CN114380460A - Urine sewage nitrogen and phosphorus recovery and purification treatment device and method - Google Patents
Urine sewage nitrogen and phosphorus recovery and purification treatment device and method Download PDFInfo
- Publication number
- CN114380460A CN114380460A CN202111551813.6A CN202111551813A CN114380460A CN 114380460 A CN114380460 A CN 114380460A CN 202111551813 A CN202111551813 A CN 202111551813A CN 114380460 A CN114380460 A CN 114380460A
- Authority
- CN
- China
- Prior art keywords
- urine
- nitrogen
- tank
- phosphorus
- ammonia
- 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.)
- Pending
Links
- 210000002700 urine Anatomy 0.000 title claims abstract description 154
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 114
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 57
- 238000011084 recovery Methods 0.000 title claims abstract description 57
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 54
- 239000011574 phosphorus Substances 0.000 title claims abstract description 54
- 239000010865 sewage Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000011282 treatment Methods 0.000 title claims abstract description 35
- 238000000746 purification Methods 0.000 title claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 77
- 238000004821 distillation Methods 0.000 claims abstract description 59
- 239000013078 crystal Substances 0.000 claims abstract description 39
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 35
- 238000004062 sedimentation Methods 0.000 claims abstract description 33
- 230000007062 hydrolysis Effects 0.000 claims abstract description 27
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 27
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 25
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 claims abstract description 22
- 229910052567 struvite Inorganic materials 0.000 claims abstract description 21
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 20
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 17
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910019142 PO4 Inorganic materials 0.000 claims description 22
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 22
- 239000010452 phosphate Substances 0.000 claims description 22
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 20
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 19
- 230000008569 process Effects 0.000 claims description 18
- 239000003337 fertilizer Substances 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 16
- 239000012528 membrane Substances 0.000 claims description 13
- 238000001035 drying Methods 0.000 claims description 10
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 7
- 239000011777 magnesium Substances 0.000 claims description 7
- 229910052749 magnesium Inorganic materials 0.000 claims description 7
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 6
- 239000004202 carbamide Substances 0.000 claims description 6
- 244000005700 microbiome Species 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 238000012544 monitoring process Methods 0.000 claims description 5
- 125000001477 organic nitrogen group Chemical group 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 238000001556 precipitation Methods 0.000 claims description 5
- 230000001737 promoting effect Effects 0.000 claims description 5
- 239000006228 supernatant Substances 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- 238000005292 vacuum distillation Methods 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 3
- 239000002957 persistent organic pollutant Substances 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 206010046555 Urinary retention Diseases 0.000 claims description 2
- 238000002425 crystallisation Methods 0.000 claims description 2
- 230000008025 crystallization Effects 0.000 claims description 2
- YUWBVKYVJWNVLE-UHFFFAOYSA-N [N].[P] Chemical compound [N].[P] YUWBVKYVJWNVLE-UHFFFAOYSA-N 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000003301 hydrolyzing effect Effects 0.000 abstract description 5
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 abstract description 3
- 239000012535 impurity Substances 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 3
- 239000000243 solution Substances 0.000 description 24
- 239000003344 environmental pollutant Substances 0.000 description 12
- 231100000719 pollutant Toxicity 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000010802 sludge Substances 0.000 description 7
- -1 phosphate radical Chemical class 0.000 description 5
- 238000010992 reflux Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 230000001360 synchronised effect Effects 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000002195 synergetic effect Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 108010046334 Urease Proteins 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/45—Phosphates containing plural metal, or metal and ammonium
- C01B25/451—Phosphates containing plural metal, or metal and ammonium containing metal and ammonium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/005—Black water originating from toilets
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/06—Pressure conditions
- C02F2301/063—Underpressure, vacuum
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
Abstract
The invention provides a device and a method for recycling and purifying nitrogen and phosphorus in urine sewage, belonging to the technical field of sewage treatment. The hydrolysis pool is used for collecting, storing and hydrolyzing urine resources; the reduced pressure distillation tower is used for realizing the separation of nitrogen resources in the hydrolyzed urine and completing the recovery of nitrogen and phosphorus resources by connecting the sedimentation tank with the dissolving tank; the MBR reactor is used for removing nitrogen and organic matters remained after urine resource recovery. The invention reduces the nitrogen load of downstream sewage treatment plants, improves the carbon-nitrogen ratio and saves the treatment cost; the ammonia is separated quickly and efficiently, and the ammonia gas is recovered efficiently by means of the sulfuric acid solution; the heat loss is reduced, and the energy consumption is reduced; the recovered ammonium sulfate crystal and magnesium ammonium phosphate crystal have less impurities, single component and higher purity.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a device and a method for recovering and purifying nitrogen and phosphorus in urine sewage.
