CN211734107U - Sewage treatment device for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement - Google Patents
Sewage treatment device for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement Download PDFInfo
- Publication number
- CN211734107U CN211734107U CN201922393875.3U CN201922393875U CN211734107U CN 211734107 U CN211734107 U CN 211734107U CN 201922393875 U CN201922393875 U CN 201922393875U CN 211734107 U CN211734107 U CN 211734107U
- Authority
- CN
- China
- Prior art keywords
- sludge
- sidestream
- sewage treatment
- pond
- carbon
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000010802 sludge Substances 0.000 title claims abstract description 91
- 239000010865 sewage Substances 0.000 title claims abstract description 49
- 230000006872 improvement Effects 0.000 title claims abstract description 18
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 230000009467 reduction Effects 0.000 title claims description 16
- 238000011065 in-situ storage Methods 0.000 title claims description 10
- 239000012528 membrane Substances 0.000 claims abstract description 60
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 54
- 238000001179 sorption measurement Methods 0.000 claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000000126 substance Substances 0.000 claims abstract description 22
- 238000004062 sedimentation Methods 0.000 claims abstract description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 18
- 239000001301 oxygen Substances 0.000 claims abstract description 18
- 206010021143 Hypoxia Diseases 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 16
- 230000008929 regeneration Effects 0.000 claims description 14
- 238000011069 regeneration method Methods 0.000 claims description 14
- 238000010992 reflux Methods 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 6
- 239000013049 sediment Substances 0.000 claims description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 40
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 40
- 239000011574 phosphorus Substances 0.000 abstract description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 36
- 238000000034 method Methods 0.000 abstract description 26
- 229910052799 carbon Inorganic materials 0.000 abstract description 22
- 230000008569 process Effects 0.000 abstract description 22
- 238000001914 filtration Methods 0.000 abstract description 14
- 238000010521 absorption reaction Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 34
- 229910052757 nitrogen Inorganic materials 0.000 description 17
- 239000003795 chemical substances by application Substances 0.000 description 16
- 239000000945 filler Substances 0.000 description 11
- 239000000835 fiber Substances 0.000 description 9
- -1 polypropylene Polymers 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 239000004744 fabric Substances 0.000 description 6
- 230000004907 flux Effects 0.000 description 6
- 229920000728 polyester Polymers 0.000 description 6
- 239000004033 plastic Substances 0.000 description 5
- 238000011049 filling Methods 0.000 description 4
- 239000012510 hollow fiber Substances 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 3
- 239000002033 PVDF binder Substances 0.000 description 3
- 239000004743 Polypropylene Substances 0.000 description 3
- 229920002978 Vinylon Polymers 0.000 description 3
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- URRHWTYOQNLUKY-UHFFFAOYSA-N [AlH3].[P] Chemical compound [AlH3].[P] URRHWTYOQNLUKY-UHFFFAOYSA-N 0.000 description 3
- ZQBZAOZWBKABNC-UHFFFAOYSA-N [P].[Ca] Chemical compound [P].[Ca] ZQBZAOZWBKABNC-UHFFFAOYSA-N 0.000 description 3
- 239000001913 cellulose Substances 0.000 description 3
- 229920002678 cellulose Polymers 0.000 description 3
- 239000004568 cement Substances 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 230000002209 hydrophobic effect Effects 0.000 description 3
- 239000003456 ion exchange resin Substances 0.000 description 3
- 229920003303 ion-exchange polymer Polymers 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 230000000813 microbial effect Effects 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- DPTATFGPDCLUTF-UHFFFAOYSA-N phosphanylidyneiron Chemical compound [Fe]#P DPTATFGPDCLUTF-UHFFFAOYSA-N 0.000 description 3
- 229920002492 poly(sulfone) Polymers 0.000 description 3
- 229920000098 polyolefin Polymers 0.000 description 3
- 229920001155 polypropylene Polymers 0.000 description 3
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- 229920002972 Acrylic fiber Polymers 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 229920004933 Terylene® Polymers 0.000 description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 239000010425 asbestos Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 229920000295 expanded polytetrafluoroethylene Polymers 0.000 description 2
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 2
- 238000005470 impregnation Methods 0.000 description 2
- 239000011133 lead Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 239000005020 polyethylene terephthalate Substances 0.000 description 2
- 229910052895 riebeckite Inorganic materials 0.000 description 2
- 239000005060 rubber Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229910052709 silver Inorganic materials 0.000 description 2
- 239000004332 silver Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- 239000011701 zinc Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 241000244206 Nematoda Species 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 208000034699 Vitreous floaters Diseases 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000009295 crossflow filtration Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- VLTRZXGMWDSKGL-UHFFFAOYSA-M perchlorate Inorganic materials [O-]Cl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-M 0.000 description 1
