CN110526320B - Aeration disc, gasification gray water comprehensive treatment device using same and treatment method - Google Patents
Aeration disc, gasification gray water comprehensive treatment device using same and treatment method Download PDFInfo
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- CN110526320B CN110526320B CN201910912842.7A CN201910912842A CN110526320B CN 110526320 B CN110526320 B CN 110526320B CN 201910912842 A CN201910912842 A CN 201910912842A CN 110526320 B CN110526320 B CN 110526320B
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- 238000005273 aeration Methods 0.000 title claims abstract description 299
- 239000010797 grey water Substances 0.000 title claims abstract description 170
- 238000002309 gasification Methods 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000009615 deamination Effects 0.000 claims abstract description 145
- 238000006481 deamination reaction Methods 0.000 claims abstract description 145
- 239000010802 sludge Substances 0.000 claims abstract description 69
- 239000003513 alkali Substances 0.000 claims abstract description 67
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 64
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 29
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 29
- 238000005352 clarification Methods 0.000 claims abstract description 26
- 239000007790 solid phase Substances 0.000 claims abstract description 25
- 239000010865 sewage Substances 0.000 claims abstract description 24
- 239000006228 supernatant Substances 0.000 claims abstract description 13
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 62
- 238000006243 chemical reaction Methods 0.000 claims description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 42
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 36
- 238000003825 pressing Methods 0.000 claims description 36
- 239000011259 mixed solution Substances 0.000 claims description 29
- 239000007789 gas Substances 0.000 claims description 23
- 239000000243 solution Substances 0.000 claims description 22
- 229910021529 ammonia Inorganic materials 0.000 claims description 18
- 239000011777 magnesium Substances 0.000 claims description 15
- 239000008394 flocculating agent Substances 0.000 claims description 14
- 239000007791 liquid phase Substances 0.000 claims description 12
- 238000005189 flocculation Methods 0.000 claims description 8
- 230000016615 flocculation Effects 0.000 claims description 8
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 7
- 229910052749 magnesium Inorganic materials 0.000 claims description 7
- 239000002244 precipitate Substances 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- 238000003672 processing method Methods 0.000 claims 1
- 238000009825 accumulation Methods 0.000 abstract description 4
- 238000013461 design Methods 0.000 abstract description 3
- 230000000052 comparative effect Effects 0.000 description 40
- 239000012634 fragment Substances 0.000 description 32
- 230000000694 effects Effects 0.000 description 17
- 230000006978 adaptation Effects 0.000 description 9
- 239000011575 calcium Substances 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 5
- 230000007547 defect Effects 0.000 description 4
- 239000013049 sediment Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 239000010866 blackwater Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- NKWPZUCBCARRDP-UHFFFAOYSA-L calcium bicarbonate Chemical compound [Ca+2].OC([O-])=O.OC([O-])=O NKWPZUCBCARRDP-UHFFFAOYSA-L 0.000 description 2
- 229910000020 calcium bicarbonate Inorganic materials 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- 244000025254 Cannabis sativa Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
Classifications
-
- 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
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust 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
- C02F1/52—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
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
-
- 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
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/586—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing ammoniacal nitrogen
-
- 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
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention belongs to an aeration disc, and a gasification gray water comprehensive treatment device and a treatment method using the same, wherein the gasification gray water comprehensive treatment device comprises a gasification gray water tank and a clarification tank, wherein the gasification gray water tank is connected with a hardness removal tank through an alkali liquor premixing unit and a deamination tank, and a supernatant outlet at the upper part of the hardness removal tank is connected with the clarification tank; the top of the deamination pool is connected with a torch device; the top of the hard removing tank is communicated with a flocculant storage tank; the solid phase outlets at the bottoms of the deamination tank and the hardness removal tank are respectively connected with a sludge treatment unit; the deamination pool and the hardness removal pool are communicated through a connecting pipeline; the bottom of the deamination tank and the bottom of the hardness removal tank are respectively provided with an aeration disc, the aeration disc in the deamination tank is connected with a compressed air storage tank, and the aeration disc in the hardness removal tank is connected with a carbon dioxide storage tank; the method has the advantages of reasonable flow design, capability of effectively removing 50% ammonia nitrogen content and 85% total hardness content in gasified grey water, effectively slowing down scaling of equipment and pipelines of the gasified grey water system, reducing ammonia nitrogen accumulation of the grey water system and reducing sewage terminal load.
Description
Technical Field
The invention belongs to an aeration disc, and a gasification grey water comprehensive treatment device and a treatment method using the aeration disc.
Background
The coal water slurry gasified grey water is water obtained by multi-stage flash evaporation, flocculation and clarification of black water, and is rich in a large amount of Ca 2+ 、 Mg 2+ The method comprises the steps of carrying out a first treatment on the surface of the In order to achieve the aim of saving water resources, a gasification gray water recycling mode is generally adopted, but a large amount of Ca exists 2+ And Mg (magnesium) 2+ The total hardness of the gasified grey water is continuously increased after repeated cyclic use, so that the risks of scaling and blockage of equipment and pipelines are increased, and in order to improve the cyclic use time of the gasified grey water, a general enterprise adopts a mode of adding a large amount of scale inhibition dispersing agent to maintain the stable operation of a gasified grey water system; however, the gasified grey water has high risk of scaling, and the gasified grey water must be discharged after long-time use, so that the discharged sewage has high ammonia nitrogen content and total hardness content, and the discharged pipeline is easy to be blocked, and the load of a sewage treatment terminal is increased.
The conventional methods for reducing the hardness of grey water at present are as follows: the electric flocculation method, the ion exchange resin method, the lime method and the like have the defect of high operation or maintenance cost; in addition, the accumulation of ammonia nitrogen in the grey water system still causes the problem of scaling of equipment such as a chilling chamber, a heat exchanger and the like due to the increase of the pH value of the black/grey water system; therefore, the gasification grey water system can achieve the purposes of recycling produced water and stably operating the system only by removing ammonia nitrogen while removing hardness and turbidity.
The ammonia nitrogen content removal mode in the gray water system at present is as follows: on the basis of removing hardness, ammonia nitrogen content in the grey water is removed by stirring and aeration, but the method can only remove 5% -10% of ammonia nitrogen content, has low ammonia nitrogen content removal efficiency, and cannot solve the problems of the rise of pH value of a black/grey water system, scaling of equipment such as a chilling chamber, a heat exchanger and the like; in addition, the process for removing the ammonia nitrogen in the sewage treatment industry mainly comprises a stripping process and an alkaline water washing process, but the process is not suitable for the stripping process because the temperature of the gray water is only 60-75 ℃; the gray water system has large water quantity and 400-600mg/L ammonia nitrogen content, and the alkaline water washing process needs to be specially provided with a water washing tower, is generally suitable for deamination of the conversion condensate with 5000-20000mg/L ammonia nitrogen content, has higher investment and operation and maintenance costs of the alkaline water washing process equipment, and is not suitable for gasifying the gray water system.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, and provides an aeration disc, a gasification grey water comprehensive treatment device and a treatment method using the aeration disc, which have reasonable flow design, can effectively remove 50% of ammonia nitrogen content and 85% of total hardness content in gasification grey water, effectively slow down scaling of gasification grey water system equipment and pipelines, reduce ammonia nitrogen accumulation of the grey water system and reduce sewage terminal load.
The purpose of the invention is realized in the following way:
an aeration disc comprises a main pipeline communicated with compressed gas, wherein the main pipeline is communicated with a branch pipeline, the branch pipeline is communicated with a plurality of branch pipelines, and a plurality of aeration holes are uniformly distributed on the branch pipelines; the aeration disc is arranged at the inner bottom of the reaction vessel, and the shape formed by the outer contour of the branch pipelines or the outer side ends of the plurality of branch pipelines is matched with the inner bottom of the reaction vessel; the aeration device is characterized in that a supporting rod is arranged on the inner side wall of the branch pipeline corresponding to the aeration hole, an aeration elastic sheet which is obliquely arranged is arranged on one side, close to the aeration hole, of the supporting rod, one end, connected with the supporting rod, of the aeration elastic sheet is arranged on the inner side of the branch pipeline, the other end of the aeration elastic sheet is arranged on the outer side of the branch pipeline, and the shape of the middle part of the aeration elastic sheet is matched with that of the aeration hole.
Preferably, the distance between the aeration disc and the inner bottom of the reaction vessel is 0.5-2m.
Preferably, the branch pipelines are a plurality of, which are respectively communicated with the main pipeline, and when the outer profile of the plurality of branch pipelines is matched with the inner bottom of the reaction vessel, the plurality of branch pipelines are arranged on the inner sides of the branch pipelines.
