CN107540082B - Wastewater dephosphorization reaction device - Google Patents
Wastewater dephosphorization reaction device Download PDFInfo
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- CN107540082B CN107540082B CN201610464951.3A CN201610464951A CN107540082B CN 107540082 B CN107540082 B CN 107540082B CN 201610464951 A CN201610464951 A CN 201610464951A CN 107540082 B CN107540082 B CN 107540082B
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- aeration
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 128
- 239000002351 wastewater Substances 0.000 title claims abstract description 81
- 238000005273 aeration Methods 0.000 claims abstract description 75
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 67
- 238000007872 degassing Methods 0.000 claims abstract description 63
- 239000010802 sludge Substances 0.000 claims abstract description 47
- 238000001556 precipitation Methods 0.000 claims abstract description 30
- 239000007789 gas Substances 0.000 claims abstract description 13
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 9
- 238000004062 sedimentation Methods 0.000 claims description 21
- 230000001376 precipitating effect Effects 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 6
- 238000009826 distribution Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 abstract description 14
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 8
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 38
- 238000000034 method Methods 0.000 description 34
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 28
- 229910052567 struvite Inorganic materials 0.000 description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 22
- 230000008569 process Effects 0.000 description 20
- 229910052698 phosphorus Inorganic materials 0.000 description 19
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 18
- 239000011574 phosphorus Substances 0.000 description 18
- 238000004065 wastewater treatment Methods 0.000 description 18
- 229910052757 nitrogen Inorganic materials 0.000 description 13
- 239000001913 cellulose Substances 0.000 description 11
- 229920002678 cellulose Polymers 0.000 description 11
- 239000003337 fertilizer Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 229910019142 PO4 Inorganic materials 0.000 description 4
- 229920002472 Starch Polymers 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 239000011777 magnesium Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 239000002957 persistent organic pollutant Substances 0.000 description 4
- 239000010452 phosphate Substances 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 239000008107 starch Substances 0.000 description 4
- 235000019698 starch Nutrition 0.000 description 4
- 240000003183 Manihot esculenta Species 0.000 description 3
- 235000016735 Manihot esculenta subsp esculenta Nutrition 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 240000008042 Zea mays Species 0.000 description 3
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 3
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 3
- 235000005822 corn Nutrition 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 238000012851 eutrophication Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 239000010902 straw Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229920005610 lignin Polymers 0.000 description 2
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- 239000002245 particle Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
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- 239000000126 substance Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 229910017958 MgNH Inorganic materials 0.000 description 1
- 241000192710 Microcystis aeruginosa Species 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 239000002686 phosphate fertilizer Substances 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- AAKBLFQBZDFKMP-UHFFFAOYSA-H trimagnesium azane diphosphate Chemical compound N.[Mg+2].[Mg+2].[Mg+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O AAKBLFQBZDFKMP-UHFFFAOYSA-H 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Removal Of Specific Substances (AREA)
- Physical Water Treatments (AREA)
Abstract
The application discloses a wastewater dephosphorization reaction device, which comprises: the dephosphorization reaction tank body is internally provided with a dephosphorization reaction chamber, and the dephosphorization reaction chamber is provided with a water inlet and a dephosphorization agent adding port; the aeration device is arranged in the dephosphorization reaction chamber; and the degassing and precipitation separator is arranged in the dephosphorization reaction chamber and is positioned above the aeration device and is used for separating gas, water and sludge. The wastewater dephosphorization reaction device provided by the embodiment of the application has the advantages of simple structure, low cost, good COD treatment effect, and the like, and can remove part of ammonia nitrogen at the same time.
Description
Technical Field
The application relates to the technical field of environmental protection, in particular to a wastewater dephosphorization reaction device.
Background
The traditional ethanol manufacturing process method generally adopts corn and cassava (namely starch) to prepare ethanol through fermentation and the like, the COD (organic pollutants) of the wastewater is generally between 2 thousands and 3 thousands, and the treatment is easy. However, the production process of the ethanol is forbidden due to the high cost of corn and cassava and limited raw materials.
For this reason, a process for producing ethanol from straw and stalk (cellulose) is proposed in the related art, and for straw and stalk, the cellulose in the stalk is coated with external lignin, so that the lignin in the outer layer needs to be blasted by high temperature and high pressure or sulfuric acid to expose the cellulose in the stalk, and saccharification is performed to produce ethanol, the COD of the wastewater is usually between 5 ten thousand and 9 ten thousand, the treatment is relatively difficult, the structure of the wastewater treatment equipment is complex, the cost is high, the COD treatment effect is poor, and improvement is required.
