m / s, the residence time is 1-5 h, the effective water depth is 1.5-3.0 m, and the width of each grid is 0.6-3 m.

[0184] The high-suspended substance sewage at the bottom of the grit chamber 2 is pumped into the cyclone sand remover 3 to remove sand and gravel, the water inlet pressure of the cyclone sand remover 3 is 0.2-0.5 MPa, the high-suspended substance sewage after the sand and gravel are removed is pumped into the adjusting tank 4, and the sand and gravel discharged from the lower end of the cyclone sand remover 3 can be utilized or disposed (B).

[0185] The high-suspended substance sewage in the adjusting tank 4 is stirred to form homogeneous material, the residence time of the adjusting tank is 1.0-2.0 d, and the stirring speed is 50-150 rpm to ensure the homogeneity of the material, the continuous stirring mode is adopted, or the adjusting tank is started and operated 30 min before the feed pump of the hydrolysis and separation tank 5 is started, and the stirring device of the adjusting tank 4 is stopped after the feed pump of the hydrolysis and separation tank 5 is stopped.

[0186] The hydraulic residence time of the hydrolysis and separation tank 5 is 3-5 d, the temperature range is 20-25 ℃ when the hydrolysis and separation tank 5 is operated at normal temperature, the temperature range is 30-37 ℃ when the hydrolysis and separation tank 5 is operated at medium temperature, and the temperature range is 50-55 ℃ when the hydrolysis and separation tank 5 is operated at high temperature. The hydrolysis and separation tank 5 is operated in the time sequence of “feeding-reaction-settling-discharging”, the feeding is performed by the feed pump, the discharging is performed by the feed pumps of the turbid-phase anaerobic sequencing batch reactor 6 and the clear-phase anaerobic sequencing batch reactor 7, the feeding and discharging of the hydrolysis and separation tank 5 are performed simultaneously, the feed pumps of the turbid-phase anaerobic sequencing batch reactor 6 and the clear-phase anaerobic sequencing batch reactor 7 are started and stopped in linkage with the feed pump of the hydrolysis and separation tank 5, the flow rates of the two pumps are determined in combination with the residence time of the corresponding digestion tank and the turbid-phase / clear-phase separation ratio, and the sum of the flow rates of the two pumps should be consistent with the flow rate of the feed pump of the hydrolysis and separation tank. The feeding time of the hydrolysis and separation tank 5 is 16-22 h, the reaction time is 1.0-6.0 h, and the settling time is 0.5-2.0 h. The stirring device of the hydrolysis and separation tank 5 is only operated in the reaction time sequence, the stirring is started after the feeding is completed, and the stirring is stopped after the reaction time is completed. The continuous stirring mode or the intermittent stirring mode can be adopted, the stirring is performed for 0.5-1.0 h and then stopped for 10-30 min when the intermittent stirring mode is adopted.

[0187] The hydraulic retention time of the turbid-phase anaerobic sequencing tank 6 is 10-12 days, the temperature range is 20-25°C when operated at normal temperature, 30-37°C when operated at medium temperature, and 50-55°C when operated at high temperature. The "feeding-reaction-settling-discharging" time sequence of the turbid-phase anaerobic sequencing tank 6 is consistent with that of the hydrolysis tank 5, the feeding is completed by the turbid-phase anaerobic sequencing tank 6 feeding pump, and the discharging mode is overflow. The feeding time of the turbid-phase anaerobic sequencing tank 6 is 16-22 hours, the reaction time is 1.0-6.0 hours, and the settling time is 0.5-2.0 hours. The stirring device of the turbid-phase anaerobic sequencing tank 6 only operates in the reaction time sequence section, the stirring is started after the feeding is completed, and the stirring is stopped at the end of the reaction time. The stirring can be continuous or intermittent, and when intermittent stirring is used, the stirring is 0.5-1.0 hours and the stopping is 10-30 minutes. The bottom sludge pump of the turbid-phase anaerobic sequencing tank 6 is discharged according to the actual operating conditions and the mineralization degree of anaerobic sludge, and the bottom sludge is discharged once every 1-7 days, and the discharge amount is 0.1-1.0 times the daily water inflow.