- VLTRZXGMWDSKGL-UHFFFAOYSA-N perchloric acid Chemical compound OCl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-N 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- KIEOKOFEPABQKJ-UHFFFAOYSA-N sodium dichromate Chemical compound [Na+].[Na+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KIEOKOFEPABQKJ-UHFFFAOYSA-N 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 150000003751 zinc Chemical class 0.000 description 1
Images
Landscapes
- Water Treatment By Sorption (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The utility model relates to a sewage treatment plant of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio, including the raw water pump that connects gradually, the oxygen deficiency pond, built-in good oxygen membrane bioreactor's good oxygen pond, the sidestream reactor, ammonia nitrogen adsorption column, chemical phosphorus removal pond and sedimentation tank, wherein, the mud return line who returns to connect the oxygen deficiency pond has still been arranged to the bottom in good oxygen pond, the delivery port position of sidestream reactor still is equipped with filtering component, this filtering component's delivery port passes through sidestream pond outlet pipe way and connects ammonia nitrogen adsorption column, the sedimentation effluent of sedimentation tank returns the oxygen deficiency pond. Compared with the prior art, the utility model discloses an insert an upflow sidestream reactor behind conventional sewage treatment process to insert ammonia nitrogen absorption and phosphorus removal device at the rear end, get rid of the ammonia nitrogen and the phosphorus of SSR release, during the process water pump that will be rich in the carbon source returns main part reactor, improve the utilization ratio of system carbon source, thereby realize the rational utilization of mud normal position decrement and carbon source.
Description
Technical Field
The utility model belongs to the technical field of sewage sludge treatment, a sewage treatment of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio is related to.
Background
The activated sludge process is currently widely used for removing organic matter and nutrients from wastewater. In order to realize stable water quality reaching the standard, a sewage treatment plant generally carries out upgrading transformation on conventional secondary biological treatment so as to meet the requirements of lower suspended matters, COD (chemical oxygen demand) and nitrogen emission. However, the carbon source shortage problem of the urban sewage treatment plant in China is serious, and the phenomenon of unreasonable utilization and even waste of the carbon source exists in the running process. Meanwhile, a large amount of excess sludge is generated in the sewage treatment process, and the annual output of the sludge in China in 2020 is estimated to reach 6000 million tons. The sludge treatment cost is expensive and accounts for about 25 to 65 percent of the investment and operation cost of the whole sewage treatment plant. Therefore, the realization of the sludge in-situ reduction in the sewage treatment process is the best method for solving the problem of large-amount sludge discharge, the main method is a physical, chemical or biological method, and no matter the reduction is carried out in the physicochemical or biochemical enhanced activated sludge process, if the main flow of the treatment process is directly disturbed, the impact load is probably caused to the original process, and the sludge activity and the effluent quality are influenced. Therefore, currently, a sidestream reactor (SSR) unit is often inserted into the sludge return bypass of the activated sludge process to achieve process reduction of activated sludge.
After the filler is added into the SSR, a large number of microorganisms grow on the filler, the sludge concentration can be increased to 6-7 g/L, the sludge age is increased under the condition that other parameters are not changed, and various biological floras such as bacteria, protozoa, oligotrichines and nematodes in a biological membrane can form a long food chain. Meanwhile, the surface of the filler is beneficial to the growth of microorganisms with long generation period and low proliferation speed, and the sludge yield of the system is reduced. However, the sludge reduction effect of the conventional SSR system is not ideal.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a sewage treatment plant and technology of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio in order to overcome the defect that above-mentioned prior art exists, come to detach ammonia nitrogen and phosphorus in the sewage that comes out from SSR through ammonia nitrogen adsorption column and chemical dephosphorization pond, in pumping the processing water that will be rich in the carbon source back to main part reactor, improve the utilization ratio of system carbon source, thereby realize the rational utilization of mud normal position decrement and carbon source, and then improve mud normal position decrement and sewage treatment effect.
The purpose of the utility model can be realized through the following technical scheme:
the utility model discloses one of the technical scheme provides a sewage treatment plant of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio, include raw water pump, oxygen deficiency pond, built-in good oxygen membrane bioreactor's good oxygen pond, sidestream reactor, ammonia nitrogen adsorption column, chemical dephosphorization pond and the sedimentation tank that connect gradually along the sewage treatment direction, wherein, return connection has still been arranged to good oxygen pond's bottom the mud return line in oxygen deficiency pond, the delivery port position of sidestream reactor still is equipped with filter assembly, and this filter assembly's delivery port passes through sidestream pond outlet pipe and connects ammonia nitrogen adsorption column, the precipitation play water of sedimentation tank returns the oxygen deficiency pond.
