CN115611443A - High ammonia nitrogen wastewater treatment device and method - Google Patents
High ammonia nitrogen wastewater treatment device and method Download PDFInfo
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- CN115611443A CN115611443A CN202110782922.2A CN202110782922A CN115611443A CN 115611443 A CN115611443 A CN 115611443A CN 202110782922 A CN202110782922 A CN 202110782922A CN 115611443 A CN115611443 A CN 115611443A
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- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 14
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- 239000002351 wastewater Substances 0.000 claims abstract description 78
- 239000007789 gas Substances 0.000 claims abstract description 65
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 23
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims description 67
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 43
- 239000002253 acid Substances 0.000 claims description 27
- 230000002209 hydrophobic effect Effects 0.000 claims description 25
- 238000000926 separation method Methods 0.000 claims description 25
- 229910021529 ammonia Inorganic materials 0.000 claims description 23
- 239000012071 phase Substances 0.000 claims description 19
- -1 polypropylene Polymers 0.000 claims description 19
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- 239000012982 microporous membrane Substances 0.000 claims description 15
- 238000010521 absorption reaction Methods 0.000 claims description 12
- 238000002360 preparation method Methods 0.000 claims description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 11
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 11
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 239000004743 Polypropylene Substances 0.000 claims description 8
- 229920001155 polypropylene Polymers 0.000 claims description 8
- 239000011148 porous material Substances 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000003672 processing method Methods 0.000 claims 2
- 150000007514 bases Chemical class 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 8
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- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
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- 241000251468 Actinopterygii Species 0.000 description 1
- 206010007269 Carcinogenicity Diseases 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 206010021143 Hypoxia Diseases 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
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- 238000010170 biological method Methods 0.000 description 1
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- 238000009388 chemical precipitation Methods 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
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- 230000008878 coupling Effects 0.000 description 1
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- 235000020188 drinking water Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 208000005135 methemoglobinemia Diseases 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- XKLJHFLUAHKGGU-UHFFFAOYSA-N nitrous amide Chemical compound ON=N XKLJHFLUAHKGGU-UHFFFAOYSA-N 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
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- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
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- 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
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Physical Water Treatments (AREA)
Abstract
The application discloses high ammonia nitrogen wastewater treatment device and method, and the device comprises a pH adjusting unit, a gas dissolving unit, a releasing unit and a wastewater absorbing unit. The invention can realize the rapid release and recovery of ammonia nitrogen in the wastewater by utilizing the high specific surface area and mass transfer efficiency of the membrane contactor, obtains ammonia water with higher concentration while treating the wastewater to reach the specified discharge standard, and has higher economic benefit. In addition, the invention has the advantages of high integration level, compact equipment and easy skid-mounting, and has good application prospect in the field of ammonia nitrogen wastewater treatment.
Description
Technical Field
The application relates to a high ammonia nitrogen wastewater treatment device and method, and belongs to the field of wastewater treatment.
Background
The ammonia nitrogen wastewater has wide sources, such as domestic sewage, garbage penetrating fluid, industrial wastewater and the like. If ammonia nitrogen in the wastewater is directly discharged, great harm is caused to the ecological environment: ammonia nitrogen is one of the main factors causing eutrophication of water, and if ammonia nitrogen wastewater is directly discharged into water, a large amount of algae and microorganisms in the water can be caused to breed, so that the content of dissolved oxygen in the water is reduced, and in severe cases, fish and other aquatic organisms can be caused to die due to oxygen deficiency, thereby causing serious influence on water quality; the nitrifying action of ammonia nitrogen in water body can produce nitrite and nitrate, if the polluted water body is drinking water, the human can induce methemoglobinemia if drinking for a long time, and when the nitrite nitrogen content in the water is too high, the nitrite nitrogen can form nitrosamine by combining with protein, so that the nitrite nitrogen has carcinogenicity and can cause serious harm to human health. Therefore, the ammonia nitrogen wastewater has potential harm to both the ecological environment and human health, and the research on the treatment method has important significance.