[0188] The hydraulic retention time of the turbid-phase anaerobic sequencing tank 6 is 10-12 days, the temperature range is 20-25°C when operated at normal temperature, 30-37°C when operated at medium temperature, and 50-55°C when operated at high temperature. The "feeding-reaction-settling-discharging" time sequence of the turbid-phase anaerobic sequencing tank 6 is consistent with that of the hydrolysis tank 5, the feeding is completed by the turbid-phase anaerobic sequencing tank 6 feeding pump, and the discharging mode is overflow. The feeding time of the turbid-phase anaerobic sequencing tank 6 is 16-22 hours, the reaction time is 1.0-6.0 hours, and the settling time is 0.5-2.0 hours. The stirring device of the turbid-phase anaerobic sequencing tank 6 only operates in the reaction time sequence section, the stirring is started after the feeding is completed, and the stirring is stopped at the end of the reaction time. The stirring can be continuous or intermittent, and when intermittent stirring is used, the stirring is 0.5-1.0 hours and the stopping is 10-30 minutes. The bottom sludge pump of the turbid-phase anaerobic sequencing tank 6 is discharged according to the actual operating conditions and the mineralization degree of anaerobic sludge, and the bottom sludge is discharged once every 1-7 days, and the discharge amount is 0.1-1.0 times the daily water inflow.

[0189] The biogas heat and electricity utilization equipment 8 reduces the water content of the biogas to below 1% and the hydrogen sulfide content to less than 100 ppm through an attached biogas dehydration equipment, buffers the biogas through a biogas storage tank and balances the pressure of the gas production end and the gas consumption end, the volume of the biogas storage tank is 0.2-0.5 times of the daily biogas production. The biogas generator or the biogas boiler is determined according to the daily biogas production, the sewage treatment system preferentially uses the electricity generated by the biogas generator, automatically switches to the mains power supply when the electricity generation of the biogas generator is insufficient, and realizes the uninterrupted operation of the electrical equipment through the uninterruptible power supply; the heat energy produced by the biogas boiler is preferentially supplied to the turbid-phase anaerobic sequencing tank, then to the clear-phase anaerobic sequencing tank, and then to the hydrolysis separation tank, so as to maintain the suitable fermentation temperature and reduce the temperature fluctuation as much as possible, the daily change of the fermentation temperature of the digestion tank is not more than 1℃; when the biogas production speed and the consumption speed are instantaneously unmatched, the biogas is fully burned through the biogas burner and then discharged.

[0190] The dosing equipment of the primary coagulation and flocculation tank 9 is linked to the feed pump of the clear-phase anaerobic sequencing tank and is started and stopped together, the medicament is lime or cationic polyacrylamide, or other suitable medicaments, the mass-volume concentration of lime is 0.5%-1%, the dosing ratio is 3%-15% of the dry matter of the flocculation object, the dosing concentration of cationic polyacrylamide is 0.1%-0.2%, the dosing ratio is 0.3%-0.5% of the dry matter of the flocculation object, the type, dosing concentration, dosing flow and dosing ratio of the medicament should be determined through field tests to determine the most suitable dosage form and dosage.

[0191] The hydraulic retention time of the primary sedimentation tank 10 is 8-16h, and the effective water depth is 2.0-4.0m.

[0192] The hydraulic retention time of the short-cut nitrification tank 11 is 1.5-3.5d, the pH is controlled in the range of 7.0-8.5, the dissolved oxygen is controlled in the range of 0.5-1.0mg / L through frequency control of the aeration device, and the water temperature is preferably 20-30℃.

[0193] The concentration ratio of ammonia nitrogen to nitrite nitrogen of the influent of the anaerobic ammonia oxidation tank 12 is controlled to be 1:1.0-1.2 by adjusting the inflow of the primary sedimentation effluent and the short-cut nitrification tank effluent, the hydraulic retention time is 0.5-2.0d, the pH is controlled in the range of 7.0-8.0, and the water temperature is preferably 20-30℃. The filler of the anaerobic ammonia oxidation tank 12 should be a porous filler, and fixed filler or suspended filler can be selected, and the material is polyurethane, polyethylene or polypropylene, etc.