Background
With the gradual manifestation of the defects of the traditional sewage treatment facility (high cost, high energy consumption, low benefits, difficulty in maintaining balance of income and expenditure, and the like), the emergence of the problem of exhaustion of non-renewable resources caused by the fact that chemical fertilizers are used in large quantities due to the rapid increase of population, and the urgent need for renewable agricultural fertilizers, scientists propose a concept of 'source separation', namely, the concept conversion from 'human excrement from buildings to sewage treatment plants' to 'food from farmlands to buildings and back to farmlands' is completed by taking the separation of human excrement from the source to the recovery, concentration and recycling of phytonutrients (using the phytonutrients as crop fertilizers) as a whole of a cycle. Wherein, human urine is one of the important components of domestic sewage, although only occupies 1% of sewage volume, the human urine contains 80% of nitrogen and 50% of phosphorus in the domestic sewage, and has extremely high recovery value and pollution load. The pressure of a sewage treatment plant can be greatly relieved by collecting human urine from the source, recycling resources and removing pollutants, and meanwhile, high-quality renewable fertilizer can be obtained for sustainable development of farmlands.
Nitrogen in fresh human urine mainly exists in the form of urea, and after being stored at normal temperature, the nitrogen is hydrolyzed by urease generated by microorganisms and converted into ammonia and carbonate ions, and meanwhile, the pH value is increased from 7.0 to about 9.0. At this pH, the ammonia is predominantly NH3·H2The O exists in a form and is easy to volatilize and separate. Meanwhile, phosphorus in urine is mainly phosphate radical (PO)4 3-) In the form of (A), under alkaline conditionsIs easy to react with calcium and magnesium ions to form crystal crystals. When the urine hydrolysis is complete, the pH rises and conditions are established for precipitation of suitable phosphate crystals.
The current common technology for urine resource recovery is to promote phosphate radical and ammonia ions in urine to form magnesium ammonium phosphate crystals by adding a magnesium-containing medicament or brine, and then to crystallize, precipitate, separate and recover. The method can efficiently recover phosphorus in urine, and the recovery rate is as high as more than 95%, but the recovery rate of nitrogen is very low, and is only about 5%. In addition, the urine has low COD (1.2:1) and N (5:1) which cannot meet the requirement of biological denitrification, thereby causing the difficulty in removing the pollutants in the urine after resource recovery. In conclusion, the main defects of the prior art are that nitrogen in the recovered urine cannot be effectively removed, which causes difficulty in subsequent biological denitrification, and further affects the operation cost of the domestic sewage treatment facility, and causes high cost, high treatment difficulty, high energy consumption, low benefit and unsustainability.
Disclosure of Invention
The invention aims to provide a method for synchronously adding a reduced pressure distillation process on the basis of an ammonium magnesium phosphate precipitation method, so that urine is boiled at low temperature and low pressure, ammonia nitrogen in the urine is volatilized by ammonia gas, and then the ammonia nitrogen is separated and recovered (the recovery rate is 80%) to finish the efficient recovery of resources in the urine; the device and the method for recovering, purifying and treating the urine sewage nitrogen and phosphorus meet the requirement of biological denitrification and effectively remove residual pollutants in urine so as to solve at least one technical problem in the background technology.
In order to achieve the purpose, the invention adopts the following technical scheme:
in one aspect, the invention provides a device for recovering, purifying and treating nitrogen and phosphorus in urine sewage, comprising:
the hydrolysis tank is used for collecting urine, the hydrolysis tank is communicated with a reduced pressure distillation tower, the reduced pressure distillation tower is communicated with a dissolving tank and a sedimentation tank, the dissolving tank is communicated with a vacuum pump, and the sedimentation tank is communicated with an MBR (membrane bioreactor).
Preferably, the hydrolysis pool is used for collecting, storing and hydrolyzing urine resources; the reduced pressure distillation tower is used for realizing the separation of nitrogen resources in the hydrolyzed urine and completing the recovery of nitrogen and phosphorus resources by connecting the sedimentation tank with the dissolving tank; the MBR reactor is used for removing nitrogen and organic matters remained after urine resource recovery.
Preferably, the MBR is divided into an anoxic tank and an aerobic tank, biological denitrification is performed by a short-cut nitrification and denitrification process of pre-denitrification, dissolved oxygen is controlled by an aeration system, and water is discharged by using a flat membrane.