The treatment method of the ammonia nitrogen wastewater mainly comprises an air stripping method, a breakpoint chlorination method, a chemical precipitation method, an ion exchange method, a biological method and the like. The stripping method is a main method in the current high ammonia nitrogen wastewater treatment process, and is characterized in that the pH value of wastewater is adjusted to be alkaline, ammonia nitrogen in the wastewater exists in a free ammonia form, and then gas (usually air or steam) is introduced into a stripping tower to strip the free ammonia from the wastewater. The method is suitable for treating high-concentration ammonia nitrogen wastewater and has the advantage of simple technology. However, the stripping method consumes a large amount of air or steam, so that the energy consumption of the process is high. In addition, many existing stripping devices have no ammonia recovery system in consideration of economy, and are directly discharged into the atmosphere to cause atmospheric pollution; if the overflowed ammonia gas is absorbed by sulfuric acid, although ammonium sulfate can be prepared as a fertilizer, the economic value is poorer than that of ammonia water.
The membrane contactor is a coupling product of a traditional absorption process and a membrane technology as a separation technology emerging in recent years, and has the advantages of large mass transfer area, compact structure and small volume. There are many reports on the application of membrane contactors to treat ammonia nitrogen wastewater [ Amaral M C S, magalhas N C, moravia W G, ferreira C D.Ammonia recovery from membrane filtration using hydrophilic membrane contactors Water Sci Technol,2016,74 (9): 2177-2184; removing ammonia nitrogen [ J ] in the recovered garbage percolation waste liquid by a PVDF membrane contactor, 2014,28 (1): 53-54. A common membrane contactor adopts a hydrophobic hollow fiber membrane as a barrier to separate ammonia nitrogen wastewater from absorption liquid. The absorption liquid is the weak solution that one or more acid in sulphuric acid, nitric acid, phosphoric acid mixes, and gaseous ammonia in the feed liquid can see through hydrophobic membrane pore under the partial pressure difference effect and generate ammonium salt with the acidizing fluid reaction side, realizes desorption and the recovery of ammonia nitrogen in the feed liquid. The patent CN203451325U and the patent CN209493324U also report the preparation of ammonia water by treating ammonia nitrogen wastewater by using a membrane contactor. However, the above reports are basically limited to the research of a certain link of ammonia nitrogen wastewater, and the membrane contactor technology is adopted to carry out the whole flow design and optimization on ammonia nitrogen wastewater treatment, so that the method has higher use value.
Disclosure of Invention
According to an aspect of the application, a high ammonia nitrogen effluent treatment plant is provided, the device utilizes the high specific surface area and the mass transfer efficiency of membrane contactor, can realize quick release and the recovery of ammonia nitrogen in the waste water, when reaching regulation emission standard with waste water treatment, obtained the aqueous ammonia of higher concentration again, have higher economic benefits. In addition, the invention has the advantages of high technical integration level, compact equipment and easy skid-mounting, and has good application prospect in the field of ammonia nitrogen wastewater treatment.
The device comprises:
the pH adjusting unit comprises a pH adjusting liquid storage container; used for adjusting the pH value of ammonia nitrogen wastewater to ensure that NH in the wastewater 4 + Conversion to volatile gaseous ammonia;
the gas dissolving unit comprises a membrane contactor A, a supercharging device I and a supercharging device II, wherein the supercharging device II is connected with a tube side inlet of the membrane contactor A, and a shell side inlet of the membrane contactor A is connected with a liquid outlet pipeline of the supercharging device I; adopting a membrane contactor to enable the gas to be dissolved in the wastewater to the maximum extent in a short time to form gas-dissolved water;
the releasing unit comprises a releaser and a gas-liquid separating device, and the releaser is suspended in the upper part in the cavity of the gas-liquid separating tank through a support; in the gas-liquid separation device, gas is arranged above the gas-liquid separation device, liquid is arranged below the gas-liquid separation device, and the releaser is positioned in the gas atmosphere; the dissolved gas water is released in a gas-liquid separation device by a releaser, and a large amount of micro bubbles are generated in the process, so that the volatilization of gaseous ammonia from the wastewater is accelerated;
a wastewater absorption unit comprising a membrane contactor B; further absorbing and treating the low-concentration ammonia nitrogen wastewater at the bottom of the gas-liquid separation device by adopting a membrane contactor, and realizing the standard-reaching discharge of the wastewater;
and the pH adjusting unit, the air dissolving unit, the releasing unit and the wastewater absorbing unit are sequentially connected along the wastewater flow direction.