[0194] The hydraulic retention time of the secondary sedimentation tank 13 is 4-16h, and the effective water depth is 2.0-4.0m.

[0195] The dosing equipment of the Fenton reaction tank 14 is linked to the feed pump of the clear-phase anaerobic sequencing tank to start and stop, the suspended solids content in the water of the Fenton reaction tank is less than 200 mg / L, the pH is controlled at 3-5, the hydraulic retention time is 2.0-8.0 h, and the dosing amount and ratio of the reagents in the Fenton oxidation reaction should be determined through tests. In the absence of test data, the mass ratio of hydrogen peroxide to chemical oxygen demand is 1-2:1, and the molar ratio of hydrogen peroxide to ferrous sulfate is 1-10:1.

[0196] The dosing equipment of the secondary coagulation and flocculation tank 15 is linked to the feed pump of the clear-phase anaerobic sequencing tank to start and stop, the pH is adjusted to 5.5-8.5 by adding lime, the dosing concentration of lime is 0.5%-1%, the coagulant is polyaluminum chloride, and the dosing amount is preferably 100-200 mg / L. The coagulant aid is preferably anionic polyacrylamide, and the dosing amount is 15-35 mg / L. The type, dosing concentration, dosing flow rate, and dosing ratio of the reagents should be determined through field tests to determine the most suitable dosage form and dosage.

[0197] The hydraulic retention time of the final settling tank 16 is 4-16 h, and the effective water depth is 2.0-4.0 m.

[0198] When the disinfection tank 17 uses ultraviolet disinfection, a clear-channel ultraviolet disinfection system is used, the cleaning method is online mechanical plus chemical cleaning, the effective dose of ultraviolet disinfection is preferably 15-25 mJ / cm according to test data or similar operation experience, the channel length before and after the lamp is not less than 1 m to ensure uniform irradiation of the channel water flow. When using chlorine dioxide, sodium hypochlorite, and liquid chlorine for disinfection, the chlorine dosage should be determined according to test data or similar operation experience. When there is no test data, 5-15 mg / L can be used. After chlorine dioxide, sodium hypochlorite, or chlorine disinfection, mixing and contact should be performed, and the contact time should not be less than 30 min. Sodium hypochlorite solution should be stored at low temperature and away from light, and the storage time should not be more than 7 d.

[0199] The hydraulic retention time of the clear water tank 18 is 4-16 h, and the effective water depth is 2.0-4.0 m.

[0200] The hydraulic retention time of the biogas slurry aging pond 19 is 3-6 months, the sediment is discharged once every 7-30 days, the discharge amount is 0.1-1.0 times the daily water inflow, and the biogas is transported to the auxiliary biogas storage device of the biogas heat and power utilization equipment through a pipeline equipped with a one-way valve and a flame arrester.

[0201] The hydraulic retention time of the water and fertilizer mixing tank 20 is 1-3 h, and the mixing ratio of biogas slurry and clear water is controlled as needed through flow control valves according to planting arrangements and crop fertilizer and water requirements. The biogas slurry flow rate accounts for 0-100% of the water and fertilizer mixing tank outflow rate.

[0202] The sludge dewatering machine 21 is provided with a sludge buffer tank in front, the hydraulic retention time is 12-24h, the sludge buffer tank is equipped with high and low liquid level meters, the high liquid level meter controls the start and stop of the turbid-phase anaerobic sequencing batch digester discharge pump, the clear-phase anaerobic sequencing batch digester discharge pump and the biogas slurry aging pond sludge discharge pump, and the low liquid level meter controls the start and stop of the sludge dewatering machine feed pump. When the sludge dewatering machine fails, the sludge can be transferred from the sludge buffer tank to the biogas slurry aging pond through the sludge dewatering machine. The sludge dewatering machine is preferably a stacked screw machine, a centrifuge or a belt dewatering machine, which is determined according to the daily treatment, the dewatering agent is cationic polyacrylamide or other suitable agent, the cationic polyacrylamide has a concentration of 0.1%-0.2%, and the dosage ratio is 0.3%-0.5% of the dry matter of the flocculation object. The type, concentration, dosage and dosage ratio of the agent should be determined through field tests to determine the most suitable dosage form and dosage.