Preferably, the branched pipelines are respectively communicated with the main pipeline, and when the shape formed by the outer side end parts of the branched pipelines is matched with the inner bottom of the reaction vessel, the inner sides of the branched pipelines are respectively communicated with the outer sides of the branched pipelines.
Preferably, the aeration holes are round holes with the diameter of 8-10mm, and the distance between adjacent aeration holes is 10-15cm.
Preferably, the branch is arranged on the inner side wall of the branch pipe corresponding to the middle part of the aeration hole, the two sides of the branch are respectively provided with an aeration elastic sheet which is obliquely arranged, one end of the aeration elastic sheet connected with the branch is arranged on the inner side of the branch pipe, the other end of the aeration elastic sheet is arranged on the outer side of the branch pipe, and the shape of the middle part of the aeration elastic sheet is matched with the shape of the corresponding area of the aeration hole.
The gasification ash water comprehensive treatment device comprises a gasification ash water tank and a clarification tank, wherein the gasification ash water tank is connected with a hardness removal tank through an alkali liquor premixing unit and a deamination tank, and a supernatant outlet at the upper part of the hardness removal tank is connected with the clarification tank; the top of the deamination pool is connected with a torch device; the top of the hardness removal tank is communicated with a flocculant storage tank; the solid phase outlets at the bottoms of the deamination tank and the hardness removal tank are respectively connected with a sludge treatment unit; the middle part of the deamination tank is communicated with the middle part of the hardness removal tank through a connecting pipeline; the inner bottom of the deamination tank and the inner bottom of the hardness removal tank are respectively provided with the aeration disc, the main pipeline of the aeration disc in the deamination tank is connected with the compressed air storage tank, and the main pipeline of the aeration disc in the hardness removal tank is connected with the carbon dioxide storage tank.
Preferably, the alkali liquor premixing unit comprises a pipeline mixer arranged between the gasified ash water tank and the deamination tank, a first inlet of the pipeline mixer is connected with the gasified ash water tank, a second inlet of the pipeline mixer is connected with the alkali liquor storage tank through an alkali liquor pump, and an outlet of the pipeline mixer is connected with the deamination tank.
Preferably, the sludge treatment unit comprises a sludge pressing machine, the sludge pressing machine is respectively connected with the solid phase outlets at the bottoms of the deamination tank and the hardness removal tank through a sludge pump, the solid phase outlet of the sludge pressing machine is connected with the boiler furnace through a paste pump, and the liquid phase outlet of the sludge pressing machine is connected with the sewage terminal treatment device.
A treatment method of a gasification grey water comprehensive treatment device comprises the following steps:
step 1: the gasified ash water from the gasified ash water tank enters the pipeline mixer through a first inlet of the pipeline mixer, and alkali liquor in the alkali liquor storage tank enters the pipeline mixer through an alkali liquor pump and a second inlet of the pipeline mixer; the gasified grey water and the alkali liquor are uniformly mixed and then enter a deamination tank, and ammonia nitrogen in the gasified grey water can be converted into removable free ammonia by the gasified grey water and the alkali liquor; the temperature of the gasified grey water is as follows: 60-75 ℃, the hardness is: 1000-2000mg/L, ammonia nitrogen content 400-600mg/L; the alkali liquor is sodium hydroxide solution with the concentration of 30% -32%; the flow rate of the sodium hydroxide solution entering the pipeline mixer is 120-160L/h; the flow ratio of the gasified grey water to the sodium hydroxide solution is as follows: 1 m: 1.5-2L; the pH value of the gasified grey water mixed solution entering the deamination tank is as follows: 10.5-11.5;
Step 2: after the gasified grey water mixed solution in the step 1 enters the deamination tank, the compressed air storage tank supplies compressed air to the aeration disc through the main pipeline, the compressed air enters the deamination tank through the main pipeline, the branch pipelines and the aeration holes, and the compressed air is sent into the torch device for combustion after free ammonia in the grey water is carried out; the ammonia nitrogen content in the gasified grey water mixed solution can be reduced to 150-250mg/L by introducing compressed air into the deamination tank;
the compressed air pressure is: 0.4-0.6Mpa, the compressed air flow is: 210-400 m/h, the flow ratio between compressed air and gasified grey water mixture is 4-6:1.2-1.5;
when compressed air is introduced into the aeration disc, the compressed air pushes the aeration elastic sheet to move to the outer side of the branch pipeline, so that the compressed air enters the deamination tank; when compressed air is not introduced into the aeration disc, the gasified grey water mixed solution in the deamination tank pushes the aeration elastic sheet to move towards the direction of the branch pipeline, so that the inside of the aeration disc is isolated from the inside of the deamination tank; the distance between the aeration disc in the deamination tank and the bottom in the deamination tank is 0.5-1m;
step 3: the gasified grey water mixed solution in the deamination pool enters the hardness removal pool through a connecting pipeline and is led into Adding a flocculating agent PAC into the hardness removal tank through a flocculating agent storage tank, and simultaneously enabling compressed carbon dioxide gas in a carbon dioxide storage tank to supply the compressed carbon dioxide gas to an aeration disc in the hardness removal tank through a main pipeline, and enabling the compressed carbon dioxide gas to enter the hardness removal tank through the main pipeline, a branch pipeline and an aeration hole; carbon dioxide forms a large amount of HCO in alkaline environment 3 － And CO 3 2－ Which is compatible with Ca present in gasified grey water 2+ And Mg (magnesium) 2 Insoluble precipitate is formed, and flocculation sedimentation is carried out under the action of a flocculating agent PAC; the distance between the inner bottoms is 1-2m;
step 4: the gasified grey water passing through the hardness removal tank enters a clarification tank through a supernatant outlet at the upper part of the hardness removal tank, the pH value of the gasified grey water in the clarification tank is 7.8-8.5, the hardness is 100-300mg/L, and the ammonia nitrogen content is 150-250mg/L;
step 5: the sludge at the bottom of the deamination tank and the de-hardening tank respectively enter a sludge pump through the corresponding solid phase outlets, and are pressurized by the sludge pump and sent to a sludge pressing machine; mud paste generated by the mud pressing machine is pumped into a boiler hearth through a paste pump to be combusted; the water content of the mud paste is as follows: 50% -60%;
step 6: the sewage generated by the mud pressing machine is sent into a sewage terminal treatment device for advanced treatment through a liquid phase outlet of the mud pressing machine.
According to the aeration disc manufactured according to the scheme, the gasification grey water comprehensive treatment device and the treatment method using the aeration disc, the alkali liquor premixing unit is arranged, so that uniform mixing of the alkali liquor and the gasification grey water can be realized, a good foundation is laid for subsequent ammonia nitrogen removal, and the aeration disc has the characteristics of small occupied area, high mixing efficiency and no power; the aeration disc is arranged, so that the aeration efficiency can be effectively improved, and the gasified grey water and sludge are prevented from blocking the aeration holes; the aim of removing 50% ammonia nitrogen content in gasified grey water can be fulfilled by matching the alkali liquor premixing unit with the aeration disc; in addition, the total hardness content of 85% in gasified grey water can be removed by arranging the hardness removal tank and combining the aeration disc in the hardness removal tank with the flocculant; the aeration disc can be maximized by arranging the branch pipelines or the branch pipelines, and the aeration efficiency can be effectively improved by arranging the diameter of the aeration holes and the spacing between the aeration holes adjacent to the aeration holes; the aeration spring plate is arranged to realize automatic opening when compressed gas is introduced, and is automatically closed when the compressed gas is not introduced, so that gasified gray water and sludge are prevented from entering the branch pipeline or the sludge blocks the aeration hole or the branch pipeline; the method has the advantages of reasonable flow design, capability of effectively removing 50% ammonia nitrogen content and 85% total hardness content in gasified grey water, effectively slowing down scaling of equipment and pipelines of the gasified grey water system, reducing ammonia nitrogen accumulation of the grey water system and reducing sewage terminal load.
Drawings
FIG. 1 is a schematic view of the structure of an aeration disc according to the present invention.
FIG. 2 is another schematic structure of the aeration disc of the present invention.
FIG. 3 is a schematic structural view of an aeration hole and an aeration elastic sheet according to the present invention.
Fig. 4 is a schematic view of another structure of the aeration hole and the aeration elastic sheet of the present invention.
Fig. 5 is a schematic structural diagram of the aeration elastic sheet of the present invention when closed.
FIG. 6 is a schematic structural view of the gasification grey water comprehensive treatment device of the invention.