In a second aspect, the invention provides a urine sewage treatment method using the urine sewage nitrogen and phosphorus recovery and purification device, comprising: collecting and hydrolyzing urine in a hydrolysis tank; the urine is hydrolyzed and enters a reduced pressure distillation tower to complete nitrogen resource separation, ammonia is converted into ammonia gas through reduced pressure distillation and is discharged from the top of the reduced pressure distillation tower, and meanwhile, phosphate is converted into magnesium ammonium phosphate crystals through chemical dosing crystallization; ammonia enters a dissolving tank, is absorbed by sulfuric acid solution and reacts to be converted into ammonium sulfate solution, and is dried into ammonium sulfate crystals after being saturated to be collected; the urine after the reduced pressure distillation enters a sedimentation tank to complete the separation of phosphorus resources, and the magnesium ammonium phosphate crystals are discharged and collected after sedimentation; and finally, the residual urine enters an MBR reactor to finish the removal of the residual organic pollutants and ammonia nitrogen in the sewage.
Preferably, the specific steps comprise:
step 1, urine enters a hydrolysis tank through a urinal, high-concentration organic nitrogen and urea in the urine are hydrolyzed into ammonia nitrogen under the action of microorganisms in the tank, and organic phosphorus is hydrolyzed into phosphate;
step 2, feeding the hydrolyzed urine into a reduced pressure distillation tower, boiling the urine in a low temperature environment through low-temperature heating and vacuum pump pressure reduction, promoting ammonia nitrogen in the urine to be converted into gaseous ammonia, and capturing the gaseous ammonia by a dissolving tank through suction of a vacuum pump to form ammonium sulfate;
and 6, periodically monitoring the pH value of the dissolving tank, replacing the solution in the tank when the pH value is more than or equal to 5, and drying the saturated ammonium sulfate solution into ammonium sulfate crystals at low temperature to realize the efficient recovery of ammonia in urine.
Preferably, the ammonia nitrogen accounts for more than 99% of the total nitrogen content and the phosphate accounts for more than 99% of the total phosphorus content after the urine is hydrolyzed in the step 1.
Preferably, the heating temperature of the reduced pressure distillation tower in the step 2 is 55-60 ℃, and the air pressure is controlled to be 21-26 KPa.
Preferably, in step 3, the phosphate is precipitated in the precipitation tank by adding magnesium chloride, magnesium: the adding mass ratio of phosphorus is 1.2: 1.
preferably, the recovery rate of phosphorus in the hydrolyzed urine in the step 4 is more than 95%.
Preferably, the total ammonia nitrogen removal rate of the recovered effluent in the step 5 is more than 15%, more than 95% of nitrogen in urine is removed by vacuum distillation recovery coupled biological denitrification, and the total removal rate of COD is more than 90%.
In the above technical solution, the related technical terms are explained as follows:
MBR reactor: the membrane bioreactor is mainly used for treating domestic sewage and removing pollutants such as nitrogen, phosphorus and the like contained in the sewage;
magnesium ammonium phosphate: urine contains high-concentration phosphate radical ions, and the ions can react with calcium, magnesium, ammonium and other ions under alkaline conditions to form crystals, so that the slow-release fertilizer is efficient.
And (3) reduced pressure distillation: the surface pressure of the solution is reduced under a closed condition, so that the solution is promoted to boil under a low-temperature condition, and components with different volatility in the solution are separated through violent evaporation.
The invention has the beneficial effects that:
the resource recovery of urine of the urinal is completed at the source of a sewage pipe network by utilizing the coupling of the reduced pressure distillation tower with the dissolving tank and the sedimentation tank, so that the recovery value of the urine is fully realized; meanwhile, the rear MBR reactor prevents the pollution load in urine from entering a sewage pipe network, thereby reducing the nitrogen load of a downstream sewage treatment plant, improving the carbon-nitrogen ratio, reducing the treatment difficulty and saving the treatment cost;
the magnesium chloride is added into the reduced pressure distillation tower, so that the synchronous separation, concentration and subsequent recovery of nitrogen and phosphorus in urine are realized;
the reduced pressure distillation tower promotes urine to boil under the low temperature condition in a reduced pressure heating mode, accelerates the volatilization of ammonia, solves the problems of low efficiency and low separation speed when ammonia is separated from urine, does not need to provide an additional aeration device, realizes the rapid and efficient separation of ammonia, and realizes the efficient recovery of ammonia gas by means of sulfuric acid solution;
the reduced pressure distillation tower promotes the urine to boil under the low temperature condition in a reduced pressure heating mode, so that the energy required for heating the urine to boil under normal pressure is greatly reduced, the heat loss is reduced through measures such as external heat preservation, the energy consumption is reduced, and the resource recovery with more energy conservation and environmental protection is realized;
the MBR reactor removes the residual nitrogen and organic matters in the urine by using a short-cut nitrification and denitrification process, the process is simple to operate, stable to operate and less in sludge discharge, and the pollutants are efficiently removed;
the recovered ammonium sulfate crystal and magnesium ammonium phosphate crystal have less impurities, single component and higher purity, can be used as fertilizer, and are high-quality renewable fertilizer.
Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
Fig. 1 is a flow chart of a urine sewage treatment method using a urine sewage nitrogen and phosphorus recovery and purification device according to an embodiment of the present invention.
Wherein: 1-a urinal; 2-a hydrolysis tank; 3-a reduced pressure distillation column; 4-a sedimentation tank; 5-MBR reactor; 6-a dissolving tank; 7-vacuum pump.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below by way of the drawings are illustrative only and are not to be construed as limiting the invention.
It will be understood by those skilled in the art that, unless otherwise defined, all terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the prior art and will not be interpreted in an idealized or overly formal sense unless expressly so defined herein.
As used herein, the singular forms "a", "an", "the" and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It will be further understood that the terms "comprises" and/or "comprising," when used in this specification, specify the presence of stated features, integers, steps, operations, elements, and/or components, but do not preclude the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean 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 invention. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
In the description of the present specification, the terms "first", "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implying any number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
In the description of the present specification, the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, only for convenience of description and simplification of description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present technology.
Unless expressly stated or limited otherwise, the terms "mounted," "connected," "coupled," and "disposed" are intended to be inclusive and mean, for example, that they may be fixedly coupled or disposed, or that they may be removably coupled or disposed, or that they may be integrally coupled or disposed. The specific meaning of the above terms in the present technology can be understood by those of ordinary skill in the art as appropriate.
For the purpose of facilitating an understanding of the present invention, the present invention will be further explained by way of specific embodiments with reference to the accompanying drawings, which are not intended to limit the present invention.
It should be understood by those skilled in the art that the drawings are merely schematic representations of embodiments and that the elements shown in the drawings are not necessarily required to practice the invention.
Example 1
As shown in fig. 1, in order to achieve efficient, energy-saving and fast recovery of nitrogen and phosphorus in urine of a urinal and removal of residual pollutants, in this embodiment 1, a processing apparatus and method for recovering nitrogen and phosphorus from urine sewage of a urinal and removing pollutants are provided.
A treatment device for recovering nitrogen and phosphorus from urine sewage of a toilet stool and removing pollutants mainly comprises a hydrolysis tank 2, a reduced pressure distillation tower 3, a sedimentation tank 4, an MBR (membrane bioreactor) 5, a dissolving tank 6, a vacuum pump 7 and the like. The hydrolysis tank 2 is used for pretreatment before urine resource recovery of the urinal and is a functional regulation and storage structure for collecting, storing and hydrolyzing urine; the reduced pressure distillation tower 3 is used for realizing the separation of nitrogen and phosphorus resources in the hydrolyzed urine and completing the recovery of the nitrogen and phosphorus resources by connecting the dissolving tank 6 with the sedimentation tank 4; MBR 5 is used for high-efficient remaining nitrogen and organic matter after getting rid of urine resource recovery, and the sewage after the processing can flow to municipal pipe network. The recovered ammonium sulfate solution and magnesium ammonium phosphate crystal are further dried at low temperature and then used as fertilizer.
In this embodiment 1, the urine sewage treatment comprises the following steps:
step 1, urine enters a hydrolysis tank 2 through a urinal 1, high-concentration organic nitrogen and urea in the urine are hydrolyzed into ammonia nitrogen under the action of microorganisms in the tank, and organic phosphorus is hydrolyzed into phosphate;
step 2, feeding the hydrolyzed urine into a reduced pressure distillation tower 3 from a hydrolysis tank 2, boiling the urine in a low temperature environment through low temperature heating and vacuum pump pressure reduction, promoting ammonia nitrogen in the urine to be converted into gaseous ammonia, and capturing the gaseous ammonia by a dissolving tank 6 through suction of a vacuum pump 7 to form ammonium sulfate;
and 6, regularly monitoring the pH value of the dissolving tank 6, replacing the solution in the tank when the pH value is more than or equal to 5, and drying the saturated ammonium sulfate solution into ammonium sulfate crystals at low temperature to realize the efficient recovery of ammonia in urine.
In the step 1, the ammonia nitrogen/total nitrogen content after the urine hydrolysis is more than 99 percent, and the phosphate/total phosphorus content is more than 99 percent.
In the step 2, the reduced pressure distillation tower 3 consists of an upper part, a middle part and a lower part, and the lowest end is a heating part for realizing the temperature rise and boiling of urine; the middle part is used for placing urine; the upper end is a condensation layer for recovering the redundant moisture in the volatilized ammonia gas. The periphery of the tower is wrapped with heat insulation materials for reducing heat loss.
In the step 2, the reduced pressure distillation tower 3 and the dissolving tank 6 are sealed for keeping a low pressure state.