[0203] The sludge tank 22 has a hydraulic retention time of 5-12h, and the effective water depth is 2.0-4.0m.

[0204] The present application provides a kind of high suspended solids wastewater hydrolysis phase separation anaerobic sequencing batch digestion and water fertilizer integrated system, which combines gravity sedimentation and cyclone sand removal to efficiently separate organic and inorganic solids, separate sand and gravel from high-suspended solids wastewater, reduce the wear and risk of clogging of subsequent pipes, pumps, valves and tank bodies, improve the volumetric efficiency of fermentation tank, and reduce equipment maintenance costs; The system dissolves, hydrolyzes and migrates the solid organic matter under controlled anaerobic conditions through the hydrolysis phase separation tank, and realizes the turbid and clear phase separation of the solid organic matter and soluble organic matter in the high-suspended solids wastewater through the sedimentation process, so as to better match different anaerobic digestion forms according to the characteristics of different materials;

[0205] The turbid-phase anaerobic sequencing batch digester is controlled by time sequence control of "feeding-reaction-sedimentation-discharge", which traps solid organic matter with slow degradation speed and reduces the loss of anaerobic microorganisms, so that the solid retention time and microbial retention time are several times the hydraulic retention time, thereby greatly reducing the design volume of the digester to save equipment investment;

[0206] The clear-phase anaerobic sequencing batch digester is controlled by time sequence control of "feeding-reaction-sedimentation-discharge", which effectively traps microorganisms and undegraded insoluble organic matter, can adapt to a wide range of suspended solids concentration changes and water fluctuations, reduces the investment of three-phase separator and other equipment while ensuring efficient decomposition and conversion of organic matter.

[0207] The biochemical treatment process of the system uses short-cut nitrification and anaerobic ammonia oxidation reaction to reduce the yield of biochemical sludge, and all sludge is introduced into the turbid-phase anaerobic sequencing batch digester for anaerobic decomposition and conversion, thereby reducing the amount of sludge produced and the amount of dewatering agent used in the overall process system, reducing the overall operating cost while also enriching the microbial population structure of the anaerobic digester;

[0208] After the sludge of each unit is mixed and then subjected to anaerobic degradation, it is beneficial to form highly homogenized sludge to facilitate efficient flocculation in the dewatering process, thereby further saving the cost of reagent consumption in the dewatering process.

[0209] The water and fertilizer mixing tank of the system can mix biogas slurry and clean water in any ratio, so as to flexibly carry out biogas slurry field return, water and fertilizer integration and clean water irrigation and other planting and breeding integration operations according to the fertilizer and water requirement of crops.

[0210] Comparative Example 1

[0211] One of the currently commonly used planting and breeding combination implementation modes is "grid impurity removal + continuous stirring type anaerobic reactor (CSTR) biogas fermentation + digestion discharge dewatering + biogas slurry storage + biogas slurry field return"; the existing project under this mode has a high suspended solid sewage, and the inlet and outlet modes of the biogas fermentation tank are solid-liquid mixing inlet and solid-liquid mixing outlet, so that after the original soluble organic matter in the high suspended solid sewage is rapidly degraded, a large amount of low organic matter concentration liquid still exists in the tank, causing volume invalid occupation, wasting equipment investment, and the slow degradation rate of insoluble organic matter in the high suspended solid sewage being unable to be decomposed and converted in time and being discharged from the fermentation tank with the discharge process; if the design hydraulic retention time of the fermentation tank matches the degradation rate of the soluble organic matter, the insoluble organic matter degradation rate is too low, the harmless and stable degree of the high suspended solid sewage is not enough, and the sludge yield is large; if the design hydraulic retention time of the fermentation tank matches the degradation rate of the insoluble organic matter, the volume of the fermentation tank is large, and the equipment investment is high; in addition, the biogas slurry rich in nutrients can only be used as fertilizer, and cannot be used when the crops only need water but not fertilizer, limiting the use of water resources in the biogas slurry.