Detailed Description
For a clearer understanding of the technical features, objects and effects of the present invention, embodiments of the present invention will now be described with reference to the drawings, in which like reference numerals refer to like parts throughout the various views. For simplicity of the drawing, only the parts relevant to the invention are schematically shown in each drawing, and they do not represent the actual structure thereof as a product.
As shown in fig. 1-5, the invention relates to an aeration disc, and a gasification grey water comprehensive treatment device and a treatment method using the same, wherein the aeration disc comprises a main pipeline 1 communicated with compressed gas, the main pipeline 1 is communicated with a branch pipeline 2, the branch pipeline 2 is communicated with a plurality of branch pipelines 3, and a plurality of aeration holes 4 are uniformly distributed on the branch pipelines 3; the aeration disc is arranged at the inner bottom of the reaction vessel, and the outer contour of the branch pipeline 2 or the shape formed by the outer side ends of the plurality of branch pipelines 3 is matched with the inner bottom of the reaction vessel; be equipped with branch 5 on the corresponding lateral conduit 3 inside wall of aeration hole 4, the branch 5 is close to the aeration hole 4 one side and is equipped with the aeration shell fragment 6 that the slope set up, and the one end that aeration shell fragment 6 links to each other with branch 5 sets up in the inboard of lateral conduit 3, and the other end setting of aeration shell fragment 6 is in the outside of lateral conduit 3, and aeration shell fragment 6's middle part shape and aeration hole 4 looks adaptation. When the outer contour of the branch pipe 2 is matched with the inner bottom of the reaction vessel, the aeration disc is in a surrounding form, and the branch pipe 3 is arranged in the surrounding form; when the shape formed by the outer side ends of the plurality of branch pipes 3 is matched with the inner bottom of the reaction vessel, the aeration disc is open, the branch pipes 2 are arranged inside, and the plurality of branch pipes 3 are arranged outside the branch pipes 2, so that more gas and solution can be mixed when the aeration disc is aerated; because the area covered by the aeration disc is larger, when sediment is generated, the defect that the branch pipeline 3 or the aeration hole 4 is blocked is unavoidable, in order to overcome the defect, the invention is provided with related parts of the aeration elastic sheet 6, when the aeration elastic sheet 6 is arranged at the side part of the aeration hole 4, the support rod 5 can be fixedly connected with the branch pipeline 3 at the edge part of the aeration hole 4, so as to achieve the purpose of ensuring the support rod 5 to be fixed more firmly, at the moment, the aeration elastic sheet 6 is a piece, the shape of the aeration elastic sheet is consistent with the shape of the aeration hole 4, and the area of the aeration elastic sheet is not smaller than the area of the aeration hole 4. The distance between the aeration disc and the inner bottom of the reaction vessel is 0.5-2m. The distance between the aeration disc and the inner bottom of the reaction vessel is determined by the amount of sediment generated by the solution in the reaction vessel, and the aeration disc and the inner bottom of the reaction vessel are arranged at the position close to the inner bottom of the reaction vessel as much as possible when the amount of sediment is less, and the aeration disc and the inner bottom of the reaction vessel are arranged at the position far away from the inner bottom of the reaction vessel as much as possible when the amount of sediment is more; the aeration disc can make the solution more and more effectively contact the solution when it is disposed near the inner bottom of the reaction vessel, and can prevent the clogging of the branch pipe 3 or the aeration holes 4 by the precipitate when it is disposed far from the inner bottom of the reaction vessel. The branch pipelines 2 are respectively communicated with the main pipeline 1, and when the outer contours of the branch pipelines 2 are matched with the inner bottom of the reaction vessel, the branch pipelines 3 are arranged on the inner sides of the branch pipelines 2. The branch pipelines 2 are respectively communicated with the main pipeline 1, and when the shape formed by the outer side end parts of the plurality of branch pipelines 3 is matched with the inner bottom of the reaction vessel, the inner sides of the plurality of branch pipelines 3 are respectively communicated with the outer sides of the branch pipelines 2. The aeration holes 4 are round holes with the diameter of 8-10mm, and the distance between adjacent aeration holes 4 is 10-15cm. Through the arrangement, the aeration efficiency can be effectively improved. The branch 5 sets up on the corresponding lateral conduit 3 inside wall in aeration hole 4 middle part, and aeration shell fragment 6 that the slope set up are installed respectively to the both sides of branch 5, and aeration shell fragment 6 links to each other with branch 5 one end setting in lateral conduit 3, and aeration shell fragment 6's the other end setting is in lateral conduit 3's outside, and aeration shell fragment 6's middle part shape and the regional shape looks adaptation in aeration hole 4 correspondence. When the supporting rod 5 is arranged at the middle position of the aeration hole 4, the number of the aeration elastic sheets 6 is two, and at the moment, the shape of the aeration elastic sheets 6 is semicircle, and the shape of the aeration elastic sheets can be more matched with the aeration hole 4.
As shown in fig. 6, the gasification gray water comprehensive treatment device comprises a gasification gray water tank 7 and a clarification tank 12, wherein the gasification gray water tank 7 is connected with a hardness removal tank 15 through an alkali liquor premixing unit and a deamination tank 11, and a supernatant outlet at the upper part of the hardness removal tank 15 is connected with the clarification tank 12; the top of the deamination tank 11 is connected with a torch device 9; the top of the hardness removal tank 15 is communicated with the flocculant storage tank 10; the solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 are respectively connected with a sludge treatment unit; the middle part of the deamination tank 11 is communicated with the middle part of the hardness removal tank 15 through a connecting pipeline 19; the inner bottom of the deamination tank 11 and the inner bottom of the hardness removal tank 15 are respectively provided with the aeration disc, the main pipeline 1 of the aeration disc in the deamination tank 11 is connected with the compressed air storage tank 17, and the main pipeline 1 of the aeration disc in the hardness removal tank 15 is connected with the carbon dioxide storage tank 16. The alkali liquor premixing unit comprises a pipeline mixer 8 arranged between the gasified ash water tank 7 and the deamination tank 11, a first inlet of the pipeline mixer 8 is connected with the gasified ash water tank 7, a second inlet of the pipeline mixer 8 is connected with an alkali liquor storage tank 13 through an alkali liquor pump 14, and an outlet of the pipeline mixer 8 is connected with the deamination tank 11. The sludge treatment unit comprises a sludge pressing machine 21, the sludge pressing machine 21 is respectively connected with solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 through a sludge pump 20, the solid phase outlet of the sludge pressing machine 21 is connected with a boiler furnace 23 through a paste pump 22, and the liquid phase outlet of the sludge pressing machine 21 is connected with a sewage terminal treatment device 18.
A treatment method of a gasification grey water comprehensive treatment device comprises the following steps:
step 1: gasified ash water from the gasified ash water tank 7 enters the pipeline mixer 8 through a first inlet of the pipeline mixer 8, and alkali liquor in the alkali liquor storage tank 13 enters the pipeline mixer 8 through the alkali liquor pump 14 and a second inlet of the pipeline mixer 8; the gasified grey water and the alkali liquor are evenly mixed and then enter the deamination tank 11, and the gasified grey water and the alkali liquor can convert ammonia nitrogen in the gasified grey water into removable free ammonia; the temperature of the gasified grey water is as follows: 60-75 ℃, the hardness is: 1000-2000mg/L, ammonia nitrogen content 400-600mg/L; the alkali liquor is sodium hydroxide solution with the concentration of 30% -32%; the flow rate of the sodium hydroxide solution entering the pipeline mixer 8 is 120-160L/h; the flow ratio of the gasified grey water to the sodium hydroxide solution is as follows: 1 m: 1.5-2L; the pH value of the gasified grey water mixture entering the deamination tank 11 is as follows: 10.5-11.5;
step 2: after the gasified grey water mixed solution in the step 1 enters the deamination tank 11, the compressed air storage tank 17 supplies compressed air to the aeration disc through the main pipeline 1, the compressed air enters the deamination tank 11 through the main pipeline 1, the branch pipeline 2, the branch pipeline 3 and the aeration holes 4, and carries out free ammonia in the grey water and then sends the ammonia into the torch device 9 for combustion; the ammonia nitrogen content in the gasified grey water mixed solution can be reduced to 150-250mg/L by introducing compressed air into the deamination tank 11; the compressed air pressure is: 0.4-0.6Mpa, the compressed air flow is: the flow ratio between the compressed air and the gasified grey water mixed solution is 210-400 m/h: 4-6:1.2-1.5; when compressed air is introduced into the aeration disc, the compressed air pushes the aeration spring plate 6 to move to the outer side of the branch pipeline 3, so that the compressed air enters the deamination tank 11; when compressed air is not introduced into the aeration disc, the gasified grey water mixed liquid in the deamination tank 11 pushes the aeration elastic sheet 6 to move towards the direction of the branch pipeline 3, so that the interior of the aeration disc is isolated from the interior of the deamination tank 11; the distance between the aeration disc in the deamination tank 11 and the bottom in the deamination tank 11 is 0.5-1m;
Step 3: the gasified grey water mixed solution in the deamination tank 11 enters the hardness removal tank 15 through a connecting pipeline 19, a flocculating agent PAC is added into the hardness removal tank 15 through a flocculating agent storage tank 10, meanwhile, compressed carbon dioxide gas in a carbon dioxide storage tank 16 is supplied to an aeration disc in the hardness removal tank 15 through a main pipeline 1, and the compressed carbon dioxide gas enters the hardness removal tank 15 through the main pipeline 1, a branch pipeline 2, a branch pipeline 3 and an aeration hole 4; carbon dioxide forms a large amount of HCO in alkaline environment 3 － And CO 3 2－ Which is compatible with Ca present in gasified grey water 2+ And Mg (magnesium) 2 Insoluble precipitate is formed, and flocculation sedimentation is carried out under the action of a flocculating agent PAC; the distance between the inner bottoms is 1-2m;
step 4: the gasified grey water passing through the hardness removal tank 15 enters the clarification tank 12 through a supernatant outlet at the upper part of the hardness removal tank 15, the pH value of the gasified grey water in the clarification tank 12 is 7.8-8.5, the hardness is 100-300mg/L, and the ammonia nitrogen content is 150-250mg/L;
step 5: the sludge at the bottoms of the deamination tank 11 and the hardness removal tank 15 respectively enter a sludge pump 20 through the corresponding solid phase outlets, and are pressurized by the sludge pump 20 and sent to a sludge press 21; the mud paste generated by the mud pressing machine 21 is sent into a boiler hearth 23 to be burnt by a paste pump 22; the water content of the mud paste is as follows: 50% -60%;
Step 6: the sewage generated by the mud pump 21 is sent to the sewage terminal treatment device 18 for advanced treatment through the liquid phase outlet of the mud pump 21.