In the step 2, the heating temperature of the reduced pressure distillation tower 3 is 55-60 ℃, the air pressure is controlled to be 21-26 KPa, and the reaction time is 3 hours.
The recovery rate of nitrogen in the hydrolyzed urine in step 2 was 80%.
Precipitation of phosphate by addition of magnesium chloride in step 3 had little effect on ammonia separation and recovery, magnesium: the optimal adding ratio of phosphorus is 1.2: 1.
the recovery rate of the phosphorus in the hydrolyzed urine in the step 4 is over 95 percent.
The total removal rate of ammonia nitrogen in the recovered effluent in the step 5 is more than 15%, more than 95% of nitrogen in urine is removed by vacuum distillation recovery coupled with biological denitrification, and the total removal rate of COD is 90%.
In the step 5, the MBR 5 carries out biological denitrification through a short-cut nitrification and denitrification process of pre-denitrification and is divided into an anoxic tank and an aerobic tank. Urine sewage flows into the anoxic tank through a pipeline for denitrification to remove organic matters in the sewage; then the sludge enters an aerobic tank for short-range nitrification, the sludge reflux is used for refluxing the sludge-water mixture containing the nitrite to the anoxic tank, the nitrite in the sludge is removed through denitrification, and the reflux ratio is 3.0.
In the step 5, the MBR 5 controls the dissolved oxygen to be 0.5 +/-0.1 mg/L through an aeration system, the urine sewage stays for 3 days, the reaction temperature is 20-25 ℃, and water is discharged by utilizing a flat membrane with the pore diameter of 0.1 micron.
In the embodiment 1, the resource recovery of urine of the urinal is completed at the source of a sewage pipe network by using a reduced pressure distillation tower coupled with a dissolving tank and a sedimentation tank, so that the recovery value of the urine is fully realized; meanwhile, the rear MBR reactor prevents the pollution load in urine from entering a sewage pipe network, thereby reducing the nitrogen load of a downstream sewage treatment plant, improving the carbon-nitrogen ratio, reducing the treatment difficulty and saving the treatment cost; the magnesium chloride is added into the reduced pressure distillation tower, so that the synchronous separation, concentration and subsequent recovery of nitrogen and phosphorus in urine are realized; the reduced pressure distillation tower promotes urine to boil under the low temperature condition in a reduced pressure heating mode, accelerates the volatilization of ammonia, solves the problems of low efficiency and low separation speed when ammonia is separated from urine, does not need to provide an additional aeration device, realizes the rapid and efficient separation of ammonia, and realizes the efficient recovery of ammonia gas by means of sulfuric acid solution; the reduced pressure distillation tower promotes the urine to boil under the low temperature condition in a reduced pressure heating mode, so that the energy required for heating the urine to boil under normal pressure is greatly reduced, the heat loss is reduced through measures such as external heat preservation, the energy consumption is reduced, and the resource recovery with more energy conservation and environmental protection is realized; the MBR reactor removes the residual nitrogen and organic matters in the urine by using a short-cut nitrification and denitrification process, the process is simple to operate, stable to operate and less in sludge discharge, and the pollutants are efficiently removed; the recovered ammonium sulfate crystal and magnesium ammonium phosphate crystal have less impurities, single component and higher purity, can be used as fertilizer, and is a high-quality renewable fertilizer.
Example 2
In this embodiment 2, a treatment process and a method for recovering nitrogen and phosphorus from urine wastewater of a toilet stool and removing pollutants are provided, the process mainly comprises a hydrolysis tank, a reduced pressure distillation tower, an MBR reactor, a dissolving tank, a settling tank, and the like. The hydrolysis tank is used for pretreatment before urine resource recovery of the urinal and is a functional regulation and storage structure for collecting, storing and hydrolyzing urine; the reduced pressure distillation tower is used for realizing the separation of nitrogen and phosphorus resources in the hydrolyzed urine and completing the recovery of the nitrogen and phosphorus resources by connecting the dissolving tank with the sedimentation tank; the MBR reactor is used for removing residual nitrogen and organic matters after urine resources are recovered with high efficiency, and the treated sewage flows to a municipal pipe network. The recovered ammonium sulfate solution and magnesium ammonium phosphate crystal are further dried at low temperature and then used as fertilizer.
The specific process is as follows: urine sewage of the urinal enters a hydrolysis tank firstly; the rear part of the hydrolysis tank is connected with a reduced pressure distillation tower; the upper end of the reduced pressure distillation tower is connected with a dissolving tank, and a gas outlet of the dissolving tank is connected with a vacuum pump; the lower end of the reduced pressure distillation tower is connected with a sedimentation tank; the back of the sedimentation tank is connected with an MBR reactor. The treatment effect is shown in table 1.