[0212] The hydrolysis phase separation, turbid phase anaerobic sequencing batch digestion and clear phase anaerobic sequencing batch digestion adopted by the present application can make the high suspended solid sewage occur organic matter dissolution and occurrence phase separation in the hydrolysis phase separation tank, and then adopt suitable biogas fermentation processes for the turbid phase and clear liquid respectively, and then through the settlement process to strengthen the interception of insoluble organic matter and microorganisms, and through the stirring in the reaction process to form sufficient contact between the microorganisms and the organic matter, so as to save the equipment investment, reduce the anaerobic sludge yield, improve the harmless and stable degree of the high suspended solid sewage, and better realize the mineralization of nitrogen and phosphorus nutrients and the formation of organic nutrients such as humic acid; in addition, the biogas slurry rich in high concentration nutrients generated by the turbid phase anaerobic sequencing batch digestion tank is used as fertilizer, the effluent of the clear phase anaerobic sequencing batch digestion tank is used as water resources after denitrification and phosphorus removal, and the nutrient concentration can be regulated through the water and fertilizer mixing tank, so that the operation flexibility of the planting and breeding combination process in adapting to the nutrient and water requirement is improved.

[0213] Comparative Example 2

[0214] One of the current commonly used sewage standard treatment methods is "grating impurity removal + solid-liquid separation + UASB biogas fermentation + nitrification and denitrification + Fenton oxidation"; the existing projects under this method rarely consider the impact of inorganic substances such as sand on the system. When the sand content in high-suspended solids wastewater is high and not removed, it will cause equipment and facility blockage and wear, resulting in increased maintenance costs. Due to the large amount of dry manure produced by solid-liquid separation, the solid residue of the high-suspended solids wastewater treatment system is large, and the organic matter contained in the dry manure does not enter the biogas fermentation process, resulting in insufficient biogas production, and even unable to meet the heating needs of biogas fermentation itself. The UASB reactor cannot well adapt to the large suspended solids content and fluctuations of high-suspended solids wastewater, and cannot achieve efficient biogas fermentation performance. The anaerobic effluent needs to consume a large amount of coagulation and flocculation reagents to remove excess suspended solids before entering the nitrification and denitrification unit. The existing project denitrification is full nitrification and denitrification (ammonia nitrogen → nitrite nitrogen → nitrate nitrogen → nitrite nitrogen → nitrogen gas), the nitration and nitrification process of this process needs to consume a large amount of aeration energy consumption, the two steps of denitrification need to consume organic matter as carbon source, thus conflicting with the process of converting biogas organic matter into biogas, each step of full nitrification and denitrification will produce more activated sludge, and then need to invest more dewatering reagent cost; if the biogas fermentation and nitrification and denitrification process is not enough for the degradation of COD in wastewater, more Fenton reagent needs to be consumed to ensure that the effluent COD meets the standard; the sludge properties of primary sedimentation tank, short-cut nitrification tank, secondary sedimentation tank and final sedimentation tank are not uniform, if mixed in the sludge tank for direct dewatering, flocculation is difficult, reagent consumption is high and cannot well guarantee the stability of the moisture content of dewatered sludge.