Furthermore, the side surface of the lower part of the side flow reactor is also provided with a residual sludge pipeline which is connected with the anoxic tank in a returning way.
Furthermore, the aerobic membrane bioreactor is immersed in the sludge in the aerobic tank, and a built-in membrane module of the aerobic membrane bioreactor is arranged perpendicular to the water inlet direction.
Further, the side flow reactor is an upflow side flow reactor.
Furthermore, the ammonia nitrogen adsorption column is provided with one or a plurality of ammonia nitrogen adsorption columns side by side, and a regeneration liquid tank is also arranged at the inlet of the ammonia nitrogen adsorption column.
Furthermore, the bottom of the aerobic tank is provided with a perforated aeration pipeline and an air pump connected with the aeration pipeline.
The second technical scheme of the utility model provides a sewage treatment process of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio, and it adopts foretell sewage treatment plant to implement, and this sewage treatment process includes following step:
(1) the raw sewage is sent into an anoxic tank for treatment by a raw water pump and then sent into an aerobic tank, the effluent treated by an aerobic membrane bioreactor is taken as the system effluent, the sludge obtained at the bottom end flows back to the anoxic tank, and the obtained sludge mixed liquor is pumped into the bottom of a side flow reactor;
(2) setting the dissolved oxygen level in the side flow reactor to be in an aerobic, micro-aerobic or anaerobic state, and placing a filtering component consisting of filter cloth in the upper area of the side flow reactor, so that the sewage treated in the side flow reactor is filtered by the filtering component, the obtained sewage rich in carbon source, nitrogen and phosphorus is sent to an ammonia nitrogen adsorption column through a side flow water outlet pipeline, and all or part of the residual sludge obtained at the bottom of the side flow reactor flows back to an anoxic tank;
(3) the ammonia nitrogen adsorption column is used for carrying out ammonia nitrogen adsorption treatment on the fed sewage and then feeding the sewage into a chemical phosphorus removal tank for carrying out chemical phosphorus removal treatment;
(4) and (3) the sludge mixed liquor after the reaction in the chemical phosphorus removal tank enters a sedimentation tank again, solid-liquid separation is carried out, the sludge obtained at the bottom is discharged, and the treated carbon-rich water obtained at the upper part is circulated to the anoxic tank.
Further, in the step (1), the dissolved oxygen in the anoxic pond is 0.2-2 mg/L, and the Hydraulic Retention Time (HRT) is 0.5-10 h;
the dissolved oxygen in the aerobic tank is 0.5-8 mg/L, the HRT is 0.5-10 h, and the sludge reflux ratio is 10-500%;
the membrane component used by the aerobic membrane-bioreactor is tubular, plate frame type or hollow fiber type, the material of the membrane component is hydrophobic polyolefin or polyvinylidene fluoride or hydrophilic polysulfone or cellulose, the aperture of the membrane pores in the membrane component is 0.1-1 mu m, and the membrane flux is 3-30L/(m) m2·h)。
Further, in the step (2), the side flow reactor is designed in an up-flow mode, the effluent of the aerobic tank enters from the bottom end of the side flow reactor, the sludge is intercepted by the filler and the baffle after the treatment of the side flow reactor, and the sewage rich in carbon source, nitrogen and phosphorus is sent into the ammonia nitrogen adsorption column after the treatment of the upper end membrane module.
Furthermore, a membrane component (namely a membrane filtration component) in the side flow reactor is of a dynamic membrane structure, the type is a pre-coating membrane or a stock solution forming membrane, a cross flow filtration mode is adopted, and the aperture of a corresponding membrane hole is 0.1-100 mu m.
Furthermore, the dissolved oxygen in the side flow reactor is 0-8 mg/L, and the HRT is 0.5-10 h.
Furthermore, the type of the filler filled in the side flow reactor is at least two of cement, fly ash, rubber, expanded polytetrafluoroethylene, sponge, metal (such as aluminum, zinc, silver, lead and the like), plastic/plastic impregnation, fiber (such as acrylic fiber, terylene, asbestos, plant, ceramic, carbon and the like) or activated carbon, and the filling rate is 1-80%;
furthermore, the filter cloth used by the filtering component (namely the membrane filtering component) in the side flow reactor is selected from at least one of polyester staple fiber, polyester long fiber, vinylon or polypropylene, the corresponding filter hole aperture is 0.1-100 mu m, and the flux is 3-30L/(m2·h)。
Further, in the step (3), the ammonia nitrogen adsorbing material used by the ammonia nitrogen adsorbing column has a particle size of 0.1-10 mm, and is activated carbon, a molecular sieve, ceramsite, zeolite or ion exchange resin.