TABLE 1 Water quality index and removal Rate before and after urinal urine treatment
Example 3
As shown in fig. 1, a treatment process and method for recovering nitrogen and phosphorus from urine wastewater of a toilet stool and removing pollutants comprises the following steps:
step 1, urine enters a hydrolysis tank through a urinal and a sewer pipe, high-concentration organic nitrogen and urea in the urine are hydrolyzed into ammonia nitrogen under the synergistic action of microorganisms in the tank, organic phosphorus is hydrolyzed into phosphate, and the conversion rate is up to 99%;
step 2, feeding the hydrolyzed urine into a reduced pressure distillation tower through a pipeline and a valve, boiling the urine through low-temperature heating at 55 ℃ and a reduced pressure environment of 26KPa, promoting ammonia nitrogen in the urine to be converted into gaseous ammonia, capturing the gaseous ammonia by a dissolving tank through suction of a vacuum pump to form ammonium sulfate, and reacting for 3 hours to obtain the ammonia nitrogen conversion rate of 75%;
and 6, regularly monitoring the pH value of the dissolving and recovering pool, replacing the solution in the pool when the pH value is more than or equal to 5, and drying the saturated ammonium sulfate solution into ammonium sulfate crystals at low temperature to realize the efficient recovery of ammonia in urine.
This embodiment 3 can be fast, high-efficient, energy-conserving synchronous recovery urine in nitrogen, phosphorus resource to remaining organic pollutant and nitrogen in the more thorough removal urine, be a set of environmental protection sustainable urine sewage treatment process and method.
Example 4
In this embodiment 4, a treatment process and method for recovering nitrogen and phosphorus from urine wastewater of a toilet stool and removing pollutants includes the following steps:
step 1, urine enters a hydrolysis tank through a urinal and a sewer pipe, high-concentration organic nitrogen and urea in the urine are hydrolyzed into ammonia nitrogen under the synergistic action of microorganisms in the tank, organic phosphorus is hydrolyzed into phosphate, and the conversion rate is up to 99%;
step 2, feeding the hydrolyzed urine into a reduced pressure distillation tower through a pipeline and a valve, boiling the urine through low-temperature heating at 60 ℃ and a reduced pressure environment of 21KPa, promoting ammonia nitrogen in the urine to be converted into gaseous ammonia, capturing the gaseous ammonia by a dissolving tank through suction of a vacuum pump to form ammonium sulfate, and reacting for 3 hours to obtain the ammonia nitrogen conversion rate of 80%;
step 6, enabling supernatant of the sedimentation tank to enter an MBR (membrane bioreactor) through a pump and a pipeline, removing residual ammonia and organic matters after distillation of hydrolyzed urine by utilizing a short-range nitrification-denitrification treatment process of pre-denitrification, wherein the MBR is divided into an anoxic tank and an aerobic tank, the sludge reflux ratio is 3.0, dissolved oxygen is controlled to be 0.5 +/-0.1 mg/L through an aeration system, the retention time of sewage is 2-3 days, the reaction temperature is 25-30 ℃, and water is discharged by utilizing a flat membrane with the pore size of 0.1 micrometer;
and 7, regularly monitoring the pH value of the dissolving and recovering pool, replacing the solution in the pool when the pH value is more than or equal to 5, and drying the saturated ammonium sulfate solution into ammonium sulfate crystals at low temperature to realize the efficient recovery of ammonia in urine.
Although the embodiments of the present invention have been described with reference to the accompanying drawings, it is not intended to limit the scope of the present invention, and it should be understood by those skilled in the art that various modifications and variations can be made without inventive efforts based on the technical solutions disclosed in the present invention.
Claims (10)
1. The utility model provides a urine sewage nitrogen phosphorus recovery purification unit which characterized in that includes:
a pond (2) of hydrolysising for collecting the urine, pond (2) of hydrolysising intercommunication has reduced pressure distillation tower (3), reduced pressure distillation tower (3) intercommunication dissolving tank (6) and sedimentation tank (4), dissolving tank (6) intercommunication vacuum pump (7), sedimentation tank (4) intercommunication MBR reactor (5).
2. The device for the recovery, purification and treatment of nitrogen and phosphorus in urine wastewater as claimed in claim 1, wherein the hydrolysis tank (2) is used for collection, storage and hydrolysis of urine resources; the reduced pressure distillation tower (3) is used for separating nitrogen resources in the hydrolyzed urine and completing the recovery of the nitrogen and phosphorus resources by connecting the sedimentation tank (4) and the dissolving tank (6); the MBR (5) is used for removing nitrogen and organic matters remained after the urine resource recovery.
3. The apparatus for recovering, purifying and treating nitrogen and phosphorus in urine wastewater according to claim 2, wherein the MBR (5) is divided into an anoxic tank and an aerobic tank, biological denitrification is performed by a pre-denitrification shortcut nitrification and denitrification process, dissolved oxygen is controlled by an aeration system, and water is discharged by using a flat membrane.