[0215] The present application combines gravity settling and cyclone sand to remove inorganic substances such as sand from high-suspended matter sewage, improves the stability of equipment operation, reduces the volume waste and maintenance cost; the present application retains dry manure and feed particles in high-suspended matter sewage to promote the dissolution and hydrolysis of organic matter in the hydrolysis phase separation tank, and the occurrence phase separation of soluble / insoluble organic matter, and more insoluble organic matter is decomposed and converted into biogas, so as to better meet the heating demand of the high-suspended matter sewage treatment system and reduce the volume of solid residues of the high-suspended matter sewage treatment system; the present application combines the anaerobic sequencing batch digestion of the clear phase to intercept insoluble organic matter and microorganisms, so that a longer solid residence time and a longer microorganism residence time can be realized under a lower hydraulic residence time, so that better organic matter decomposition and conversion and coagulation and flocculation agent saving can be realized; the short-cut nitrification and anaerobic ammonia oxidation adopted by the present application only needs to remove most of the suspended matter in the effluent of the clear phase anaerobic sequencing batch digestion tank, and about 55% of the effluent is subjected to aeration oxidation, and only needs to be oxidized to nitrite nitrogen, and then mixed with about 45% of the sewage containing ammonia nitrogen, and under the action of anaerobic ammonia oxidation bacteria, ammonia nitrogen is used as an electron donor, and nitrite nitrogen is used as an electron acceptor, nitrogen gas is generated to realize denitrification, and compared with full nitrification and denitrification, the short-cut nitrification and anaerobic ammonia oxidation can save about 60% of the aeration energy consumption, save 100% of the carbon source, avoid the conflict with biogas fermentation, and reduce the sludge yield by more than 85% in the denitrification process, so as to reduce the sludge yield and dewatering agent cost of the high-suspended matter sewage treatment system; the sludge in the primary sedimentation tank, the short-cut nitrification tank, the secondary sedimentation tank and the final sedimentation tank is preliminarily mixed in the sludge tank, and then is transported to the conditioning tank, mixed with the high-suspended matter sewage, and then enters the hydrolysis phase separation tank to dissolve and hydrolyze part of the organic matter, and the undissolved part enters the turbid phase anaerobic sequencing batch digestion tank for further degradation, which can realize the degradation and reduction of sludge suspended solids, and can make the sludge produced in the whole high-suspended matter sewage treatment system have uniform properties, so as to reduce the flocculation difficulty, save the agent cost, ensure the stability of the moisture content of the dewatered sludge.

[0216] Finally, it should be pointed out that: the above embodiments are only used to illustrate the technical solutions of the present application, and not to limit them; although the present application has been described in detail with reference to the above examples, those skilled in the art should understand that: the technical solutions recorded in the above examples can still be modified, or part or all of the technical features can be replaced by equivalents; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A high suspended solids wastewater treatment process characterized by, The method comprises the following steps: 1) hydrolytic separation treatment of the feed sewage to obtain turbid-phase sewage and clear-phase sewage; The hydrolytic separation treatment adopts a hydrolytic separation tank, and is used for organic matter dissolution, hydrolysis and small molecule in an anaerobic state, and natural sedimentation of suspended solids in a sedimentation timing stage, to form the clear-phase sewage with low suspended solid content in the upper part of the hydrolytic separation tank, and the turbid-phase sewage with high suspended solid content in the lower part of the hydrolytic separation tank; 2) anaerobic sequencing batch digestion treatment of the turbid-phase sewage to obtain turbid-phase sludge, turbid-phase biogas slurry and turbid-phase biogas; anaerobic sequencing batch digestion treatment of the clear-phase sewage to obtain clear-phase sludge, clear-phase biogas and clear-phase anaerobic sequencing batch digestion effluent; The hydraulic retention time of the turbid-phase anaerobic sequencing batch digestion treatment is 10-12 days, and the hydraulic retention time of the clear-phase anaerobic sequencing batch digestion treatment is 2-4 days; 3) primary coagulation and flocculation treatment and primary sedimentation treatment of the clear-phase anaerobic sequencing batch digestion effluent in sequence to obtain primary sedimentation sludge; 4) short-cut nitrification treatment and anaerobic ammonia oxidation treatment of the clear-phase anaerobic sequencing batch digestion effluent in sequence to obtain short-cut nitrification sludge and anaerobic ammonia oxidation effluent; 5) secondary sedimentation treatment and Fenton treatment of the anaerobic ammonia oxidation effluent in sequence to obtain secondary sedimentation sludge and Fenton effluent; 6) secondary coagulation and flocculation treatment, final sedimentation treatment and disinfection treatment of the Fenton effluent in sequence to obtain final sedimentation sludge and disinfection effluent.

2. The method of claim 1, wherein, The method further comprises hydrolytic separation treatment of the short-cut nitrification sludge, the primary sedimentation sludge, the secondary sedimentation sludge and the final sedimentation sludge.