The pH adjusting liquid storage container is connected with the supercharging device I, the shell pass outlet of the membrane contactor A is connected with the releaser, and the liquid outlet of the gas-liquid separation device is connected with the shell pass inlet of the membrane contactor B.
Optionally, the wastewater absorption unit further comprises a pump I and an acid storage tank, wherein a tube pass inlet of the membrane contactor B is connected with an outlet of the acid storage tank through the pump I, a tube pass outlet of the membrane contactor B is connected with an inlet of the acid storage tank through a pipeline, and the tube pass of the membrane contactor B contains acid.
Optionally, the membrane contactor a comprises a hollow fiber hydrophobic microporous membrane therein;
the material of the hollow fiber hydrophobic microporous membrane is selected from one of polypropylene, polytetrafluoroethylene, surface hydrophobic modified polypropylene and surface hydrophobic modified polytetrafluoroethylene;
the membrane porosity of the hollow fiber hydrophobic microporous membrane is 40-65%, and the average pore diameter is 0.02-0.25 μm.
Optionally, the device further comprises an ammonia water preparation unit, and the ammonia water is prepared by absorbing gaseous ammonia in gas-phase components at the top of the gas-liquid separation device in the membrane contactor by using low-temperature pure water.
Along the direction of the gas flow direction, the release unit, the ammonia water preparation unit and the gas dissolving unit are communicated in sequence;
the ammonia water preparation unit comprises a membrane contactor group and a water supply module; the membrane contactor group comprises N membrane contactors B, wherein N is more than or equal to 3;
along the gas flow direction, a tube side inlet of a 1 st membrane contactor B in the membrane contactor group is connected with a gas outlet pipeline of a gas-liquid separation device of the release unit, and a tube side outlet of an Nth membrane contactor B is connected with a gas inlet of a pressurizing device II of the gas dissolving unit;
optionally, along the gas flow direction, a tube side outlet of a 1 st membrane contactor B is communicated with a tube side inlet of a 2 nd membrane contactor B, and in turn, two adjacent tube sides of the membrane contactors B are communicated, and a tube side outlet of an N-1 st membrane contactor B is communicated with a tube side inlet of an nth membrane contactor B;
and the shell pass inlet of the Nth membrane contactor B is communicated with the water outlet of the water supply module, the shell passes of two adjacent membrane contactors B are communicated in sequence, and the shell pass outlet of the (N-1) th membrane contactor B is communicated with the shell pass inlet of the Nth membrane contactor B.
Optionally, a hollow fiber hydrophobic microporous membrane is included within the membrane contactor B;
the material of the hollow fiber hydrophobic microporous membrane is selected from one of polypropylene, polytetrafluoroethylene, surface hydrophobic modified polypropylene and surface hydrophobic modified polytetrafluoroethylene;
the membrane porosity of the hollow fiber hydrophobic microporous membrane is 35-55%, and the average pore diameter is 0.01-0.2 mu m;
the water supply module comprises a cooling component, a pump II and a liquid storage tank, wherein the shell pass inlet of the Nth membrane contactor B is sequentially connected with the cooling component, the pump II and the liquid storage tank through pipelines, and pure water is stored in the liquid storage tank.
According to another aspect of the present application, there is provided a method for treating high ammonia nitrogen wastewater, the method comprising: the high ammonia-nitrogen wastewater is treated by the wastewater treatment device, and the content of ammonia nitrogen in the high ammonia-nitrogen wastewater is more than or equal to 3500ppm.