The invention will now be further illustrated with reference to examples for a more detailed explanation of the invention. Specific examples are as follows:
example 1
The aeration disc comprises a main pipeline 1 communicated with compressed gas, wherein the main pipeline 1 is communicated with a branch pipeline 2, the branch pipeline 2 is communicated with a plurality of branch pipelines 3, and a plurality of aeration holes 4 are uniformly distributed on the branch pipelines 3; the aeration disc is arranged at the inner bottom of the reaction vessel, and the outer contour of the branch pipeline 2 or the shape formed by the outer side ends of the plurality of branch pipelines 3 is matched with the inner bottom of the reaction vessel; be equipped with branch 5 on the corresponding lateral conduit 3 inside wall of aeration hole 4, the branch 5 is close to the aeration hole 4 one side and is equipped with the aeration shell fragment 6 that the slope set up, and the one end that aeration shell fragment 6 links to each other with branch 5 sets up in the inboard of lateral conduit 3, and the other end setting of aeration shell fragment 6 is in the outside of lateral conduit 3, and aeration shell fragment 6's middle part shape and aeration hole 4 looks adaptation. The distance between the aeration disc and the inner bottom of the reaction vessel is 0.5-2m. The aeration holes 4 are round holes with the diameter of 8-10mm, and the distance between adjacent aeration holes 4 is 10-15cm. The branch 5 sets up on the corresponding lateral conduit 3 inside wall in aeration hole 4 middle part, and aeration shell fragment 6 that the slope set up are installed respectively to the both sides of branch 5, and aeration shell fragment 6 links to each other with branch 5 one end setting in lateral conduit 3, and aeration shell fragment 6's the other end setting is in lateral conduit 3's outside, and aeration shell fragment 6's middle part shape and the regional shape looks adaptation in aeration hole 4 correspondence.
The gasification gray water comprehensive treatment device comprises a gasification gray water tank 7 and a clarification tank 12, wherein the gasification gray water tank 7 is connected with a hardness removal tank 15 through an alkali liquor premixing unit and a deamination tank 11, and a supernatant outlet at the upper part of the hardness removal tank 15 is connected with the clarification tank 12; the top of the deamination tank 11 is connected with a torch device 9; the top of the hardness removal tank 15 is communicated with the flocculant storage tank 10; the solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 are respectively connected with a sludge treatment unit; the middle part of the deamination tank 11 is communicated with the middle part of the hardness removal tank 15 through a connecting pipeline 19; the inner bottom of the deamination tank 11 and the inner bottom of the hardness removal tank 15 are respectively provided with the aeration disc, the main pipeline 1 of the aeration disc in the deamination tank 11 is connected with the compressed air storage tank 17, and the main pipeline 1 of the aeration disc in the hardness removal tank 15 is connected with the carbon dioxide storage tank 16. The alkali liquor premixing unit comprises a pipeline mixer 8 arranged between the gasified ash water tank 7 and the deamination tank 11, a first inlet of the pipeline mixer 8 is connected with the gasified ash water tank 7, a second inlet of the pipeline mixer 8 is connected with an alkali liquor storage tank 13 through an alkali liquor pump 14, and an outlet of the pipeline mixer 8 is connected with the deamination tank 11. The sludge treatment unit comprises a sludge pressing machine 21, the sludge pressing machine 21 is respectively connected with solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 through a sludge pump 20, the solid phase outlet of the sludge pressing machine 21 is connected with a boiler furnace 23 through a paste pump 22, and the liquid phase outlet of the sludge pressing machine 21 is connected with a sewage terminal treatment device 18.
A treatment method of a gasification grey water comprehensive treatment device comprises the following steps:
step 1: gasified ash water from the gasified ash water tank 7 enters the pipeline mixer 8 through a first inlet of the pipeline mixer 8, and alkali liquor in the alkali liquor storage tank 13 enters the pipeline mixer 8 through the alkali liquor pump 14 and a second inlet of the pipeline mixer 8; the gasified grey water and the alkali liquor are evenly mixed and then enter the deamination tank 11, and the gasified grey water and the alkali liquor can convert ammonia nitrogen in the gasified grey water into removable free ammonia; the temperature of the gasified grey water is as follows: 60 ℃, the hardness is: 1000mg/L and ammonia nitrogen content of 400mg/L; the alkali liquor is sodium hydroxide solution with the concentration of 30%; the flow rate of the sodium hydroxide solution entering the pipeline mixer 8 is 120L/h; the flow ratio of the gasified grey water to the sodium hydroxide solution is as follows: 1 m: 1.5L; the pH value of the gasified grey water mixture entering the deamination tank 11 is as follows: 10.5;
step 2: after the gasified grey water mixed solution in the step 1 enters the deamination tank 11, the compressed air storage tank 17 supplies compressed air to the aeration disc through the main pipeline 1, the compressed air enters the deamination tank 11 through the main pipeline 1, the branch pipeline 2, the branch pipeline 3 and the aeration holes 4, and carries out free ammonia in the grey water and then sends the ammonia into the torch device 9 for combustion; the ammonia nitrogen content in the gasified grey water mixed solution can be reduced to 150mg/L by introducing compressed air into the deamination tank 11; the compressed air pressure is: 0.4Mpa, compressed air flow is: 210m w/h, the flow ratio between the compressed air and the gasified grey water mixed solution is as follows: 4:1.2; when compressed air is introduced into the aeration disc, the compressed air pushes the aeration spring plate 6 to move to the outer side of the branch pipeline 3, so that the compressed air enters the deamination tank 11; when compressed air is not introduced into the aeration disc, the gasified grey water mixed liquid in the deamination tank 11 pushes the aeration elastic sheet 6 to move towards the direction of the branch pipeline 3, so that the interior of the aeration disc is isolated from the interior of the deamination tank 11; the distance between the aeration disc in the deamination tank 11 and the bottom in the deamination tank 11 is 0.5-1m;
Step 3: the gasified grey water mixed solution in the deamination tank 11 enters the hardness removal tank 15 through a connecting pipeline 19,adding a flocculating agent PAC into the hardness removal tank 15 through a flocculating agent storage tank 10, and simultaneously enabling compressed carbon dioxide gas in a carbon dioxide storage tank 16 to supply the compressed carbon dioxide gas to an aeration disc in the hardness removal tank 15 through a main pipeline 1, and enabling the compressed carbon dioxide gas to enter the hardness removal tank 15 through the main pipeline 1, a branch pipeline 2, a branch pipeline 3 and an aeration hole 4; carbon dioxide forms a large amount of HCO in alkaline environment 3 － And CO 3 2－ Which is compatible with Ca present in gasified grey water 2+ And Mg (magnesium) 2 Insoluble precipitate is formed, and flocculation sedimentation is carried out under the action of a flocculating agent PAC; the distance between the inner bottoms is 1-2m;
step 4: the gasified grey water passing through the hardness removal tank 15 enters the clarification tank 12 through a supernatant outlet at the upper part of the hardness removal tank 15, the pH value of the gasified grey water in the clarification tank 12 is 7.8, the hardness is 100mg/L, and the ammonia nitrogen content is 150mg/L;
step 5: the sludge at the bottoms of the deamination tank 11 and the hardness removal tank 15 respectively enter a sludge pump 20 through the corresponding solid phase outlets, and are pressurized by the sludge pump 20 and sent to a sludge press 21; the mud paste generated by the mud pressing machine 21 is sent into a boiler hearth 23 to be burnt by a paste pump 22; the water content of the mud paste is as follows: 50%;
Step 6: the sewage generated by the mud pump 21 is sent to the sewage terminal treatment device 18 for advanced treatment through the liquid phase outlet of the mud pump 21.