Disclosure of Invention
The present application aims to solve at least one of the above-mentioned technical problems in the related art to some extent. Therefore, the application provides the wastewater dephosphorization reaction device which has the advantages of simple structure, low cost, good COD treatment effect, and the like, and can remove part of ammonia nitrogen at the same time.
To achieve the above object, according to an embodiment of the present application, there is provided a wastewater dephosphorization reaction apparatus including: the dephosphorization reaction tank body is internally provided with a dephosphorization reaction chamber, and the dephosphorization reaction chamber is provided with a water inlet and a dephosphorization agent adding port; the aeration device is arranged in the dephosphorization reaction chamber; and the degassing and precipitation separator is arranged in the dephosphorization reaction chamber and is positioned above the aeration device and is used for separating gas, water and sludge.
The wastewater dephosphorization reaction device provided by the embodiment of the application has the advantages of simple structure, low cost, good COD treatment effect, and the like, and can remove part of ammonia nitrogen at the same time.
In addition, the wastewater dephosphorization reaction device according to the embodiment of the application can also have the following additional technical characteristics:
according to one embodiment of the application, the aeration device has a plurality of aeration heads or aeration tubes arranged at intervals.
According to one embodiment of the present application, the wastewater dephosphorization reaction apparatus further comprises: the upper end and the lower end of each guide cylinder are open, and a plurality of aeration heads or aeration pipes extend into a plurality of guide cylinders from the lower ends of the guide cylinders respectively.
According to one embodiment of the present application, the wastewater dephosphorization reaction apparatus further comprises: the water distributor is arranged in the dephosphorization reaction chamber and positioned below the aeration device, and the water distributor is connected with the water inlet.
According to one embodiment of the application, the water distributor is provided with a plurality of water distribution openings which are arranged at intervals and are downward in opening.
According to one embodiment of the application, the dephosphorization reaction chamber is provided with a discharge hole positioned at the lower part of the dephosphorization reaction tank body.
According to one embodiment of the present application, the wastewater dephosphorization reaction apparatus further comprises: the cyclone is provided with a cyclone inlet, a mud outlet and a cyclone outlet, wherein the cyclone inlet is communicated with the discharge port, and the cyclone outlet is connected with the dephosphorization reaction chamber through a water return pipe.
According to one embodiment of the present application, the wastewater dephosphorization reaction apparatus further comprises: the device comprises a pump and a desliming device connected with the pump, wherein clear liquid after sludge is removed by the desliming device is returned to the dephosphorization reaction chamber.
According to one embodiment of the present application, the wastewater dephosphorization reaction apparatus further comprises: and the clear liquid after being precipitated by the precipitation device is returned to the dephosphorization reaction chamber.
According to one embodiment of the application, the degassing precipitation separator comprises: the separator body is internally provided with a degassing and precipitating chamber, the bottom of the degassing and precipitating chamber is provided with a sludge discharge port, and the cross-sectional area of the lower part of the degassing and precipitating chamber is gradually reduced along the direction from top to bottom; the baffle plate is arranged at the upper part of the degassing and precipitating chamber, the baffle plate divides the upper part of the degassing and precipitating chamber into a degassing cavity and a precipitating cavity, and the bottom of the degassing cavity is communicated with the bottom of the precipitating cavity so that wastewater overflows from the dephosphorization reaction chamber into the degassing cavity and flows into the precipitating cavity from the bottom of the degassing cavity; the inclined sedimentation plate or the inclined sedimentation pipe is arranged in the sedimentation cavity; the water outlet overflow weir is arranged in the sedimentation cavity and forms a water outlet overflow groove with a separation outlet.
According to one embodiment of the application, the upper edge of the separator body portion defining the degassing chamber with the baffle is lower than the upper edge of the baffle and the upper edge of the separator body portion defining the sedimentation chamber with the baffle.
According to one embodiment of the application, the separator body is rectangular in cross section.
According to one embodiment of the application, the lower end of the first longitudinal side wall of the lower part of the separator body extends downwards beyond the lower end of the second longitudinal side wall of the lower part of the separator body, and the lower end of the first longitudinal side wall overlaps with the lower end of the second longitudinal side wall in the up-down direction.
According to one embodiment of the present application, the wastewater dephosphorization reaction apparatus further comprises: an aeration pump or an aeration fan which is arranged outside the dephosphorization reaction tank body and connected with the aeration device, and the water inlet is connected with a wastewater control valve.
According to one embodiment of the application, a top cover is arranged at the top of the dephosphorization reaction tank body, and the dephosphorization agent adding port is arranged on the top cover.