Further, the agents used for removing phosphorus in the chemical phosphorus removal tank are calcium salt phosphorus removal agents, microbial flocculant phosphorus removal agents, iron salt phosphorus removal agents or aluminum salt phosphorus removal agents, and the adding amount of the agents is 5-1500 mg/g SS.
Furthermore, the HRT of the sedimentation tank is 0.5-10 h.
Compared with the prior art, the utility model has the advantages of it is following:
(1) is suitable for treating sewage with low C/N ratio and high nitrogen load, has low sludge yield and greatly reduces the burden of subsequent treatment.
(2) The sludge in the high sludge concentration in the side flow reactor releases carbon sources, so that a large amount of carbon sources are provided for subsequent nitrogen and phosphorus removal, sludge reduction is realized, and a large amount of operation cost is saved.
(3) The dynamic membrane component (namely the filtering component) has low cost, and the dynamic membrane on the surface of the membrane matrix can be precoated or self-generated after being removed in a high-sludge concentration system, so that the membrane pollution is effectively controlled.
Drawings
Fig. 1 is a schematic structural view of the present invention;
the notation in the figure is:
the system comprises a raw water pump 1, an anoxic tank 2, an aerobic tank 3, a water outlet pump 4, a sludge reflux pump 5, a side flow tank water inlet pump 6, a side flow reactor 7, a dynamic membrane module 8, an excess sludge pump 9, an excess sludge discharge system 10, a side flow tank water outlet pump 11, an ammonia nitrogen adsorption column 12, a chemical phosphorus removal tank 13, a sedimentation tank 14, a treated water reflux pump 15, an excess sludge discharge system II 16 and a regeneration liquid tank 17.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments. The embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
One of the technical schemes of the utility model provides a sewage treatment plant of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio, its structure is seen in figure 1, include raw water pump 1, oxygen deficiency pond 2, built-in aerobic membrane bioreactor's that connect gradually along the sewage treatment direction aerobic tank 3, sidestream reactor 7, ammonia nitrogen adsorption column 12, chemical phosphorus removal pond 13 and sedimentation tank 14, wherein, the return connection has still been arranged to the bottom in aerobic tank 3 the mud return line in oxygen deficiency pond 2, the delivery port position of sidestream reactor 7 still is equipped with filtering component, and this filtering component's delivery port passes through sidestream pond outlet pipe connection ammonia nitrogen adsorption column 12, the sediment effluent of sedimentation tank 14 returns oxygen deficiency pond 2.
In a specific embodiment of the present invention, please refer to fig. 1 again, a stirring assembly is further disposed in the anoxic tank 2, and meanwhile, the bottom of the anoxic tank 2 is communicated with the bottom of the aerobic tank 3.
In a specific embodiment of the present invention, please refer to fig. 1 again, the lower side of the side flow reactor 7 is further provided with a residual sludge pipeline connected back to the anoxic tank 2.
In a specific embodiment of the present invention, please refer to fig. 1 again, the aerobic membrane bioreactor is immersed in the sludge in the aerobic tank 3, and the built-in membrane module is disposed perpendicular to the water inlet direction.
In a specific embodiment of the present invention, the side flow reactor 7 is an upflow side flow reactor 7.
The utility model discloses a specific embodiment, ammonia nitrogen adsorption column 12 be equipped with one or many side by side, and still be provided with regeneration liquid case 17 in ammonia nitrogen adsorption column 12's entrance.
In a specific embodiment of the present invention, please refer to fig. 1 again, the bottom of the aerobic tank 3 is provided with a perforated aeration pipeline and an air pump connected to the aeration pipeline.
In the above embodiments, referring to fig. 1 again, a sludge return pump 5 may be further disposed in the sludge return line, a side-stream pool water inlet pump 6 is further disposed between the aerobic pool 3 and the side-stream pool 7, a part of excess sludge discharged from an excess sludge outlet on the side of the bottom of the side-stream pool 7 is discharged through an excess sludge discharge system 10, another part of excess sludge is returned to the anoxic pool 2 for reuse through an excess sludge pump 9, a treated water return pump 15 is disposed between the sedimentation pool 14 and the anoxic pool 2, and sludge obtained at the bottom of the sedimentation pool 14 is discharged through an excess sludge discharge system two 16.