4. The urine sewage treatment method using the urine sewage nitrogen and phosphorus recovery and purification device as claimed in claim 1, 2 or 3, comprising: the hydrolysis pool (2) collects and hydrolyzes urine; the urine is hydrolyzed and enters a reduced pressure distillation tower (3) to complete nitrogen resource separation, ammonia is converted into ammonia gas through reduced pressure distillation and is discharged from the top of the reduced pressure distillation tower (3), and meanwhile, phosphate is converted into magnesium ammonium phosphate crystals through chemical dosing crystallization; ammonia enters a dissolving tank (6) and is absorbed by a sulfuric acid solution to react and be converted into an ammonium sulfate solution, and after saturation, the ammonium sulfate solution is dried into ammonium sulfate crystals to be collected; the urine after the reduced pressure distillation enters a sedimentation tank to complete the separation of phosphorus resources, and the magnesium ammonium phosphate crystals are discharged and collected after sedimentation; and finally, the residual urine enters an MBR (5) to finish the removal of the residual organic pollutants and ammonia nitrogen in the sewage.
5. The method of claim 4, wherein:
step 1, urine enters a hydrolysis tank through a urinal, high-concentration organic nitrogen and urea in the urine are hydrolyzed into ammonia nitrogen under the action of microorganisms in the tank, and organic phosphorus is hydrolyzed into phosphate;
step 2, feeding the hydrolyzed urine into a reduced pressure distillation tower, boiling the urine in a low temperature environment through low-temperature heating and vacuum pump pressure reduction, promoting ammonia nitrogen in the urine to be converted into gaseous ammonia, and capturing the gaseous ammonia by a dissolving tank through suction of a vacuum pump to form ammonium sulfate;
step 3, during the reduced pressure distillation, adding a magnesium chloride solution into a reduced pressure distillation tower to promote phosphate in the hydrolyzed urine to form magnesium ammonium phosphate crystals;
step 4, feeding the hydrolyzed urine into a sedimentation tank after distillation is finished, periodically clearing the magnesium ammonium phosphate crystals after sedimentation, and drying the crystals at a low temperature to be used as a fertilizer, thereby realizing efficient recovery of phosphorus in the urine;
step 5, enabling supernatant in the sedimentation tank to enter an MBR (membrane bioreactor), and removing residual ammonia and organic matters after distillation of the hydrolyzed urine by using a short-cut nitrification and denitrification treatment process;
and 6, periodically monitoring the pH value of the dissolving tank, replacing the solution in the tank when the pH value is more than or equal to 5, and drying the saturated ammonium sulfate solution into ammonium sulfate crystals at low temperature to realize the efficient recovery of ammonia in urine.
6. The method according to claim 5, wherein the ammonia nitrogen is more than 99% of the total nitrogen content and the phosphate is more than 99% of the total phosphorus content after the urine is hydrolyzed in step 1.
7. The method as claimed in claim 6, wherein the heating temperature of the vacuum distillation tower in the step 2 is 55-60 ℃, the air pressure is controlled to be 21-26 Kpa, and the recovery rate of nitrogen in the hydrolyzed urine is 80%.
8. The method according to claim 7, characterized in that in step 3, the phosphate is precipitated in the precipitation tank by adding magnesium chloride, magnesium: the adding mass ratio of phosphorus is 1.2: 1.
9. the method of claim 8, wherein the recovery of phosphorus from the hydrolyzed urine in step 4 is greater than 95%.