Drawings
Fig. 1 is a schematic structural view of a wastewater dephosphorization reaction apparatus according to an embodiment of the present application.
Fig. 2 is a schematic diagram of a structure of a degassing and precipitation separator of a wastewater dephosphorization reaction apparatus according to an embodiment of the present application.
Reference numerals:
a wastewater dephosphorization reaction device 20,
A dephosphorization reaction tank 1100, a dephosphorization reaction chamber 1110, a water inlet 1111, a dephosphorization agent adding port 1112, a discharge port 1113, a wastewater control valve 1114, a top cover 1115, a discharge valve 1116,
Aeration device 1200, aeration head or aeration pipe 1210,
The degassing and settling separator 1300, the separator body 1310, the degassing and settling chamber 1311, the degassing chamber 1312, the settling chamber 1313, the sludge discharge port 1314, the first longitudinal side wall 1315, the second longitudinal side wall 1316, the baffle 1320, the inclined settling plate or pipe 1330, the effluent weir 1340, the effluent overflow launder 1341, the separation outlet 1342,
A guide cylinder 1400,
Water distributor 1500, water distribution port 1510,
Cyclone 1600, cyclone inlet 1610, mud outlet 1620, cyclone outlet 1630, return tube 1640,
An aeration pump or fan 1700.
Detailed Description
Embodiments of the present application are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative and intended to explain the present application and should not be construed as limiting the application.
Along with the prohibition of the process method for preparing the ethanol by adopting corn and cassava (namely starch), the process method for preparing the ethanol by taking straw and stalk (cellulose) as raw materials is increasingly widely applied, but compared with the traditional process for preparing the ethanol by adopting starch by using cellulose, the COD in the wastewater is increased from 2 thousands to 3 thousands to 5 thousands to 9 thousands, and the difficulty of wastewater treatment is correspondingly increased.
The inventor of the application discovers through researches and experiments that the waste water treatment system for preparing ethanol from cellulose in the related technology has limited COD treatment effect, can not treat COD in waste water to below 100mg/L, has complicated procedures, complex system constitution and higher cost.
For example, in a conventional wastewater treatment system for producing ethanol from cellulose, a high-load aeration process and a dephosphorization process are usually provided, and the high-load aeration process and the dephosphorization process are separately performed, and separate facilities are required for the high-load aeration process and the dephosphorization process, respectively, which results in complicated processes, complicated system configuration, and high cost.
In addition, with the development of industrial and agricultural production and the improvement of the living standard of people, the discharge amount of nitrogen and phosphorus pollutants is dramatically increased. The eutrophication of water body caused by nitrogen and phosphorus pollution is serious, and the water bloom and the offshore red tide of the lake occur more and more violently. The eutrophication of water body endangers many industries such as agriculture, fishery, travel industry and the like, and also forms a great threat to drinking water sanitation and food safety. The economic and effective control of nitrogen and phosphorus pollution has become a major environmental protection problem to be solved urgently. Struvite has a molecular formula of MgNH4PO4 & 6H2O, is a white crystal which is difficult to dissolve in water, and has a solubility product of 2.5X10-13 in water at normal temperature. By adding chemical reagent, ammonia and phosphate in the wastewater can form struvite, so that nitrogen and phosphorus pollutants can be removed simultaneously. In addition, the struvite contains two nutrient elements of nitrogen and phosphorus, and is a good slow release fertilizer.
The struvite has very low solubility in water and alkali, and the method for forming struvite is used for removing ammonia nitrogen and phosphate in wastewater, so that the method has the characteristics of high efficiency, simplicity and convenience. Such as starch industrial wastewater, livestock and poultry raising wastewater, landfill leachate and the like, contain high-concentration ammonia nitrogen, are difficult to directly carry out biological treatment, and are usually treated by a physical and chemical method (such as a stripping method) in advance. The stripping method requires pH to be more than 10, has low efficiency (not more than 50 percent) and is easy to cause secondary pollution. If the guanite precipitation method is used for treatment, the requirement on the pH condition can be reduced compared with the stripping method, and the efficiency is higher. According to the experiment of Tu nay et al on leather-making waste water, under the condition of pH value of 8-9, adopting struvite dephosphorization method can make the NH4+ removing rate be up to above 75%. Li et al adopts a struvite precipitation method, the concentration of the initial ammonia nitrogen is reduced to 210mg/l within 15 minutes, and the removal rate is over 96 percent. While the pH is controlled to be between 8.5 and 9. In the experiment of Chimenos et al on dye wastewater with initial concentration of NH4 < + > -N of 2320mg/l, the removal rate of NH4 < + > -N is also over 90 percent.