The second technical scheme of the utility model provides a sewage treatment process of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio, its specific process flow refers to shown in figure 1, and it adopts foretell sewage treatment plant to implement, and this sewage treatment process includes following step:
(1) the raw sewage is sent into an anoxic tank 2 for treatment by a raw water pump 1 and then sent into an aerobic tank 3, the effluent treated by an aerobic membrane bioreactor is taken as the system effluent, the sludge obtained at the bottom end flows back to the anoxic tank 2, and the obtained sludge mixed liquor is pumped into the bottom of a lateral flow reactor 7;
(2) setting the dissolved oxygen level in the side flow reactor 7 to be in an aerobic, micro-aerobic or anaerobic state, placing a filtering component consisting of filter cloth in the upper area of the side flow reactor 7, so that after the sewage treated in the side flow reactor 7 is filtered by the filtering component, the obtained sewage rich in carbon source, nitrogen and phosphorus is sent to an ammonia nitrogen adsorption column 12 through a side flow water outlet pipeline, and all or part of the residual sludge obtained at the bottom position of the side flow reactor 7 flows back to the anoxic tank 2;
(3) the ammonia nitrogen adsorption column 12 carries out ammonia nitrogen adsorption treatment on the fed sewage, and then the sewage is fed into a chemical phosphorus removal tank 13 for chemical phosphorus removal treatment;
(4) and the sludge mixed liquor after the reaction in the chemical phosphorus removal tank 13 enters a sedimentation tank 14 again, solid-liquid separation is carried out, the sludge obtained at the bottom is discharged, and the treated carbon-rich water obtained at the upper part is circulated to the anoxic tank 2.
Further, in the step (1), the dissolved oxygen in the anoxic pond 2 is 0.2-2 mg/L, and the hydraulic retention time is 0.5-10 h;
the dissolved oxygen in the aerobic tank 3 is 0.5-8 mg/L, the HRT is 0.5-10 h, and the sludge reflux ratio is 10-500%;
the membrane component used by the aerobic membrane bioreactor is tubular, plate frame type or hollow fiber type, the material of the membrane component is hydrophobic polyolefin or polyvinylidene fluoride or hydrophilic polysulfone or cellulose, the aperture of the membrane pores in the membrane component is 0.1-1 mu m, and the membrane flux is 3-30L/(m) m2·h)。
In a specific embodiment of the present invention, in step (2), the type of the filler filled in the side flow reactor 7 is at least two of cement, fly ash, rubber, expanded polytetrafluoroethylene, sponge, metal (aluminum, zinc, silver, lead, etc.), plastic/plastic impregnation, fiber (acrylic fiber, terylene, asbestos, plant, ceramic, carbon, etc.), or activated carbon, and the filling rate is 1-80%;
in a specific embodiment of the present invention, the filter cloth used in the filtering component in the side flow reactor 7 is at least one selected from polyester staple fiber, polyester filament, vinylon or polypropylene, the corresponding filter pore diameter is 0.1-100 μm, and the flux is 3-30L/(m)2·h)。
In a specific embodiment of the present invention, in step (3), the particle size of the ammonia nitrogen adsorbing material used in the ammonia nitrogen adsorbing column 12 is 0.1-10 mm, which is activated carbon, molecular sieve, ceramsite, zeolite or ion exchange resin.
In a specific embodiment of the present invention, the agent for removing phosphorus in the chemical phosphorus removal tank 13 is calcium salt phosphorus removal agent, microbial flocculant phosphorus removal agent, iron salt phosphorus removal agent or aluminum salt phosphorus removal agent, and the dosage thereof is 5-1500 mg/g SS.
In a specific embodiment of the present invention, the HRT of the sedimentation tank 14 is 0.5-10 h.
The above embodiments may be implemented individually, or in any combination of two or more.
The above embodiments will be described in more detail with reference to specific examples.