10. The method according to claim 9, wherein the total removal rate of ammonia nitrogen in the recovered effluent in the step 5 is more than 15%, more than 95% of nitrogen in urine is removed by vacuum distillation recovery coupled with biological denitrification, and the total removal rate of COD is more than 90%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111551813.6A CN114380460A (en) | 2021-12-17 | 2021-12-17 | Urine sewage nitrogen and phosphorus recovery and purification treatment device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111551813.6A CN114380460A (en) | 2021-12-17 | 2021-12-17 | Urine sewage nitrogen and phosphorus recovery and purification treatment device and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114380460A true CN114380460A (en) | 2022-04-22 |
Family
ID=81197827
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111551813.6A Pending CN114380460A (en) | 2021-12-17 | 2021-12-17 | Urine sewage nitrogen and phosphorus recovery and purification treatment device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114380460A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117263289A (en) * | 2023-11-10 | 2023-12-22 | 北京工业大学 | Distributed treatment system and method for recycling nutrition of source separation urine |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4137158A (en) * | 1975-12-25 | 1979-01-30 | Hitachi, Ltd. | Process for tertiary treatment of waste waters from anaerobic digestion treatment process |
| CN103482824A (en) * | 2013-09-18 | 2014-01-01 | 西安建筑科技大学 | Method and device for quickly recycling nitrogen and phosphorus nutrient substances in urine |
| CN106186593A (en) * | 2016-09-20 | 2016-12-07 | 浙江工商大学 | The urine wastewater treatment equipment of a kind of recyclable nitrogen phosphorus and the method for recyclable nitrogen phosphorus |
| CN108423953A (en) * | 2018-05-11 | 2018-08-21 | 西安交通大学 | Recovery of nitrogen and phosphorus system and method in a kind of municipal sludge based on supercritical technology |
| CN111875171A (en) * | 2020-08-03 | 2020-11-03 | 河北工业大学 | Duck breeding wastewater treatment process and resource recovery method |
-
2021
- 2021-12-17 CN CN202111551813.6A patent/CN114380460A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4137158A (en) * | 1975-12-25 | 1979-01-30 | Hitachi, Ltd. | Process for tertiary treatment of waste waters from anaerobic digestion treatment process |
| CN103482824A (en) * | 2013-09-18 | 2014-01-01 | 西安建筑科技大学 | Method and device for quickly recycling nitrogen and phosphorus nutrient substances in urine |
| CN106186593A (en) * | 2016-09-20 | 2016-12-07 | 浙江工商大学 | The urine wastewater treatment equipment of a kind of recyclable nitrogen phosphorus and the method for recyclable nitrogen phosphorus |
| CN108423953A (en) * | 2018-05-11 | 2018-08-21 | 西安交通大学 | Recovery of nitrogen and phosphorus system and method in a kind of municipal sludge based on supercritical technology |
| CN111875171A (en) * | 2020-08-03 | 2020-11-03 | 河北工业大学 | Duck breeding wastewater treatment process and resource recovery method |
Non-Patent Citations (1)
| Title |
|---|
| 高振超: "源分离尿液的氮磷资源化与处理技术研究", 《中国优秀硕士学位论文全文数据库 工程科技I辑》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117263289A (en) * | 2023-11-10 | 2023-12-22 | 北京工业大学 | Distributed treatment system and method for recycling nutrition of source separation urine |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105461061B (en) | A kind of municipal sewage A2/ O- biology synchronous denitrification dephosphorizing device and method | |
| CN103641272B (en) | High concentrated organic wastewater and percolate zero-discharge treatment system | |
| CN112661266B (en) | Process for enriching phosphorus and recovering wustite by using biomembrane method | |
| CN112093981B (en) | Sewage treatment device and process for synchronous efficient pollutant removal and comprehensive recycling | |
| CN102503035B (en) | Biological phosphorus accumulating and phosphorus recycling method for treating phosphorus-containing liquid waste | |
| CN115057534B (en) | Low-carbon sewage nitrogen and phosphorus removal system and process | |
| CN111675322A (en) | Method for quickly obtaining high-concentration anaerobic ammonia oxidation granular sludge and anaerobic ammonia oxidation granular sludge | |
| CN104609651B (en) | A kind of Large-scale pig farm advanced waste treatment system | |
| CN109912145B (en) | Aerobic granular sludge power generation device | |
| CN109502748B (en) | Sewage treatment system and method based on nitrosation-anaerobic ammonium oxidation-induced crystallized phosphorus recovery | |
| CN109851161B (en) | Treatment method of sewage produced in production of biphenyl dichlorobenzyl and o-sodium sulfonate benzaldehyde | |
| CN114380460A (en) | Urine sewage nitrogen and phosphorus recovery and purification treatment device and method | |
| CN214360828U (en) | Sewage treatment device for synchronously removing high-efficiency pollutants and comprehensively recycling pollutants | |
| CN113213714A (en) | Raw material medicine wastewater treatment process | |
| CN111592104A (en) | Short-range efficient biological treatment device and treatment method for kitchen waste digestive juice | |
| CN112520852B (en) | Method for removing and recovering phosphorus in sewage | |
| CN114477652B (en) | Advanced treatment system and method for urban sewage | |
| CN207418548U (en) | A kind of sewage recycling processing unit | |
| CN203112656U (en) | Short-cut nitrification sewage treatment device | |
| CN113860431A (en) | Device and process for relieving ion exchanger pollution | |
| US20230242427A1 (en) | Method for phosphorus removal and recovery using organic carbon source of urban sewage | |
| CN217377622U (en) | Percolate concentrate treatment system | |
| CN216614109U (en) | Device for relieving ion exchanger pollution | |
| CN215886702U (en) | Sludge drying liquid treatment system | |
| CN220201636U (en) | Enhanced sludge pre-precipitation concentration deep denitrification sewage treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20220422 |