Phosphorus serves on the one hand as a key factor causing eutrophication and on the other hand is a very valuable mineral resource. The world has ascertained that the phosphorus reserves are only enough for human use for 100 years. Since struvite can be directly used as fertilizer, it is considered as one of the most promising phosphorus recovery paths, and the second international academy of phosphorus recovery conference is also an special topic for this purpose, and research on phosphorus recovery from sewage is being conducted. The supernatant of the anaerobic digestion sludge contains high concentration of NH4+ -N and PO 43-P, and is suitable for treatment by a struvite precipitation method. As long as a small amount of Mg2+ is added, the solubility product of various ions in the wastewater can reach a supersaturated state, and struvite precipitation is formed. And because of the lower SS, the produced struvite has higher purity. Mg (OH) 2 and NaOH are added into the sludge digestion liquid in a molar ratio of 1:1 to increase the pH, so that struvite is precipitated in a fluidized bed in the form of small particles. The phosphorus recovery device can realize 90% of soluble phosphate recovery at present, and ensure that biological phosphorus removal runs up to standard. In actual wastewater treatment, struvite precipitation has various limiting factors. First, many wastewater streams have high concentrations of nitrogen and phosphorus, but the ratio of these to each other does not meet the requirements of struvite precipitation. In this case, the addition of certain ions may increase the precipitation efficiency, but may increase the processing cost. And nitrogen and phosphorus are control targets of wastewater treatment, and secondary pollution can be caused by excessive addition. The addition of excess mg2+ is necessary for struvite precipitation, and therefore, inexpensive additives are critical to the practical application of struvite precipitation. Mg (OH) 2 is a relatively desirable Mg2+ additive, which increases both the Mg2+ content and the pH. Mg (OH) 2 slurries have been used in practical production.
In actual wastewater treatment, the wastewater often contains organic pollutants besides nitrogen and phosphorus pollutants, and if the pollutants are not removed, part of the organic pollutants can be entrained in struvite after the struvite process is adopted, so that the purity and the value of the struvite are reduced, and secondary pollution is caused.
In summary, it is important to develop a reaction device capable of simultaneously removing organic pollutants, nitrogen and phosphorus in water for practical wastewater. Under the guidance of the thought, the inventor of the application provides a dephosphorization reaction device which is used for simultaneously removing ammonia nitrogen (NH 4 < + >), phosphate (PO 43 < + >) and COD from wastewater, and can also recycle struvite as phosphate fertilizer when treating the wastewater.
Considering the technical condition of wastewater treatment in the related art, especially the technical condition of wastewater treatment of ethanol prepared from cellulose, the application provides a wastewater dephosphorization reaction device with simple structure, low cost and good COD treatment effect.
The wastewater dephosphorization reaction apparatus 20 according to the embodiment of the present application is described below with reference to the accompanying drawings.
As shown in fig. 1 and 2, the wastewater dephosphorization reaction apparatus 20 according to the embodiment of the present application includes a dephosphorization reaction tank 1100, an aeration apparatus 1200, and a degassing and precipitation separator 1300.
The dephosphorization reaction tank 1100 has a dephosphorization reaction chamber 1110, and the dephosphorization reaction chamber 1110 has a water inlet 1111 and a dephosphorization agent adding port 1112. The aeration device 1200 is disposed within the dephosphorization reaction chamber 1110. The degassing and precipitation separator 1300 is provided in the dephosphorization reaction chamber 1110, and the degassing and precipitation separator 1300 is positioned above the aeration device 1200, and the degassing and precipitation separator 1300 is used for separating gas, water and sludge.
The operation of the wastewater dephosphorization reaction apparatus 20 according to the embodiment of the present application will be described with reference to the accompanying drawings.
Wastewater (for example, wastewater after anaerobic fermentation purification) enters a dephosphorization reaction chamber 1110 from a water inlet 1111, a dephosphorization oxidant (for example, magnesium oxide) is added into the dephosphorization reaction chamber 1110 through a dephosphorization agent adding port 1112, oxygen is supplied to the dephosphorization reaction chamber 1110 by an aeration device 1200, an aerobic environment is formed in the dephosphorization reaction chamber 1110, meanwhile, air supplied by the aeration device 1200 plays a role of stirring the wastewater, thereby the wastewater in the dephosphorization reaction chamber 1110 is rapidly mixed with aerobic sludge and the dephosphorization oxidant, biochemical organic matters in a colloid state of solubility in the wastewater are removed and dephosphorization is carried out, the reacted wastewater overflows into a degassing and precipitation separator 1300, thereby gas, water and aerobic sludge are separated, the separated gas is discharged from the top of the dephosphorization reaction chamber 1110, then the water is separated from the aerobic sludge, the separated aerobic sludge returns to the dephosphorization reaction chamber 1300 for recycling, and the water after the separation overflows out of the degassing and precipitation separator 1300, and the dephosphorization reaction chamber is discharged, and the wastewater is conveyed to a subsequent treatment process.