Optionally, the method specifically includes the following steps:
(1) After passing through a pH adjusting liquid storage container, the high ammonia nitrogen wastewater enters a membrane contactor A through a supercharging device I and contacts with gas supercharged by a supercharging device II to form dissolved gas water;
(2) Releasing the dissolved gas water formed in the step (1) into a gas-liquid separation device through a releaser to form micro bubbles, volatilizing gaseous ammonia from the wastewater to form a gas-phase component containing the gaseous ammonia and ammonia nitrogen wastewater I;
(3) And (3) enabling acid liquor in the acid liquor storage tank to enter a membrane contactor B in the wastewater absorption unit through a pump I, and enabling the ammonia nitrogen wastewater I formed in the step (2) to be in contact treatment with the acid liquor in the membrane contactor B.
Optionally, the pH adjusting liquid storage container contains an alkaline compound for adjusting the pH value of the wastewater, and the alkaline compound can be added into the pH adjusting liquid storage container in the form of solid or concentrated solution;
the alkaline compound is selected from NaOH, KOH, ca (OH) 2 At least one of;
the pH value of the wastewater discharged from the pH adjusting liquid storage container is 9-13;
preferably, the pH value of the wastewater discharged from the pH adjusting liquid storage container is 10-12.
Optionally, in the step (1),
the gas is selected from at least one of air and nitrogen;
the pressure of the gas is 3-10 bar;
preferably, the pressure of the gas is between 5 and 8bar;
the contact time is 30 to 600s,
preferably, the contact time is 60 to 300s.
Optionally, in the step (2),
the pressure of the gas-liquid separation device is 1-5 bar;
preferably, the pressure of the gas-liquid separation device is 2-4 bar;
the size of the micro-bubbles is 10-200 mu m;
preferably, the size of the fine bubbles is 30 to 100 μm.
Optionally, in the step (3), the side pressure of ammonia nitrogen wastewater I in the membrane contactor B is 0-0.5 bar, and the side pressure of acid liquor is 0-0.5 bar;
the acid liquor is selected from one of phosphoric acid, sulfuric acid or hydrochloric acid;
the pH of the acid liquor is less than 3; the ammonia nitrogen content of the treated wastewater is lower than 25ppm.
Optionally, the method further comprises the steps of:
the gas-phase component containing gaseous ammonia enters a membrane contactor B in the ammonia water preparation unit, pure water enters the membrane contactor B through a water supply module, and the gas-phase component and the pure water are subjected to contact reaction to form ammonia water;
after contacting with pure water, unreacted gas phase components enter the membrane contactor A through the supercharging device II;
optionally, the temperature of the pure water is 0-20 ℃;
preferably, the temperature of the pure water is 1-10 ℃;
and the gas phase pressure in the membrane contactor B is 1-3 bar, the liquid phase pressure is 1.2-4 bar, and the liquid phase pressure is 0.2-1.0 bar higher than the gas phase pressure.
The beneficial effect that this application can produce includes:
1) Compared with the traditional stripping method which needs a large amount of gas for stripping, the method only needs a small amount of dissolved gas, has less gas consumption and low operation energy consumption;
2) The waste water after gas dissolving is released to a gas-liquid separation tank through a releaser, a large amount of micro bubbles are generated in the process, the size is 10-200 mu m, and the volatilization of gaseous ammonia from the waste water can be accelerated;
3) The ammonia water preparation unit is carried out under the pressure of 1-3 bar, the high operation pressure is favorable for ammonia absorption, and the ammonia water with higher concentration can be prepared compared with a vacuum pump mode;
4) The wastewater treatment reaches the specified discharge standard, and meanwhile, the ammonia water with higher concentration is obtained, so that the method has higher economic benefit;
5) The invention has the advantages of high technical integration level, compact equipment and easy skid-mounting.
Drawings
FIG. 1 is a schematic view of the apparatus of the present invention.
In the figure:
1-a pH adjusting liquid storage container; 2-a supercharging device I; 3-membrane contactor a; 4-a releaser; 5-a gas-liquid separation device; 6-membrane contactor B; 7-a cooling component; 8-pump II; 9-a liquid storage tank; 10-a supercharging device II; 11-membrane contactor B; 12-pump I; 13-an acid liquor storage tank.