Example two
An aeration disc and a gasification grey water comprehensive treatment device and a treatment method using the same, wherein the aeration disc comprises a main pipeline 1 communicated with compressed gas, the main pipeline 1 is communicated with a branch pipeline 2, the branch pipeline 2 is communicated with a plurality of branch pipelines 3, and a plurality of aeration holes 4 are uniformly distributed on the branch pipelines 3; the aeration disc is arranged at the inner bottom of the reaction vessel, and the outer contour of the branch pipeline 2 or the shape formed by the outer side ends of the plurality of branch pipelines 3 is matched with the inner bottom of the reaction vessel; be equipped with branch 5 on the corresponding lateral conduit 3 inside wall of aeration hole 4, the branch 5 is close to the aeration hole 4 one side and is equipped with the aeration shell fragment 6 that the slope set up, and the one end that aeration shell fragment 6 links to each other with branch 5 sets up in the inboard of lateral conduit 3, and the other end setting of aeration shell fragment 6 is in the outside of lateral conduit 3, and aeration shell fragment 6's middle part shape and aeration hole 4 looks adaptation. The distance between the aeration disc and the inner bottom of the reaction vessel is 0.5-2m. The branch pipelines 2 are respectively communicated with the main pipeline 1, and when the shape formed by the outer side end parts of the plurality of branch pipelines 3 is matched with the inner bottom of the reaction vessel, the inner sides of the plurality of branch pipelines 3 are respectively communicated with the outer sides of the branch pipelines 2. The aeration holes 4 are round holes with the diameter of 8-10mm, and the distance between adjacent aeration holes 4 is 10-15cm. The branch 5 sets up on the corresponding lateral conduit 3 inside wall in aeration hole 4 middle part, and aeration shell fragment 6 that the slope set up are installed respectively to the both sides of branch 5, and aeration shell fragment 6 links to each other with branch 5 one end setting in lateral conduit 3, and aeration shell fragment 6's the other end setting is in lateral conduit 3's outside, and aeration shell fragment 6's middle part shape and the regional shape looks adaptation in aeration hole 4 correspondence.
The gasification gray water comprehensive treatment device comprises a gasification gray water tank 7 and a clarification tank 12, wherein the gasification gray water tank 7 is connected with a hardness removal tank 15 through an alkali liquor premixing unit and a deamination tank 11, and a supernatant outlet at the upper part of the hardness removal tank 15 is connected with the clarification tank 12; the top of the deamination tank 11 is connected with a torch device 9; the top of the hardness removal tank 15 is communicated with the flocculant storage tank 10; the solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 are respectively connected with a sludge treatment unit; the middle part of the deamination tank 11 is communicated with the middle part of the hardness removal tank 15 through a connecting pipeline 19; the inner bottom of the deamination tank 11 and the inner bottom of the hardness removal tank 15 are respectively provided with the aeration disc, the main pipeline 1 of the aeration disc in the deamination tank 11 is connected with the compressed air storage tank 17, and the main pipeline 1 of the aeration disc in the hardness removal tank 15 is connected with the carbon dioxide storage tank 16. The alkali liquor premixing unit comprises a pipeline mixer 8 arranged between the gasified ash water tank 7 and the deamination tank 11, a first inlet of the pipeline mixer 8 is connected with the gasified ash water tank 7, a second inlet of the pipeline mixer 8 is connected with an alkali liquor storage tank 13 through an alkali liquor pump 14, and an outlet of the pipeline mixer 8 is connected with the deamination tank 11. The sludge treatment unit comprises a sludge pressing machine 21, the sludge pressing machine 21 is respectively connected with solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 through a sludge pump 20, the solid phase outlet of the sludge pressing machine 21 is connected with a boiler furnace 23 through a paste pump 22, and the liquid phase outlet of the sludge pressing machine 21 is connected with a sewage terminal treatment device 18.
A treatment method of a gasification grey water comprehensive treatment device comprises the following steps:
step 1: gasified ash water from the gasified ash water tank 7 enters the pipeline mixer 8 through a first inlet of the pipeline mixer 8, and alkali liquor in the alkali liquor storage tank 13 enters the pipeline mixer 8 through the alkali liquor pump 14 and a second inlet of the pipeline mixer 8; the gasified grey water and the alkali liquor are evenly mixed and then enter the deamination tank 11, and the gasified grey water and the alkali liquor can convert ammonia nitrogen in the gasified grey water into removable free ammonia; the temperature of the gasified grey water is as follows: 75 ℃ and the hardness is: 2000mg/L and ammonia nitrogen content of 600mg/L; the alkali liquor is sodium hydroxide solution with the concentration of 32%; the flow rate of the sodium hydroxide solution entering the pipeline mixer 8 is 160L/h; the flow ratio of the gasified grey water to the sodium hydroxide solution is as follows: 2L of 1m grass; the pH value of the gasified grey water mixture entering the deamination tank 11 is as follows: 11.5;
step 2: after the gasified grey water mixed solution in the step 1 enters the deamination tank 11, the compressed air storage tank 17 supplies compressed air to the aeration disc through the main pipeline 1, the compressed air enters the deamination tank 11 through the main pipeline 1, the branch pipeline 2, the branch pipeline 3 and the aeration holes 4, and carries out free ammonia in the grey water and then sends the ammonia into the torch device 9 for combustion; the ammonia nitrogen content in the gasified grey water mixed solution can be reduced to 250mg/L by introducing compressed air into the deamination tank 11; the compressed air pressure is: 0.6Mpa, compressed air flow is: 400m w/h, the flow ratio between the compressed air and the gasified grey water mixed solution is as follows: 6:1.5; when compressed air is introduced into the aeration disc, the compressed air pushes the aeration spring plate 6 to move to the outer side of the branch pipeline 3, so that the compressed air enters the deamination tank 11; when compressed air is not introduced into the aeration disc, the gasified grey water mixed liquid in the deamination tank 11 pushes the aeration elastic sheet 6 to move towards the direction of the branch pipeline 3, so that the interior of the aeration disc is isolated from the interior of the deamination tank 11; the distance between the aeration disc in the deamination tank 11 and the bottom in the deamination tank 11 is 0.5-1m;
Step 3: the gasified grey water mixed solution in the deamination tank 11 enters into the de-hardening device through a connecting pipeline 19In the tank 15, adding a flocculating agent PAC into the hardness removal tank 15 through the flocculating agent storage tank 10, and simultaneously enabling the compressed carbon dioxide gas in the carbon dioxide storage tank 16 to supply the compressed carbon dioxide gas to an aeration disc in the hardness removal tank 15 through the main pipeline 1, and enabling the compressed carbon dioxide gas to enter the hardness removal tank 15 through the main pipeline 1, the branch pipeline 2, the branch pipeline 3 and the aeration holes 4; carbon dioxide forms a large amount of HCO in alkaline environment 3 － And CO 3 2－ Which is compatible with Ca present in gasified grey water 2+ And Mg (magnesium) 2 Insoluble precipitate is formed, and flocculation sedimentation is carried out under the action of a flocculating agent PAC; the distance between the inner bottoms is 1-2m;
step 4: the gasified grey water passing through the hardness removal tank 15 enters the clarification tank 12 through a supernatant outlet at the upper part of the hardness removal tank 15, the pH value of the gasified grey water in the clarification tank 12 is 8.5, the hardness is 300mg/L, and the ammonia nitrogen content is 250mg/L;
step 5: the sludge at the bottoms of the deamination tank 11 and the hardness removal tank 15 respectively enter a sludge pump 20 through the corresponding solid phase outlets, and are pressurized by the sludge pump 20 and sent to a sludge press 21; the mud paste generated by the mud pressing machine 21 is sent into a boiler hearth 23 to be burnt by a paste pump 22; the water content of the mud paste is as follows: 60 percent;
Step 6: the sewage generated by the mud pump 21 is sent to the sewage terminal treatment device 18 for advanced treatment through the liquid phase outlet of the mud pump 21.