Example 1:
the sewage flows into an anoxic tank 2 with HRT of 2h through a regulating tank to remove a small amount of nitrogen and COD, and enters an aerobic tank 3 with HRT of 8h (a built-in aerobic membrane bioreactor) for nitrification to remove most of ammonia nitrogen and COD. The method comprises the steps that a sludge mixed solution enters from the bottom end of a side flow reactor 7 (namely a side flow tank with various fillers inside), the HRT is 8 hours, the sludge concentration at the bottom end of the side flow reactor is high, a large amount of carbon sources, nitrogen and phosphorus are released, the reduction rate of a system is enhanced by adding ceramic fiber fillers (the filling rate is 75%), an effluent rich in the carbon sources, the nitrogen and the phosphorus is firstly adsorbed for 10 minutes by a dynamic membrane assembly 8 through an ammonia nitrogen adsorption column 12 to remove ammonia nitrogen in the water, the effluent is added with ferric trichloride in a chemical phosphorus removal tank 13 to remove phosphorus and then enters a sedimentation tank 14 for sedimentation, and the sludge discharge period of the sedimentation tank 14 is 3 hours. The treated water contains a large amount of carbon sources and returns to the anoxic tank 2 through the treated water recycling pump 15, so that the C/N ratio of the whole system is improved. Anaerobic reaction and sludge reduction are carried out in the side flow reactor 7. Wherein, the ammonia nitrogen adsorption columns 12 need to be arranged in parallel, the adsorption columns operate for 24 hours, then the regeneration liquid (sodium chloride, about 15 g/L) is pumped into the regeneration liquid tank 17 for regeneration for 4 hours, and the inflow water is switched to another adsorption column for continuous operation. And discharging the regenerated waste liquid to a regenerated liquid tank. After regeneration for a certain number of times, the regeneration liquid can be subjected to calcium removal treatment, and the treated regeneration liquid can be recycled. The flat membrane module (i.e. aerobic membrane bioreactor) in the aerobic tank 3 is cleaned every month and soaked with sodium hypochlorite and citric acid to restore the permeability of the membrane. When a large amount of sludge is adhered to the dynamic membrane module 8, the dynamic membrane on the surface of the membrane substrate is removed and then precoated or self-generated again, so that the membrane pollution is reduced.
The operation is carried out continuously for 120 days according to the process mode. The average concentration of soluble COD, ammonia nitrogen, total nitrogen and total phosphorus in the inlet water is 280.5, 45.6, 65.1 and 10.4 mg/L. After the treatment by the process provided by the embodiment, the pH value of the reactor is 6.5-7.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus in the effluent are 18.2, 0.5, 2.2 and 0.3mg/L respectively. The sludge yield is reduced by 70 percent compared with the same period of the last year.
Comparative example 1:
most of them are the same as in example 1 above, except that the treated sewage of this example is directly returned to the anoxic tank 2 after passing through the side flow reactor 7.
The same procedure as described above for example 1 was followed for 120 consecutive days. The average concentration of soluble COD, ammonia nitrogen, total nitrogen and total phosphorus in the inlet water is 280.5, 45.6, 65.1 and 10.4 mg/L. After the treatment by the process provided by the comparative example, the pH value of the reactor is 6.5-8.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus of effluent are 20.1, 19.5, 35.4 and 7.2mg/L respectively. The sludge yield is reduced by 13.2 percent compared with the same period in the last year.
Example 2
High ammonia nitrogen wastewater which is obtained by intercepting coarse floaters and suspended matters in a certain sewage plant through a grid enters an anoxic tank 2 and an aerobic tank 3 with HRT of 3h and 6.7h respectively through a raw water pump 1 to remove COD and nitrogen. The membrane module (i.e. aerobic membrane bioreactor unit) in the aerobic tank 3 is a hollow fiber membrane, and the membrane module is backwashed every month to recover the permeability of the membrane. Then the sludge mixed liquor flows through a side flow reactor 7 filled with 25 percent of activated carbon and 25 percent of suspended filler, the HRT is 6.7h, and the filter cloth of the dynamic membrane module 8 is coated with fine particle activated carbon. The effluent of the dynamic membrane enters an ammonia nitrogen adsorption column 12 with HRT of 1h to remove most of ammonia nitrogen, and when a single ammonia nitrogen adsorption column continuously operates for 12h and penetrates through the column, the regeneration stage is carried out, and the inlet water is switched to another adsorption column to continuously operate. When the ammonia nitrogen adsorption column 12 is regenerated, the regenerated liquid in the regenerated liquid tank 17 is pumped into the ammonia nitrogen adsorption column 12 to desorb and regenerate the adsorption material, and the desorbed ammonia nitrogen is converted into nitrogen. Wherein the concentration of the composite regeneration liquid is 30g/L, and the regeneration soaking time is 6 h. And then the sewage enters a chemical phosphorus removal tank 13 to be mixed with aluminum chloride, enters a sedimentation tank to be settled for 4 hours, and then is discharged by a sludge discharge system. The sewage after dephosphorization returns to the anoxic tank 2 by a pump. Most ammonia nitrogen released by the sidestream reactor 7 is adsorbed when the ammonia nitrogen adsorption column 12 is used, and phosphorus is removed in the chemical phosphorus removal tank 13, so that a carbon source in the system can be recovered, and the C/N ratio of a main flow system (namely the anoxic tank 2, the aerobic tank 3 and the like) is improved. Finally, the effluent is discharged through a membrane component in the aerobic tank 3.