According to the wastewater dephosphorization reaction device 20 of the embodiment of the application, the dephosphorization reaction tank body 1100 is provided with the dephosphorization agent adding port 1112, and the dephosphorization reaction chamber 1110 is internally provided with the aeration device 1200, so that aeration and dephosphorization functions are integrated, and equipment required by a high-load aeration process and a dephosphorization process in the cellulose ethanol wastewater treatment system can be replaced, thereby simplifying the structure of the cellulose ethanol wastewater treatment system, reducing the cost of the cellulose ethanol wastewater treatment system and having good COD treatment effect. The cellulose-made ethanol wastewater treatment system employing the wastewater dephosphorization reaction apparatus 20 according to the embodiment of the present application can treat COD in wastewater to 100 or less. Therefore, the wastewater dephosphorization reaction device 20 according to the embodiment of the application has the advantages of simple structure, low cost, good COD treatment effect and the like.
The wastewater dephosphorization reaction apparatus 20 according to the embodiment of the present application is described below with reference to the accompanying drawings.
As shown in fig. 1 and 2, the wastewater dephosphorization reaction apparatus 20 according to the embodiment of the present application includes a dephosphorization reaction tank 1100, an aeration apparatus 1200, and a degassing and precipitation separator 1300.
Further, as shown in fig. 1, the wastewater dephosphorization reaction apparatus 20 further includes an aeration pump or fan 1700, and the aeration pump or fan 1700 is provided outside the dephosphorization reaction tank 1100 and connected to the aeration apparatus 1200 to pump air to the aeration apparatus 1200. In some embodiments, aeration device 1200 is blast aeration and includes an aeration air pipe and an aeration pan or aeration tube mounted at the end of the aeration air pipe, the aeration pump or aeration blower 1700 delivering air through the aeration air pipe to the aeration pan or aeration tube, the aeration pan or aeration tube aerating the air into the dephosphorization reaction chamber 1110.
Alternatively, the aeration device 1200 may be a jet aeration device, in which case an aeration pump or an aeration fan 1700 provided outside the dephosphorization reaction tank 1100 is not required, and the jet aeration device sucks air into the dephosphorization reaction chamber 1110 using a jet hydraulic impact type air diffusion device, for example, a jet ejector provided in the dephosphorization reaction chamber 1110 is combined with a jet pump provided outside the dephosphorization reaction tank 1100.
Advantageously, as shown in fig. 1, a wastewater control valve 1114, which is located outside the dephosphorization reaction tank 1100, is connected to the water inlet 1111 to control whether wastewater is supplied to the dephosphorization reaction chamber 1110 and the amount of wastewater supplied to the dephosphorization reaction chamber 1110.
As shown in fig. 1, in order to facilitate the smooth feeding of the dephosphorizing oxidizing agent into the dephosphorizing reaction chamber 1110 and to prevent other impurities from entering the dephosphorizing reaction chamber 1110, and to achieve the effect of reducing the heating energy consumption, a top cover 1115 is provided on the top of the dephosphorizing reaction tank 1100, and a dephosphorizing agent feeding port 1112 is provided on the top cover 1115.
In some embodiments of the present application, as shown in fig. 1, the aeration device 1200 has a plurality of aeration heads or aeration pipes 1210, the plurality of aeration heads or aeration pipes 1210 are disposed at intervals in the dephosphorization reaction chamber 1110, and the aeration device 1200 uniformly aerates the dephosphorization reaction chamber 1110 through the plurality of aeration heads or aeration pipes 1210, thereby improving the uniform effect of oxygen supply and the uniform stirring effect of wastewater and aerobic sludge.