Example III
An aeration disc and a gasification grey water comprehensive treatment device and a treatment method using the same, wherein the aeration disc comprises a main pipeline 1 communicated with compressed gas, the main pipeline 1 is communicated with a branch pipeline 2, the branch pipeline 2 is communicated with a plurality of branch pipelines 3, and a plurality of aeration holes 4 are uniformly distributed on the branch pipelines 3; the aeration disc is arranged at the inner bottom of the reaction vessel, and the outer contour of the branch pipeline 2 or the shape formed by the outer side ends of the plurality of branch pipelines 3 is matched with the inner bottom of the reaction vessel; be equipped with branch 5 on the corresponding lateral conduit 3 inside wall of aeration hole 4, the branch 5 is close to the aeration hole 4 one side and is equipped with the aeration shell fragment 6 that the slope set up, and the one end that aeration shell fragment 6 links to each other with branch 5 sets up in the inboard of lateral conduit 3, and the other end setting of aeration shell fragment 6 is in the outside of lateral conduit 3, and aeration shell fragment 6's middle part shape and aeration hole 4 looks adaptation. The distance between the aeration disc and the inner bottom of the reaction vessel is 0.5-2m. The branch pipelines 2 are respectively communicated with the main pipeline 1, and when the outer contours of the branch pipelines 2 are matched with the inner bottom of the reaction vessel, the branch pipelines 3 are arranged on the inner sides of the branch pipelines 2. The aeration holes 4 are round holes with the diameter of 8-10mm, and the distance between adjacent aeration holes 4 is 10-15cm. The branch 5 sets up on the corresponding lateral conduit 3 inside wall in aeration hole 4 middle part, and aeration shell fragment 6 that the slope set up are installed respectively to the both sides of branch 5, and aeration shell fragment 6 links to each other with branch 5 one end setting in lateral conduit 3, and aeration shell fragment 6's the other end setting is in lateral conduit 3's outside, and aeration shell fragment 6's middle part shape and the regional shape looks adaptation in aeration hole 4 correspondence.
The gasification gray water comprehensive treatment device comprises a gasification gray water tank 7 and a clarification tank 12, wherein the gasification gray water tank 7 is connected with a hardness removal tank 15 through an alkali liquor premixing unit and a deamination tank 11, and a supernatant outlet at the upper part of the hardness removal tank 15 is connected with the clarification tank 12; the top of the deamination tank 11 is connected with a torch device 9; the top of the hardness removal tank 15 is communicated with the flocculant storage tank 10; the solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 are respectively connected with a sludge treatment unit; the middle part of the deamination tank 11 is communicated with the middle part of the hardness removal tank 15 through a connecting pipeline 19; the inner bottom of the deamination tank 11 and the inner bottom of the hardness removal tank 15 are respectively provided with the aeration disc, the main pipeline 1 of the aeration disc in the deamination tank 11 is connected with the compressed air storage tank 17, and the main pipeline 1 of the aeration disc in the hardness removal tank 15 is connected with the carbon dioxide storage tank 16. The alkali liquor premixing unit comprises a pipeline mixer 8 arranged between the gasified ash water tank 7 and the deamination tank 11, a first inlet of the pipeline mixer 8 is connected with the gasified ash water tank 7, a second inlet of the pipeline mixer 8 is connected with an alkali liquor storage tank 13 through an alkali liquor pump 14, and an outlet of the pipeline mixer 8 is connected with the deamination tank 11. The sludge treatment unit comprises a sludge pressing machine 21, the sludge pressing machine 21 is respectively connected with solid phase outlets at the bottoms of the deamination tank 11 and the hardness removal tank 15 through a sludge pump 20, the solid phase outlet of the sludge pressing machine 21 is connected with a boiler furnace 23 through a paste pump 22, and the liquid phase outlet of the sludge pressing machine 21 is connected with a sewage terminal treatment device 18.
A treatment method of a gasification grey water comprehensive treatment device comprises the following steps:
step 1: gasified ash water from the gasified ash water tank 7 enters the pipeline mixer 8 through a first inlet of the pipeline mixer 8, and alkali liquor in the alkali liquor storage tank 13 enters the pipeline mixer 8 through the alkali liquor pump 14 and a second inlet of the pipeline mixer 8; the gasified grey water and the alkali liquor are evenly mixed and then enter the deamination tank 11, and the gasified grey water and the alkali liquor can convert ammonia nitrogen in the gasified grey water into removable free ammonia; the temperature of the gasified grey water is as follows: 67.5 ℃ and has the hardness of: 1500mg/L and ammonia nitrogen content of 500mg/L; the alkali liquor is sodium hydroxide solution with the concentration of 30% -32%; the flow rate of the sodium hydroxide solution entering the pipeline mixer 8 is 140L/h; the flow ratio of the gasified grey water to the sodium hydroxide solution is as follows: 1 m: 1.75L; the pH value of the gasified grey water mixture entering the deamination tank 11 is as follows: 11;
step 2: after the gasified grey water mixed solution in the step 1 enters the deamination tank 11, the compressed air storage tank 17 supplies compressed air to the aeration disc through the main pipeline 1, the compressed air enters the deamination tank 11 through the main pipeline 1, the branch pipeline 2, the branch pipeline 3 and the aeration holes 4, and carries out free ammonia in the grey water and then sends the ammonia into the torch device 9 for combustion; the ammonia nitrogen content in the gasified grey water mixed solution can be reduced to 200mg/L by introducing compressed air into the deamination tank 11; the compressed air pressure is: 0.5Mpa, compressed air flow is: 305 m/h, the flow ratio between the compressed air and the gasified grey water mixed solution is as follows: 5:1.35; when compressed air is introduced into the aeration disc, the compressed air pushes the aeration spring plate 6 to move to the outer side of the branch pipeline 3, so that the compressed air enters the deamination tank 11; when compressed air is not introduced into the aeration disc, the gasified grey water mixed liquid in the deamination tank 11 pushes the aeration elastic sheet 6 to move towards the direction of the branch pipeline 3, so that the interior of the aeration disc is isolated from the interior of the deamination tank 11; the distance between the aeration disc in the deamination tank 11 and the bottom in the deamination tank 11 is 0.5-1m;
Step 3: the gasified grey water mixed solution in the deamination tank 11 enters the de-hardening tank 15 through a connecting pipeline 19 and passes through a flocculationThe coagulant tank 10 adds the flocculant PAC into the hardness removal tank 15, and simultaneously, compressed carbon dioxide gas in the carbon dioxide tank 16 is supplied to an aeration disc in the hardness removal tank 15 through the main pipeline 1, and enters the hardness removal tank 15 through the main pipeline 1, the branch pipeline 2, the branch pipeline 3 and the aeration holes 4; carbon dioxide forms a large amount of HCO in alkaline environment 3 － And CO 3 2－ Which is compatible with Ca present in gasified grey water 2+ And Mg (magnesium) 2 Insoluble precipitate is formed, and flocculation sedimentation is carried out under the action of a flocculating agent PAC; the distance between the inner bottoms is 1-2m;
step 4: the gasified grey water passing through the hardness removal tank 15 enters the clarification tank 12 through a supernatant outlet at the upper part of the hardness removal tank 15, the pH value of the gasified grey water in the clarification tank 12 is 8.2, the hardness is 200mg/L, and the ammonia nitrogen content is 200mg/L;
step 5: the sludge at the bottoms of the deamination tank 11 and the hardness removal tank 15 respectively enter a sludge pump 20 through the corresponding solid phase outlets, and are pressurized by the sludge pump 20 and sent to a sludge press 21; the mud paste generated by the mud pressing machine 21 is sent into a boiler hearth 23 to be burnt by a paste pump 22; the water content of the mud paste is as follows: 55%;
Step 6: the sewage generated by the mud pump 21 is sent to the sewage terminal treatment device 18 for advanced treatment through the liquid phase outlet of the mud pump 21.
Experimental example
Randomly selecting two implementation modes as a first invention group of the invention.
Comparative example one: the lye premixing unit is not arranged, the lye storage tank 13 is directly connected with the deamination tank 11, and other arrangement and flow are consistent with those of the second embodiment.