Through the continuous 7-month operation of the mode, the average concentration of soluble COD, ammonia nitrogen, total nitrogen and total phosphorus in the inlet water is 250.5, 88.5, 100.1 and 8.5 mg/L. After the treatment by the process provided by the embodiment, the pH value of the reactor is 6.5-7.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus in the effluent are 8.8, 3.0, 5.2 and 0.2mg/L respectively. The sludge yield is reduced by 66.5 percent compared with the same period in the last year.
In the above embodiments or examples, the process parameters in the anoxic tank, the aerobic tank, the sidestream reactor, the ammonia nitrogen adsorption column, the chemical phosphorus removal tank and other structural units may be arbitrarily selected from their end values or intermediate values within the following defined ranges as required, and the types of the raw materials may be arbitrarily selected or arbitrarily combined as required:
the dissolved oxygen in the anoxic pond is 0.2-2 mg/L, and the hydraulic retention time is 0.5-10 h; the dissolved oxygen in the aerobic tank is 0.5-8 mg/L, the HRT is 0.5-10 h, and the sludge reflux ratio is 10-500%; the membrane component used by the aerobic membrane bioreactor is tubular, plate frame type or hollow fiber type, the material of the membrane component is hydrophobic polyolefin or polyvinylidene fluoride or hydrophilic polysulfone or cellulose, the aperture of the membrane pores in the membrane component is 0.1-1 mu m, and the membrane flux is 3-30L/(m) m2H); the type of the filler filled in the side flow reactor is at least two of cement, fly ash, sponge, plastic, fiber, suspended filler or activated carbon, and the filling rate is 1-80%; the filter cloth used by the filtering component in the side flow reactor is at least one selected from polyester staple fiber, polyester long fiber, vinylon or polypropylene, the aperture of the corresponding filtering hole is 0.1-100 mu m, and the flux is 3-30L/(m)2H); in the step (3), the ammonia nitrogen adsorbing material used by the ammonia nitrogen adsorbing column has the particle size of 0.1-10 mm, and is active carbon, a molecular sieve, ceramsite, zeolite or ion exchange resin; the chemical agents used for removing phosphorus in the chemical phosphorus removal tank are calcium salt phosphorus removing agents, microbial flocculant phosphorus removing agents, iron salt phosphorus removing agents or aluminum salt phosphorus removing agents, and the adding amount of the chemical phosphorus removal agents is 5-1500 mg/g SS; HRT of the sedimentation tank is 0.5-10 h; the salt in the regeneration liquid can be selected from magnesium salt, sylvite, calcium salt, sodium salt, ferric salt, aluminum salt and zinc salt, the concentration of the salt is 1-85 g/L, and an oxidant can be added, and the salt can be selected from hydrogen peroxide, perchlorate, permanganate, dichromate, sodium peroxide, hypochlorite, ozone and nitric acid.
And the rest of the raw materials or functional components, if not specifically stated, are conventional commercially available raw materials in the field or conventional components or conventional structures for realizing the corresponding functions.
The embodiments described above are intended to facilitate the understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention according to the disclosure of the present invention.
Claims (8)
1. The utility model provides a sewage treatment plant of high sludge concentration mud sidestream normal position decrement and improvement carbon-nitrogen ratio, its characterized in that includes raw water pump, oxygen deficiency pond, built-in aerobic membrane bioreactor's good oxygen pond, sidestream reactor, ammonia nitrogen adsorption column, chemical dephosphorization pond and the sedimentation tank that connect gradually along the sewage treatment direction, wherein, the bottom in good oxygen pond has still been arranged and has been returned the connection the mud return line in oxygen deficiency pond, the delivery port position of sidestream reactor still is equipped with filter assembly, and this filter assembly's delivery port passes through sidestream pond outlet pipe and connects ammonia nitrogen adsorption column, the sediment play water of sedimentation tank returns the oxygen deficiency pond.
2. The sewage treatment plant for the sidestream in-situ reduction and carbon-nitrogen ratio improvement of the sludge with high sludge concentration according to claim 1, wherein a residual sludge pipeline which is connected with the anoxic tank in a return mode is further arranged on the lower side face of the sidestream reactor.
3. The sewage treatment device for the sidestream in-situ reduction and carbon-nitrogen ratio improvement of the sludge with high sludge concentration according to claim 2, wherein an excess sludge pump is further arranged on the excess sludge pipeline.
4. The sewage treatment plant for the sidestream in-situ reduction and carbon-nitrogen ratio improvement of the sludge with high sludge concentration as claimed in claim 1, wherein the aerobic membrane bioreactor is immersed in the sludge in the aerobic tank, and a built-in membrane module is arranged perpendicular to the water inlet direction.