Detailed Description
The invention is further described below with reference to the accompanying drawings. The invention is described in detail below with reference to specific exemplary embodiments. It will, however, be understood that various modifications and changes may be made without departing from the scope of the invention as defined in the appended claims. The detailed description and drawings are to be regarded as illustrative rather than restrictive, and any such modifications and variations are intended to be included within the scope of the present invention as described herein. Furthermore, the background is intended to be illustrative of the state of the art as developed and the meaning of the present technology and is not intended to limit the scope of the invention or the application and field of application of the invention.
Example 1
As shown in figure 1, the invention provides a device for treating high ammonia nitrogen wastewater, which comprises a pH adjusting unit, an air dissolving unit, a releasing unit and a wastewater absorbing unit;
the pH adjusting unit comprises a pH adjusting liquid storage container 1 for adjusting the pH value of the ammonia nitrogen wastewater to ensure that NH in the wastewater 4 + Conversion to volatile gaseous ammonia;
the gas dissolving unit comprises a supercharging device II10 and a membrane contactor A3, a tube pass inlet of the membrane contactor A3 is connected with a gas outlet pipeline of the supercharging device II10, and the membrane contactor is adopted to dissolve gas in wastewater to the maximum extent in a short time to form saturated gas dissolving water;
the releasing unit comprises a releaser 4 and a gas-liquid separating device 5, the releaser 4 is arranged in a cavity of the liquid separating device 5, saturated dissolved gas water is released in a gas-liquid separating tank by the releaser to form gas phase components rich in gas ammonia and low-concentration ammonia nitrogen wastewater, a large amount of micro bubbles are generated in the process, and the volatilization of the gas ammonia from the wastewater is accelerated;
the waste water absorption unit comprises a membrane contactor B11, a pump I12 and an acid liquor storage tank 13, wherein the pipe pass inlet of the membrane contactor B11 is connected with the outlet of the acid liquor storage tank 13 through the pump I12, the pipe pass outlet of the membrane contactor B11 is connected with the inlet of the acid liquor storage tank 13 through a pipeline, the membrane contactor is adopted to further absorb and treat low-concentration ammonia nitrogen waste water at the bottom of the gas-liquid separation tank, and the waste water is discharged up to the standard.
Along the liquid flow direction, the pH adjusting liquid storage container 1 is connected with a shell side inlet of a membrane contactor A3 of the dissolved air unit through a supercharging device I2, the dissolved air unit is connected with a releaser 4 of the release unit through a shell side outlet of the membrane contactor A3, and a liquid outlet of a gas-liquid separation device 5 of the release unit is connected with a shell side inlet of a membrane contactor B11 of the waste water absorption unit.
The ammonia nitrogen wastewater treatment device shown in figure 1 further comprises an ammonia water preparation unit, wherein the ammonia water preparation unit adopts low-temperature pure water to absorb gaseous ammonia in gas-phase components at the top of the gas-liquid separation device in the membrane contactor to prepare ammonia water. Including 3 membrane contactor B6, cooling part 7, pump II, liquid storage tank 9, along gas flow direction, the tube side import of 1 st membrane contactor B6 is connected with gas-liquid separation device 5's gas outlet, and 3 membrane contactor B6's tube side connects gradually, and the shell side import of 3 rd membrane contactor B6 connects gradually with cooling part 7, pump II and liquid storage tank 9 through the pipeline. As shown, gas flows through the membrane contactor tube side, while cooling water flows through the membrane contactor shell side.