Comparative example two: the pipeline mixer 8 is replaced by a stirring tank, alkali liquor and gasified grey water enter the stirring tank for mixing, the mixture is sent into the deamination tank 11 after 15 minutes at the working condition temperature, and other settings and processes are consistent with those of the second embodiment.
Comparative example three: the flow ratio between compressed air and gasified grey water mixed solution in the second step is as follows: 4.8:1.7; other arrangements and flows are consistent with the second embodiment.
Comparative example four: the flow ratio between compressed air and gasified grey water mixed solution in the second step is as follows: 6:2; other arrangements and flows are consistent with the second embodiment.
Comparative example five: the flow ratio between compressed air and gasified grey water mixed solution in the second step is as follows: 2.5:1, a step of; other arrangements and flows are consistent with the second embodiment.
Comparative example six: the flow ratio between compressed air and gasified grey water mixed solution in the second step is as follows: 3:1.5; other arrangements and flows are consistent with the second embodiment.
Comparative example seven: the aeration holes 4 in the deamination tank 11 are round holes with the diameter of 7mm, and the intervals between adjacent aeration holes 4 are 16cm; other arrangements and flows are consistent with the second embodiment.
Comparative example eight: the aeration holes 4 in the deamination tank 11 are round holes with the diameter of 11mm, and the intervals between adjacent aeration holes 4 are 9cm; other arrangements and flows are consistent with the second embodiment.
Comparative example nine: the aeration holes 4 in the deamination tank 11 are round holes with the diameter of 10mm, and the intervals between adjacent aeration holes 4 are 18cm; other arrangements and flows are consistent with the second embodiment.
Comparative example ten: the aeration disc in the deamination tank 11 is arranged at the inner bottom of the reaction vessel, the length of the branch pipeline 2 is one third of the length of the embodiment branch pipeline 2, and the length of the branch pipeline 3 is one half of the length of the embodiment branch pipeline 3; other arrangements and flows are consistent with the second embodiment.
Comparative example eleven: the aeration disc in the deamination pool 11 is arranged at the inner bottom of the reaction vessel, the length of the branch pipeline 2 is one half of the length of the embodiment branch pipeline 2, and the length of the branch pipeline 3 is identical to the length of the embodiment branch pipeline 3; other arrangements and flows are consistent with the second embodiment.
As can be seen from the comparison of the ammonia removal content of the first inventive group with comparative examples 1 to 11, the effect of example two is superior to comparative examples 1 to 11; see in particular the following table:
| Primary ammonia nitrogen content | Present ammonia nitrogen content | Analysis of causes | |
| First inventive group | 600mg/L | 250mg/L | |
| Comparative example one | 600mg/L | 542 mg/L | Uneven mixing of alkali liquor and grey water, partial alkaline grey water removing partial ammonia nitrogen |
| Comparative example two | 600mg/L | 285 mg/L | The alkali liquor and the ash water are mechanically mixed uniformly, and the hardness removing effect is close to that of the first invention group |
| Comparative example three | 600mg/L | 298 mg/L | The compressed air flow is small, and the air quantity per unit time and area is reduced |
| Comparative example four | 600mg/L | 324 mg/L | The compressed air flow is small, and the aeration effect is reduced |
| Comparative example five | 600mg/L | 413 mg/L | The compressed air flow is small, and the aeration effect is reduced |
| Comparative example six | 600mg/L | 502 mg/L | The compressed air flow is small, the aeration mixing effect is greatly reduced, and the content of the carried ammonia nitrogen is reduced |
| Comparative example seven | 600mg/L | 283 mg/L | The aeration holes are slightly smaller but the aeration arrangement interval is large, the aeration coverage is not uniform enough, and the ammonia nitrogen removal effect is reduced |
| Comparative example eight | 600mg/L | 268 mg/L | The aeration holes are slightly larger, the aeration flow speed is reduced, and the air distribution effect of the diversion of the aeration elastic sheet is weakened |
| Comparative example nine | 600mg/L | 277 mg/L | The aeration holes are arranged at larger intervals, so that the effect of air flow opposite flushing and scattering can not be achieved |
| Comparative example ten | 600mg/L | 425 mg/L | The aeration disc is smaller, the central part of the deamination tank is aerated, and the surrounding area has no aeration and deamination effects |
| Comparative example eleven | 600mg/L | 366 mg/L | The aeration disc is slightly smaller, the aeration area can not completely cover the deamination tank, and the partial area is alkaline but no air is used for removing ammonia nitrogen |
Summarizing: as can be seen from a comparison of the first inventive group with comparative examples 1-11, the pipe mixer 8 serves as a lye premixing unit for even distribution of the grey water and the lye and for better deamination by means of the deamination cell. The preferred flow ratio of compressed air to grey water is: 4-6:1.2-1.5, the aeration effect is reduced when the compressed air flow is reduced, so that the ammonia nitrogen content of the grey water is increased. The aeration disc, the aeration holes and the aeration hole intervals are reasonably arranged, so that a better air guiding and distributing effect can be achieved.
Experimental example 2
Three implementations were chosen as the second inventive set of the present invention.
Comparative example one: the hardness removal tank 15 is provided with a stirrer instead of a carbon dioxide aeration disc, and other settings and processes are consistent with those of the third embodiment.
Comparative example two: the aeration holes 4 in the hardness removal tank 15 are round holes with the diameter of 10mm, and the intervals between adjacent aeration holes 4 are 20cm; other settings and flows are consistent with embodiment three.
Comparative example three: the aeration holes 4 in the hardness removal tank 15 are round holes with the diameter of 5mm, and the intervals between adjacent aeration holes 4 are 12cm; other settings and flows are consistent with embodiment three.
Comparative example four: the aeration disc in the hard removing tank 15 is arranged at the inner bottom of the reaction vessel, the length of the branch pipeline 2 is one half of that of the embodiment trisection pipeline 2, and the length of the branch pipeline 3 is identical to that of the embodiment trisection pipeline 3; other settings and flows are consistent with embodiment three.
Comparative example five: the clarified Chi Huishui pH in step four was 7.4 and the other settings and schemes were consistent with example three.
Comparative example six: the clarified Chi Huishui pH in step four was 9.0 and the other settings and schemes were consistent with example three.
As can be seen from the comparison of the ammonia removal content of the above-described second inventive group with comparative examples 1 to 6, the effect of example III is superior to comparative examples 1 to 6; see in particular the following table:
| original hardness content | Present hardness content | Analysis of causes | |
| Second inventive group | 1500mg/L | 200mg/L | |
| Comparative example one | 1500mg/L | 1382 mg/L | Carbon dioxide-free, grey water system CO 3 2- Failure to meet hardness removal |
| Comparative example two | 1500mg/L | 502 mg/L | The aeration interval is larger, the reaction is uneven, and the effect of removing hardness is not generated locally |
| Comparative example three | 1500mg/L | 498 mg/L | The aeration holes are smaller, the aeration coverage area is reduced, and the hardness removal reaction is insufficient |
| Comparative example four | 1500mg/L | 665 mg/L | The aeration disc is smaller, the central part of the hard removing tank is aerated, and the surrounding area has no aeration and hard removing effect |
| Comparative example five | 1500mg/L | 956 mg/L | The pH is controlled to be low, aeration is neutral, and partial calcium bicarbonate is generated |
| Comparative example six | 1500mg/L | 477 mg/L | The pH control is higher, the alkalinity after aeration is stronger, and the residual part of OH - Does not participate in the reaction of removing hardness |
Summarizing: by comparing the second invention group with comparative examples 1 to 6, the aeration shape, aeration holes, etc. of the carbon dioxide aeration device affect the aeration effect, and thus the hardness removal effect. The pH value control of the aeration reaction affects the process of the hardness removal reaction, and the pH value range of 7.8-8.5 is the most suitable pH value range, and the hardness of part of calcium bicarbonate generated in the range is increased, and the hardness reduction is limited due to incomplete hardness removal reaction in the range.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "connected," "connected," and the like are to be construed broadly and may be, for example, fixedly connected, integrally connected, or detachably connected; or the communication between the two components is also possible; may be directly connected or indirectly connected through an intermediate medium, and the specific meaning of the above terms in the present invention will be understood by those skilled in the art according to the specific circumstances. The above examples are only specific to practical embodiments of the present invention, and they are not intended to limit the scope of the present invention, but all equivalent embodiments, modifications and adaptations without departing from the technical spirit of the present invention are intended to be included in the scope of the present invention.