5. The sewage treatment plant for sidestream in-situ reduction and carbon-nitrogen ratio improvement of sludge with high sludge concentration according to claim 1, wherein the sidestream reactor is an up-flow sidestream reactor.
6. The sewage treatment plant for the sidestream in-situ reduction and carbon-nitrogen ratio improvement of sludge with high sludge concentration according to claim 1, wherein the ammonia nitrogen adsorption column is provided with one or a plurality of ammonia nitrogen adsorption columns side by side, and a regeneration liquid tank is further arranged at the inlet of the ammonia nitrogen adsorption column.
7. The sewage treatment plant for the sidestream in-situ reduction and carbon-nitrogen ratio improvement of sludge with high sludge concentration as claimed in claim 1, wherein the bottom of the aerobic tank is provided with a perforated aeration pipeline and an air pump connected with the aeration pipeline.
8. The sewage treatment plant for the sidestream in-situ reduction and carbon-nitrogen ratio improvement of the sludge with high sludge concentration as claimed in claim 1, wherein a sludge reflux pump is further arranged on the sludge reflux pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922393875.3U CN211734107U (en) | 2019-12-27 | 2019-12-27 | Sewage treatment device for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201922393875.3U CN211734107U (en) | 2019-12-27 | 2019-12-27 | Sewage treatment device for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211734107U true CN211734107U (en) | 2020-10-23 |
Family
ID=72871122
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201922393875.3U Active CN211734107U (en) | 2019-12-27 | 2019-12-27 | Sewage treatment device for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211734107U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110963648A (en) * | 2019-12-27 | 2020-04-07 | 上海电力大学 | Sewage treatment device and process for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement |
-
2019
- 2019-12-27 CN CN201922393875.3U patent/CN211734107U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110963648A (en) * | 2019-12-27 | 2020-04-07 | 上海电力大学 | Sewage treatment device and process for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109879426B (en) | Method for deep dephosphorization and denitrification of sewage treatment | |
| US10822261B1 (en) | Carbon removal and denitrification treatment device for leachate from waste incineration plant and method thereof | |
| CN105585218B (en) | Wastewater from mechanical industry treatment process | |
| CN108585385B (en) | MBBR sewage treatment system and treatment process | |
| CN102030449A (en) | Method for treating metallurgical coking wastewater by using microelectrolysis-membrane bioreactor | |
| CN110117134B (en) | Rural domestic sewage treatment process | |
| CN106219884A (en) | The processing method of high ammonia nitrogen landfill leachate | |
| CN1970474A (en) | Garbage leachate processing process and system based on membrane bioreactor-nano filtering membrane technology | |
| CN101423314A (en) | High efficiency denitrification, phosphorus removal and phosphorus resource recovery composite for urban sewage | |
| CN110963648A (en) | Sewage treatment device and process for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement | |
| CN103466902A (en) | High-concentration ammonia nitrogen wastewater treatment method | |
| CN211734107U (en) | Sewage treatment device for high-sludge-concentration sludge side-stream in-situ reduction and carbon-nitrogen ratio improvement | |
| CN200988816Y (en) | Garbage percolating liquid treating system based on film biological reactor-filter film technology | |
| CN105152471A (en) | Combined treatment process for non-biodegradable organic wastewater | |
| CN210683539U (en) | System for be used for retrieving carbon, nitrogen, phosphorus and water in sewage | |
| CN101391833A (en) | Filter tank type membrane bioreactor | |
| CN111115661A (en) | Nitric acid wastewater treatment system and method | |
| CN207671875U (en) | Printing and dyeing wastewater treatment system | |
| CN205974188U (en) | Wastewater treatment system | |
| CN214400149U (en) | Surface quasi-second-class drinking water source water replenishing regeneration treatment system | |
| CN114314850A (en) | Constructed wetland deep purification device and method for high-salt refractory organic wastewater | |
| CN211445406U (en) | Landfill leachate treatment device | |
| CN112250257A (en) | Sewage treatment system, garbage leachate treatment integrated system and sewage treatment method | |
| CN216513360U (en) | Denitrification resin regeneration waste liquid treatment system | |
| Sun et al. | A submerged tubular ceramic membrane bioreactor for high strength wastewater treatment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20230904 Address after: No. 615, Beizhai, Xintang Village, Zhelin Town, Fengxian District, Shanghai, 2014 Patentee after: Fang Leiping Address before: 200090 No. 2103, Pingliang Road, Shanghai, Yangpu District Patentee before: Shanghai University of Electric Power |
|
| TR01 | Transfer of patent right |