3. The method according to claim 1 or 2, characterized in that, The method further comprises sludge dewatering treatment of the turbid-phase sludge and the clear-phase sludge to obtain dewatered sludge and dewatered biogas slurry, and aging treatment of the dewatered biogas slurry to obtain aged biogas slurry; and / or, The method further comprises biogas slurry aging treatment of the turbid-phase biogas slurry to obtain aged biogas slurry.

4. A high suspended sewage treatment system for performing the method of any one of claims 1-3, characterized by The method comprises a hydrolytic separation tank, a turbid-phase anaerobic sequencing batch digestion tank, a clear-phase anaerobic sequencing batch digestion tank, a primary coagulation and flocculation tank, a primary sedimentation tank, a short-cut nitrification tank, an anaerobic ammonia oxidation tank, a secondary sedimentation tank, a Fenton reaction tank, a secondary coagulation and flocculation tank, a final sedimentation tank, a disinfection tank and a clear water tank; The turbid-phase sewage outlet of the hydrolytic separation tank is in communication with the turbid-phase sewage inlet of the turbid-phase anaerobic sequencing batch digestion tank; The clear-phase sewage outlet of the hydrolytic separation tank is in communication with the clear-phase sewage inlet of the clear-phase anaerobic sequencing batch digestion tank; The material flow inlet of the primary coagulation and flocculation tank is in communication with the supernatant outlet of the clear-phase anaerobic sequencing batch digestion tank; The material flow outlet of the primary coagulation and flocculation tank is in communication with the material flow inlet of the primary sedimentation tank; The supernatant outlet of the primary sedimentation tank is in communication with the material flow inlet of the short-cut nitrification tank; The supernatant outlet of the short-cut nitrification tank is in communication with the material flow inlet of the anaerobic ammonia oxidation tank; The supernatant outlet of the anaerobic ammonia oxidation tank is in communication with the material flow inlet of the secondary sedimentation tank; The supernatant outlet of the secondary sedimentation tank is in communication with the material flow inlet of the Fenton reaction tank; The stream outlet of the Fenton reaction tank is communicated with the stream inlet of the secondary coagulation and flocculation tank; The stream outlet of the secondary coagulation and flocculation tank is communicated with the stream inlet of the final sedimentation tank; The supernatant outlet of the final sedimentation tank is communicated with the stream inlet of the disinfection tank; The stream outlet of the disinfection tank is communicated with the stream inlet of the clear water tank.

5. The system of claim 4, wherein, Further comprising a grating machine, a grit chamber, a cyclone sand remover, a regulating tank, a biogas heat and power utilization device, a biogas slurry aging pond, a water and fertilizer mixing tank, a sludge dewatering machine, and a sludge tank; The grating machine, the grit chamber, the cyclone sand remover, and the regulating tank are sequentially communicated, and the stream outlet of the regulating tank is communicated with the stream inlet of the hydrolysis and phase separation tank; The biogas inlets of the biogas heat and power utilization device are respectively communicated with the biogas outlets of the hydrolysis and phase separation tank, the turbid-phase anaerobic sequencing batch reactor, and the clear-phase anaerobic sequencing batch reactor; The sludge inlets of the sludge tank are respectively communicated with the sludge outlets of the short-cut nitrification tank, the primary sedimentation tank, the secondary sedimentation tank, and the final sedimentation tank; The sludge outlet of the sludge tank is communicated with the sludge inlet of the regulating tank; The sludge outlet of the turbid-phase anaerobic sequencing batch reactor is communicated with the sludge inlet of the sludge dewatering machine; The biogas slurry inlets of the biogas slurry aging pond are respectively communicated with the biogas slurry outlets of the sludge dewatering machine and the turbid-phase anaerobic sequencing batch reactor; The aging biogas slurry outlet of the biogas slurry aging pond and the clear water outlet of the clear water tank are respectively communicated with the water and fertilizer mixing tank; The sludge outlet of the anaerobic ammonia oxidation tank is communicated with the sludge outlet of the secondary sedimentation tank; The sludge outlet of the biogas slurry aging pond is communicated with the sludge inlet of the sludge dewatering machine.

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