Further, as shown in fig. 1, the wastewater dephosphorization reaction apparatus 20 further comprises a plurality of guide cylinders 1400, the number of the guide cylinders 1400 corresponds to the number of aeration heads or aeration tubes 1210, the upper end and the lower end of each guide cylinder 1400 are open, and the plurality of aeration heads or aeration tubes 1210 extend into the plurality of guide cylinders 1400 from the lower ends of the plurality of guide cylinders 1400, respectively. Therefore, the plurality of guide cylinders 1400 can be utilized to play a role in guiding, so that the wastewater in the dephosphorization reaction chamber 1110 can be fully contacted with aerobic sludge, the aerobic sludge is in a suspension state, the contact degree of the wastewater and the aerobic sludge is improved, and the wastewater treatment efficiency is improved.
By combining with the design of a guide cylinder, mg (OH) 2 emulsion is added under the optimal reaction condition to generate magnesium ammonia phosphate (MgNH 4PO4.6H2O, commonly known as struvite) crystal. Under such circumstances, a portion of the COD may also be removed by dissolved oxygen in the wastewater, forming new biomass and carbon dioxide.
Optionally, as shown in fig. 1, the wastewater dephosphorization reaction device 20 further includes a water distributor 1500, the water distributor 1500 is disposed in the dephosphorization reaction chamber 1110 and is located below the aeration device 1200, the water distributor 1500 is connected to the water inlet 1111, and the water distributor 1500 has a plurality of water distribution ports 1510 that are spaced apart and open downward. Wastewater enters the water distributor 1500 from the water inlet 1111 and is uniformly dispersed into the dephosphorization reaction chamber 1110 from the plurality of water distribution ports 1510 of the water distributor 1500.
In some specific examples of the present application, as shown in fig. 1, the wastewater dephosphorization reaction apparatus 20 further comprises a cyclone 1600, the dephosphorization reaction chamber 1110 has a discharge outlet 1113 located at the lower part of the dephosphorization reaction tank 1100, the cyclone 1600 has a cyclone inlet 1610, a sludge outlet 1620 and a cyclone outlet 1630, the cyclone inlet 1610 is communicated with the discharge outlet 1113, a discharge valve 1116 is connected between the cyclone inlet 1610 and the discharge outlet 1113, and the cyclone outlet 1630 is connected with the dephosphorization reaction chamber 1110 through a water return pipe 1640.
The liquid-solid mixture deposited at the bottom of the dephosphorization reaction chamber 1110 can enter the cyclone 1600 through the discharge hole 1113, the discharge valve 1116 and the cyclone inlet 1610 in sequence and be separated in the cyclone 1600, the separated water returns to the dephosphorization reaction chamber 1110 through the cyclone outlet 1630 and the water return pipe 1640 in sequence, and the separated solid (such as magnesium ammonium phosphate) is conveyed to the struvite pool through the mud outlet 1620 and can be used as fertilizer.
The cyclone is combined with the design of the cyclone to separate struvite crystals from activated sludge and water so as to improve the purity of struvite and apply the struvite as fertilizer.
Compared with the traditional dephosphorization device, the dephosphorization reaction device provided by the embodiment of the application has lower cost compared with a ferric salt adding device, one set of dephosphorization reaction device has multiple purposes (ammonia nitrogen and COD removal), and the produced struvite does not cause secondary pollution, and also slowly releases high-quality fertilizers of N, P and Mg. Struvite particles are separated from the apparatus by means of cyclones, the quality of which meets for example the fertilizer related standards of the european union.
In some embodiments of the present application, the wastewater dephosphorization reaction apparatus 20 further comprises a pump and a desliming apparatus connected to the pump, wherein the clear liquid after sludge removal of the desliming apparatus is returned to the dephosphorization reaction chamber 1110, thereby improving the utilization rate of the wastewater.
Alternatively, the desliming device may be replaced by a precipitation device, i.e., the wastewater dephosphorization reaction device 20 further comprises a pump and a precipitation device connected to the pump, wherein the supernatant after precipitation by the precipitation device is returned to the dephosphorization reaction chamber 1110.
In some specific examples of the application, as shown in fig. 1 and 2. The degassing and settling separator 1300 includes a separator body 1310, a baffle 1320, an inclined settling plate or pipe 1330, and an effluent weir 1340.
A degassing settling chamber 1311 is formed in the separator body 1310, and a sludge discharge port 1314 is formed at the bottom of the degassing settling chamber 1311, and the cross-sectional area of the lower portion of the degassing settling chamber 1311 is gradually reduced in a direction from top to bottom. A baffle 1320 is provided at an upper portion of the degassing settling chamber 1311, the baffle 1320 dividing the upper portion of the degassing settling chamber 1311 into a degassing chamber 1312 and a settling chamber 1313, a bottom of the degassing chamber 1312 communicating with a bottom of the settling chamber 1313 so that wastewater overflows from the dephosphorization reaction chamber 1110 into the degassing chamber 1312 and flows from the bottom of the degassing chamber 1312 into the settling chamber 1313. An inclined settling plate or tube 1330 is provided within the settling chamber 1313. An effluent weir 1340 is provided within the settling chamber 1313 and the effluent weir 1340 forms an effluent overflow trough 1341 having a separation outlet 1342.