Example 2
The embodiment also provides a method for treating high ammonia nitrogen wastewater, which applies the device shown in figure 1 and specifically comprises the following steps:
(1) Adjusting the pH value of wastewater with ammonia nitrogen content of 5000ppm to 12 by adopting NaOH in a pH adjusting liquid storage container 1; the wastewater is sent into a membrane contactor 3 of the gas dissolving unit through a supercharging device I2 and is contacted with high-pressure nitrogen (the pressure is 6.0 bar) from a supercharging device II10 in the gas dissolving unit to form saturated gas dissolving water, and the retention time of the wastewater in a membrane contactor A3 (assembled with a polytetrafluoroethylene hollow fiber hydrophobic microporous membrane, the membrane porosity is 50 percent, and the average pore diameter is 0.15 mu m) of the gas dissolving unit is 200s;
(2) Saturated dissolved gas water generated by the dissolved gas unit is released through a releaser 4 and decompressed and released to a gas-liquid separation device 5, the pressure of a gas-liquid separation tank is 2.5bar, a large amount of micro bubbles are generated in the process, the average size is 30 mu m, the volatilization of gaseous ammonia from waste water can be accelerated, a gas phase component containing the gaseous ammonia and ammonia nitrogen waste water I are formed, the ammonia nitrogen waste water I enters a membrane contactor B11 (assembled with a polytetrafluoroethylene hollow fiber hydrophobic microporous membrane, the membrane porosity is 45%, and the average pore diameter is 0.12 mu m), and the waste water side pressure in the membrane contactor B11 is 0.3bar;
(3) Dilute sulfuric acid (pH is maintained at 1-2) in the acid liquor storage tank 13 enters a membrane contactor B11 through a pump I12, the acid liquor side pressure in the membrane contactor B11 is 0.3bar, and ammonia nitrogen wastewater I is in contact with the dilute sulfuric acid and is treated to be below 10ppm, so that the discharge requirement is met.
The embodiment also includes a method for preparing ammonia water, which specifically comprises the following steps:
the generated gas phase component containing gaseous ammonia is absorbed and prepared into ammonia water in a membrane contactor B6 (comprising 3 membrane contactors, a polytetrafluoroethylene hollow fiber hydrophobic microporous membrane is assembled in the membrane contactor, the membrane porosity is 45 percent, and the average pore diameter is 0.12 mu m) by adopting pure water at 5 ℃, and the mass concentration of the prepared ammonia water is 20 percent; the gas phase pressure in the membrane contactor B6 is 2.0bar, and the liquid phase pressure is 2.2bar; the gas phase components are absorbed and then return to the air inlet of the supercharging device II 10.
Although the present application has been described with reference to a few embodiments, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the application as defined by the appended claims.
Claims (10)
1. The high ammonia nitrogen wastewater treatment device is characterized by comprising:
the pH adjusting unit comprises a pH adjusting liquid storage container;
the gas dissolving unit comprises a membrane contactor A, a supercharging device I and a supercharging device II, wherein the supercharging device II is connected with a tube side inlet of the membrane contactor A, and a shell side inlet of the membrane contactor A is connected with a liquid outlet pipeline of the supercharging device I;
the releasing unit comprises a releaser and a gas-liquid separating device, and the releaser is arranged in a cavity of the gas-liquid separating device;
a wastewater absorption unit comprising a membrane contactor B;
and the pH adjusting unit, the air dissolving unit, the releasing unit and the wastewater absorbing unit are sequentially connected along the wastewater flow direction.
2. The apparatus of claim 1,
the pH adjusting liquid storage container is connected with the supercharging device I, the shell pass outlet of the membrane contactor A is connected with the releaser, and the liquid outlet of the gas-liquid separation device is connected with the shell pass inlet of the membrane contactor B.
3. The apparatus of claim 1,
the wastewater absorption unit also comprises a pump I and an acid liquor storage tank, wherein a tube pass inlet of the membrane contactor B is connected with an outlet of the acid liquor storage tank through the pump I, a tube pass outlet of the membrane contactor B is connected with an inlet of the acid liquor storage tank through a pipeline, and the tube pass of the membrane contactor B contains acid liquor;
preferably, the membrane contactor a comprises a hollow fiber hydrophobic microporous membrane therein;
the material of the hollow fiber hydrophobic microporous membrane is selected from one of polypropylene, polytetrafluoroethylene, surface hydrophobic modified polypropylene and surface hydrophobic modified polytetrafluoroethylene;
the membrane porosity of the hollow fiber hydrophobic microporous membrane is 40-65%, and the average pore diameter is 0.02-0.25 μm.