Claims (6)
1. The utility model provides a gasification grey water integrated treatment device, includes gasification grey basin (7) and clarification tank (12), its characterized in that: the gasified ash water tank (7) is connected with the hard removing tank (15) through the alkali liquor premixing unit and the deamination tank (11) in sequence, and a supernatant outlet at the upper part of the hard removing tank (15) is connected with the clarifying tank (12);
the top of the deamination pool (11) is connected with a torch device (9);
The top of the hardness removal tank (15) is communicated with a flocculant storage tank (10);
the solid phase outlets at the bottoms of the deamination tank (11) and the hardness removal tank (15) are respectively connected with a sludge treatment unit;
the middle part of the deamination tank (11) is communicated with the middle part of the hardness removal tank (15) through a connecting pipeline (19);
the inner bottom of the deamination tank (11) and the inner bottom of the hardness removal tank (15) are respectively provided with an aeration disc, a main pipeline (1) of the aeration disc in the deamination tank (11) is connected with a compressed air storage tank (17), and a main pipeline (1) of the aeration disc in the hardness removal tank (15) is connected with a carbon dioxide storage tank (16);
the aeration disc comprises a main pipeline (1) communicated with compressed gas, the main pipeline (1) is communicated with a branch pipeline (2), the branch pipeline (2) is communicated with a plurality of branch pipelines (3), and a plurality of aeration holes (4) are uniformly distributed on the branch pipelines (3);
the aeration disc is arranged at the inner bottom of the reaction vessel, and the shape formed by the outer outline of the branch pipeline (2) or the outer end parts of the plurality of branch pipelines (3) is matched with the inner bottom of the reaction vessel;
a supporting rod (5) is arranged on the inner side wall of the branch pipeline (3) corresponding to the aeration hole (4), an aeration spring piece (6) which is obliquely arranged is arranged on one side, close to the aeration hole (4), of the supporting rod (5), one end, connected with the supporting rod (5), of the aeration spring piece (6) is arranged on the inner side of the branch pipeline (3), the other end of the aeration spring piece (6) is arranged on the outer side of the branch pipeline (3), and the middle shape of the aeration spring piece (6) is matched with the aeration hole (4);
The branch pipelines (2) are respectively communicated with the main pipeline (1), and when the outer profile of the branch pipelines (2) is matched with the inner bottom of the reaction container, the branch pipelines (3) are arranged on the inner sides of the branch pipelines (2);
the branch pipelines (2) are respectively communicated with the main pipeline (1), and when the shape formed by the outer side ends of the branch pipelines (3) is matched with the inner bottom of the reaction container, the inner sides of the branch pipelines (3) are respectively communicated with the outer sides of the branch pipelines (2);
the distance between the aeration disc and the inner bottom of the reaction vessel is 0.5-2m.
2. The gasification grey water integrated treatment device according to claim 1, wherein: the aeration holes (4) are round holes with the diameter of 8-10mm, and the distance between every two adjacent aeration holes (4) is 10-15cm.
3. The gasification grey water integrated treatment device according to claim 1, wherein: the branch (5) is arranged on the inner side wall of the branch pipe (3) corresponding to the middle part of the aeration hole (4), the two sides of the branch (5) are respectively provided with an aeration elastic sheet (6) which is obliquely arranged, one end of the aeration elastic sheet (6) connected with the branch (5) is arranged on the inner side of the branch pipe (3), the other end of the aeration elastic sheet (6) is arranged on the outer side of the branch pipe (3), and the shape of the middle part of the aeration elastic sheet (6) is matched with the shape of the corresponding area of the aeration hole (4).
4. The gasification grey water integrated treatment device according to claim 1, wherein: the alkali liquor premixing unit comprises a pipeline mixer (8) arranged between the gasified ash water tank (7) and the deamination tank (11), a first inlet of the pipeline mixer (8) is connected with the gasified ash water tank (7), a second inlet of the pipeline mixer (8) is connected with an alkali liquor storage tank (13) through an alkali liquor pump (14), and an outlet of the pipeline mixer (8) is connected with the deamination tank (11).
5. The gasification grey water integrated treatment device according to claim 4, wherein: the sludge treatment unit comprises a sludge pressing machine (21), the sludge pressing machine (21) is respectively connected with a solid-phase outlet at the bottom of the deamination pool (11) and the hardness removal pool (15) through a sludge pump (20), the solid-phase outlet of the sludge pressing machine (21) is connected with a boiler furnace (23) through a paste pump (22), and the liquid-phase outlet of the sludge pressing machine (21) is connected with a sewage terminal treatment device (18).
6. The treatment method of the gasification grey water integrated treatment apparatus according to claim 5, wherein: the processing method comprises the following steps:
step 1: the gasified grey water from the gasified grey water tank (7) enters the pipeline mixer (8) through a first inlet of the pipeline mixer (8), and the alkali liquor in the alkali liquor storage tank (13) enters the pipeline mixer (8) through the alkali liquor pump (14) and a second inlet of the pipeline mixer (8); the gasified grey water and the alkali liquor are evenly mixed and then enter a deamination tank (11), and the gasified grey water and the alkali liquor can convert ammonia nitrogen in the gasified grey water into removable free ammonia; the temperature of the gasified grey water is as follows: 60-75 ℃, the hardness is: 1000-2000mg/L, ammonia nitrogen content 400-600mg/L; the alkali liquor is sodium hydroxide solution with the concentration of 30% -32%; the flow rate of the sodium hydroxide solution entering the pipeline mixer (8) is 120-160L/h; the flow ratio of the gasified grey water to the sodium hydroxide solution is as follows: 1 m: 1.5-2L; the pH value of the gasified grey water mixed solution entering the deamination tank (11) is as follows: 10.5-11.5;
Step 2: after the gasified grey water mixed solution in the step 1 enters the deamination tank (11), compressed air is supplied to the aeration disc by the compressed air storage tank (17) through the main pipeline (1), and enters the deamination tank (11) through the main pipeline (1), the branch pipeline (2), the branch pipeline (3) and the aeration holes (4), and free ammonia in the grey water is carried out and then is sent into the torch device (9) for combustion; the ammonia nitrogen content in the gasified grey water mixed solution can be reduced to 150-250mg/L by introducing compressed air into the deamination tank (11);
the compressed air pressure is: 0.4-0.6Mpa, the compressed air flow is: the flow ratio between the compressed air and the gasified grey water mixed solution is 210-400 m/h: 4-6:1.2-1.5;
when compressed air is introduced into the aeration disc, the compressed air pushes the aeration elastic sheet (6) to move to the outer side of the branch pipeline (3), so that the compressed air enters the deamination tank (11); when compressed air is not introduced into the aeration disc, the gasified grey water mixed liquid in the deamination tank (11) pushes the aeration elastic sheet (6) to move towards the direction of the branch pipeline (3), so that the inside of the aeration disc is isolated from the inside of the deamination tank (11);
the distance between the aeration disc in the deamination tank (11) and the inner bottom of the deamination tank (11) is 0.5-1m;
Step 3: the gasified grey water mixed liquid in the deamination tank (11) enters the hardness removal tank (15) through a connecting pipeline (19), the flocculant PAC is added into the hardness removal tank (15) through a flocculant storage tank (10), meanwhile, compressed carbon dioxide gas in a carbon dioxide storage tank (16) is supplied to an aeration disc in the hardness removal tank (15) through a main pipeline (1), and the compressed carbon dioxide gas enters through the main pipeline (1), a branch pipeline (2), a branch pipeline (3) and an aeration hole (4)Entering a hard removing tank (15); carbon dioxide forms a large amount of HCO in alkaline environment 3 － And CO 3 2－ Which is compatible with Ca present in gasified grey water 2+ And Mg (magnesium) 2 Insoluble precipitate is formed, and flocculation sedimentation is carried out under the action of a flocculating agent PAC; the distance between the aeration disc in the hardness removal tank (15) and the inner bottom of the hardness removal tank (15) is 1-2m;
step 4: the gasified grey water passing through the hardness removal tank (15) enters a clarification tank (12) through a supernatant outlet at the upper part of the hardness removal tank (15), the pH value of the gasified grey water in the clarification tank (12) is 7.8-8.5, the hardness is 100-300mg/L, and the ammonia nitrogen content is 150-250mg/L;
step 5: sludge at the bottoms of the deamination tank (11) and the hardness removal tank (15) respectively enter a sludge pump (20) through corresponding solid phase outlets, and are pressurized by the sludge pump (20) and sent to a mud pressing machine (21); the mud produced by the mud pressing machine (21) is sent into a boiler furnace (23) to be burnt by a paste pump (22); the water content of the mud paste is as follows: 50% -60%;
Step 6: the sewage generated by the mud pressing machine (21) is sent into a sewage terminal treatment device (18) for advanced treatment through a liquid phase outlet of the mud pressing machine (21).
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