The separation process of the deaeration and precipitation separator 1300 for water, gas and aerobic sludge is described below with reference to fig. 1 and 2.
The water degraded by the aerobic sludge is entrained with gas and aerobic sludge, the water with the entrained gas and the aerobic sludge overflows to a degassing cavity 1312 of a degassing and precipitating chamber 1311, wherein the gas escapes from the degassing cavity 1312 and is discharged from the top of a dephosphorization reaction chamber 1110, and gas separation is completed. The water with the aerobic sludge after being separated from the gas flows to a sedimentation chamber 1313 from the bottom of the degassing chamber 1312, at this time, the aerobic sludge is sedimented and is guided by the inclined inner wall at the lower part of the degassing sedimentation chamber 1311 to a sludge discharge port 1314, the sludge is discharged from the sludge discharge port 1314 to the degassing sedimentation separator 1300 to enter the dephosphorization reaction chamber 1110 for further wastewater degradation, and the water separated from the aerobic sludge in the degassing sedimentation chamber 1311 overflows into a water outlet overflow groove 1341 of a water outlet overflow weir 1340 and is discharged to the outside of the dephosphorization reaction chamber 1110 from a separation outlet 1342 for subsequent treatment. In the process of rising the aerobic sludge and water, the aerobic sludge is settled on an inclined sedimentation plate or an inclined sedimentation pipe 1330 and falls to the bottom of a degassing sedimentation chamber 1311, which is helpful for separating the aerobic sludge from the water, and thus, the separation of the water, the aerobic sludge and the gas is completed.
Advantageously, as shown in fig. 2, the upper edge of the separator body 1310 that defines the degassing cavity 1312 with the baffle 1320 is lower than the upper edge of the baffle 1320 and the upper edge of the portion of the separator body 1310 that defines the sedimentation cavity 1313 with the baffle 1320. In other words, the upper edge of the portion of the separator body 1310 that defines the degassing chamber 1312 is lower than the upper edge of the portion of the separator body 1310 that defines the settling chamber 1313 and lower than the upper edge of the baffle 1320. The upper edge of the effluent weir 1340 may be flush with or higher than the upper edge of the portion of the separator body 1310 defining the degassing cavity 1312 and the upper edge of the effluent weir 1340 is lower than the upper edge of the portion of the separator body 1310 defining the sedimentation cavity 1313 and the upper edge of the baffle 1320. Therefore, water in the degassing cavity 1312 can be prevented from overflowing to the sedimentation cavity 1313 from the upper side, the water in the degassing cavity 1312 is guaranteed to flow to the sedimentation cavity 1313 from the bottom of the degassing cavity 1312, aerobic sludge is further fully separated, and water in the sedimentation cavity 1313 overflows into the effluent overflow groove 1341, so that the entrainment of the aerobic sludge in the water in the effluent overflow groove 1341 is avoided.
Alternatively, as shown in fig. 2, the separator body 1310 has a rectangular cross section, such as a rectangular parallelepiped shape, a lower end of the first longitudinal side wall 1315 of the lower portion of the separator body 1310 extends downward beyond a lower end of the second longitudinal side wall 1316 of the lower portion of the separator body 1310, and the lower end of the first longitudinal side wall 1315 overlaps with the lower end of the second longitudinal side wall 1316 in the up-down direction. Whereby the aerobic sludge in the dephosphorization reaction chamber 1110 is advantageously prevented from entering the degassing and settling chamber 1311 of the degassing and settling separator 1300 through the sludge discharge port 1314.
For example, among the four longitudinal side walls of the separator body 1310, two longitudinal side walls having a longer length in the horizontal direction are the first longitudinal side wall 1315 and the second longitudinal side wall 1316, respectively, the lower end of the first longitudinal side wall 1315 and the lower end of the second longitudinal side wall 1316 are adjacent to each other with respect to the upper end of the first longitudinal side wall 1315 and the upper end of the second longitudinal side wall 1316, the lower end of the first longitudinal side wall 1315 is located below the lower end of the second longitudinal side wall 1316, and projections of the lower end of the first longitudinal side wall 1315 and the lower end of the second longitudinal side wall 1316 in the horizontal plane overlap, and a gap between the lower end of the first longitudinal side wall 1315 and the lower end of the second longitudinal side wall 1316 constitutes a sewage sludge discharge port 1314, whereby on the one hand, it can be ensured that the aerobic sludge in the degassing and precipitating chamber 1311 can smoothly return to the dephosphorization reaction chamber 1110 through the sludge discharge port 1314, and on the other hand the structure of the sludge discharge port 1314 can block the aerobic sludge in the dephosphorization reaction chamber 1110 from entering the sludge discharge port 1314 into the aerobic precipitation chamber 1311, ensuring the aerobic sludge separation effect of the degassing separator 1300.