4. The apparatus of claim 1, further comprising an ammonia preparation unit;
along the direction of the gas flow direction, the release unit, the ammonia water preparation unit and the gas dissolving unit are communicated in sequence;
the ammonia water preparation unit comprises a membrane contactor group and a water supply module; the membrane contactor group comprises N membrane contactors B, wherein N is more than or equal to 3;
a tube pass inlet of a 1 st membrane contactor B in the membrane contactor group is connected with a gas outlet pipeline of a gas-liquid separation device of the release unit, and a tube pass outlet of an Nth membrane contactor B is connected with a gas inlet of a pressurizing device II of the gas dissolving unit;
preferably, along the gas flow direction, the tube side outlet of the 1 st membrane contactor B is communicated with the tube side inlet of the 2 nd membrane contactor B, the tube sides of two adjacent membrane contactors B are communicated in sequence, and the tube side outlet of the N-1 st membrane contactor B is communicated with the tube side inlet of the Nth membrane contactor B;
the shell pass inlet of the Nth membrane contactor B is communicated with the water outlet of the water supply module, and sequentially, the shell passes of the two adjacent membrane contactors B are communicated, and the shell pass outlet of the (N-1) th membrane contactor B is communicated with the shell pass inlet of the Nth membrane contactor B.
5. The apparatus of claim 4,
the membrane contactor B comprises a hollow fiber hydrophobic microporous membrane;
the material of the hollow fiber hydrophobic microporous membrane is selected from one of polypropylene, polytetrafluoroethylene, surface hydrophobic modified polypropylene and surface hydrophobic modified polytetrafluoroethylene;
the membrane porosity of the hollow fiber hydrophobic microporous membrane is 35-55%, and the average pore diameter is 0.01-0.2 mu m;
the water supply module comprises a cooling component, a pump II and a liquid storage tank, and the shell pass inlet of the Nth membrane contactor B is sequentially connected with the cooling component, the pump II and the liquid storage tank through pipelines.
6. A method for treating high ammonia nitrogen wastewater is characterized in that the high ammonia nitrogen wastewater is treated by the device of any one of claims 1 to 5;
wherein the ammonia nitrogen content of the high ammonia nitrogen wastewater is not less than 3500ppm.
7. The processing method according to claim 6, comprising in particular the steps of:
(1) After passing through a pH adjusting liquid storage container, the high ammonia nitrogen wastewater enters a membrane contactor A through a supercharging device I and contacts with gas supercharged by a supercharging device II to form gas-dissolved water;
(2) Releasing the dissolved gas water formed in the step (1) into a gas-liquid separation device through a releaser to form micro bubbles, volatilizing gaseous ammonia from the wastewater to form a gas-phase component containing the gaseous ammonia and ammonia nitrogen wastewater I;
(3) And (3) enabling acid liquor in the acid liquor storage tank to enter a membrane contactor B in the wastewater absorption unit through a pump I, and enabling the ammonia nitrogen wastewater I formed in the step (2) to be in contact treatment with the acid liquor in the membrane contactor B.
8. The method of claim 7, wherein the pH adjusting reservoir contains a basic compound;
the alkaline compound is selected from NaOH, KOH, ca (OH) 2 At least one of;
the pH value of the wastewater discharged from the pH adjusting liquid storage container is 9-13;
preferably, the pH value of the wastewater discharged from the pH adjusting liquid storage container is 10-12.
9. The processing method according to claim 7, characterized in that: in the step (1), the step (c),
the gas is selected from at least one of air and nitrogen;
the pressure of the gas is 3-10 bar;
preferably, the pressure of the gas is between 5 and 8bar;
the contact time is 30 to 600s,
preferably, the contact time is 60 to 300s;
preferably, in the step (2),
the internal pressure of the gas-liquid separation device is 1-5 bar;
further preferably, the internal pressure of the gas-liquid separation device is 2 to 4bar;
the size of the micro bubbles is 10-200 mu m;
further preferably, the size of the fine bubbles is 30 to 100 μm.