According to the wastewater dephosphorization reaction device 20 provided by the embodiment of the application, the aeration and dephosphorization functions are integrated, namely, the aeration process and the dephosphorization process can be completed in the wastewater dephosphorization reaction device 20 at the same time, so that equipment required by each of the high-load aeration process and the dephosphorization process in the cellulose-made ethanol wastewater treatment system can be replaced, the structure of the cellulose-made ethanol wastewater treatment system is simplified, the cost of the cellulose-made ethanol wastewater treatment system is reduced, and the cellulose-made ethanol wastewater treatment system adopting the wastewater dephosphorization reaction device 20 provided by the embodiment of the application can treat COD (chemical oxygen demand) in wastewater to below 100 mg/L. In addition, according to the wastewater dephosphorization reaction device and the dephosphorization process using the same, not only the COD treatment effect is good, but also the nitrogen and phosphorus removal effect is good, for example, nitrogen can reach below 15mg/L and phosphorus can reach below 0.5 mg/L.
In the description of the present application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present application and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present application.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present application, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present application, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present application, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present application. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Further, one skilled in the art can engage and combine the different embodiments or examples described in this specification.
While embodiments of the present application have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the application, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the application.
Claims (5)
1. A wastewater dephosphorization reaction device, characterized by comprising:
the dephosphorization reaction tank body is internally provided with a dephosphorization reaction chamber, and the dephosphorization reaction chamber is provided with a water inlet and a dephosphorization agent adding port;
the dephosphorization reaction chamber is provided with a discharge port positioned at the lower part of the dephosphorization reaction tank body;
the aeration device is arranged in the dephosphorization reaction chamber;
the aeration device is provided with a plurality of aeration heads or aeration pipes which are arranged at intervals, the upper end and the lower end of each guide cylinder are open, and the plurality of aeration heads or aeration pipes extend into the plurality of guide cylinders from the lower ends of the plurality of guide cylinders respectively;
the cyclone is provided with a cyclone inlet, a mud outlet and a cyclone outlet, the cyclone inlet is communicated with the discharge port, and the cyclone outlet is connected with the dephosphorization reaction chamber through a water return pipe;
the degassing and precipitation separator is arranged in the dephosphorization reaction chamber and is positioned above the aeration device and is used for separating gas, water and sludge;
the degassing precipitation separator includes:
the separator body is internally provided with a degassing and precipitating chamber, the bottom of the degassing and precipitating chamber is provided with a sludge discharge port, and the cross-sectional area of the lower part of the degassing and precipitating chamber is gradually reduced along the direction from top to bottom;
the baffle plate is arranged at the upper part of the degassing and precipitating chamber, the baffle plate divides the upper part of the degassing and precipitating chamber into a degassing cavity and a precipitating cavity, and the bottom of the degassing cavity is communicated with the bottom of the precipitating cavity so that wastewater overflows from the dephosphorization reaction chamber into the degassing cavity and flows into the precipitating cavity from the bottom of the degassing cavity;
the inclined sedimentation plate or the inclined sedimentation pipe is arranged in the sedimentation cavity;
the water outlet overflow weir is arranged in the sedimentation cavity and forms a water outlet overflow groove with a separation outlet.
2. The wastewater dephosphorization reaction apparatus of claim 1, further comprising:
the water distributor is arranged in the dephosphorization reaction chamber and positioned below the aeration device, and the water distributor is connected with the water inlet.
3. The wastewater dephosphorization reaction apparatus of claim 2 wherein the water distributor has a plurality of water distribution openings spaced apart and opening downwardly.
4. The wastewater dephosphorization reaction apparatus of claim 1, further comprising: the device comprises a pump and a desliming device connected with the pump, wherein clear liquid after sludge is removed by the desliming device is returned to the dephosphorization reaction chamber.
5. The wastewater dephosphorization reaction apparatus of claim 1, further comprising: and the clear liquid after being precipitated by the precipitation device is returned to the dephosphorization reaction chamber.
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