Preferably, in the step (3), in the membrane contactor B, the pressure of one side for storing the ammonia nitrogen wastewater I is 0-0.5 bar, and the pressure of one side for storing the acid liquor is 0-0.5 bar;
the acid liquor is selected from one of phosphoric acid, sulfuric acid or hydrochloric acid;
the pH of the acid liquor is less than 3;
the ammonia nitrogen content of the treated wastewater is lower than 25ppm.
10. The process of claim 7, further comprising the steps of:
the gas phase component containing gaseous ammonia enters a membrane contactor B in the ammonia water preparation unit, pure water enters the membrane contactor B through a water supply module, the gas phase component and the pure water are in contact reaction to form ammonia water,
after contacting with pure water, the unreacted gas phase component enters a membrane contactor A through a supercharging device II;
preferably, the temperature of the pure water is 0-20 ℃;
further preferably, the temperature of the pure water is 1-10 ℃;
and the gas phase pressure in the membrane contactor B is 1-3 bar, the liquid phase pressure is 1.2-4 bar, and the liquid phase pressure is 0.2-1.0 bar higher than the gas phase pressure.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103331079A (en) * | 2013-07-10 | 2013-10-02 | 厦门市威士邦膜科技有限公司 | Membrane method ammonia gas treatment recovering apparatus and technology thereof |
| CN104817128A (en) * | 2015-04-17 | 2015-08-05 | 中国科学院生态环境研究中心 | Device and method for dissolved gas film deamination |
| GB201709366D0 (en) * | 2017-06-13 | 2017-07-26 | Univ Cranfield | Ammonia Seperation |
| CN110835187A (en) * | 2019-12-23 | 2020-02-25 | 上海凯鑫分离技术股份有限公司 | Ammonia nitrogen removal system and ammonia nitrogen removal process based on immersed membrane contactor |
| CN211255526U (en) * | 2019-11-21 | 2020-08-14 | 成都硕特环保科技有限公司 | Ammonia removal treatment system for ammonia nitrogen-containing wastewater |
| CN111892147A (en) * | 2020-08-25 | 2020-11-06 | 自然资源部天津海水淡化与综合利用研究所 | High ammonia-nitrogen wastewater system is handled to membrane contactor with resource recovery function |
| CN112624481A (en) * | 2021-01-11 | 2021-04-09 | 上海环保工程成套有限公司 | High ammonia-nitrogen wastewater deamination equipment and application method thereof |
| CN112875938A (en) * | 2021-04-01 | 2021-06-01 | 湖南中天元环境工程有限公司 | Ammonia nitrogen wastewater membrane absorption treatment device and method |
-
2021
- 2021-07-12 CN CN202110782922.2A patent/CN115611443A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103331079A (en) * | 2013-07-10 | 2013-10-02 | 厦门市威士邦膜科技有限公司 | Membrane method ammonia gas treatment recovering apparatus and technology thereof |
| CN104817128A (en) * | 2015-04-17 | 2015-08-05 | 中国科学院生态环境研究中心 | Device and method for dissolved gas film deamination |
| GB201709366D0 (en) * | 2017-06-13 | 2017-07-26 | Univ Cranfield | Ammonia Seperation |
| CN211255526U (en) * | 2019-11-21 | 2020-08-14 | 成都硕特环保科技有限公司 | Ammonia removal treatment system for ammonia nitrogen-containing wastewater |
| CN110835187A (en) * | 2019-12-23 | 2020-02-25 | 上海凯鑫分离技术股份有限公司 | Ammonia nitrogen removal system and ammonia nitrogen removal process based on immersed membrane contactor |
| CN111892147A (en) * | 2020-08-25 | 2020-11-06 | 自然资源部天津海水淡化与综合利用研究所 | High ammonia-nitrogen wastewater system is handled to membrane contactor with resource recovery function |
| CN112624481A (en) * | 2021-01-11 | 2021-04-09 | 上海环保工程成套有限公司 | High ammonia-nitrogen wastewater deamination equipment and application method thereof |
| CN112875938A (en) * | 2021-04-01 | 2021-06-01 | 湖南中天元环境工程有限公司 | Ammonia nitrogen wastewater membrane absorption treatment device and method |
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