WO2018021840A1 - Compact advanced water treatment apparatus using sponge filter media - Google Patents
Compact advanced water treatment apparatus using sponge filter media Download PDFInfo
- Publication number
- WO2018021840A1 WO2018021840A1 PCT/KR2017/008080 KR2017008080W WO2018021840A1 WO 2018021840 A1 WO2018021840 A1 WO 2018021840A1 KR 2017008080 W KR2017008080 W KR 2017008080W WO 2018021840 A1 WO2018021840 A1 WO 2018021840A1
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- Prior art keywords
- tank
- water
- sponge filter
- unit
- denitrification
- Prior art date
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 100
- 239000010802 sludge Substances 0.000 claims abstract description 41
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 28
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 19
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000001914 filtration Methods 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 239000000126 substance Substances 0.000 claims abstract description 12
- 239000006228 supernatant Substances 0.000 claims abstract description 9
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 claims abstract description 7
- 230000000813 microbial effect Effects 0.000 claims abstract description 7
- 239000000356 contaminant Substances 0.000 claims abstract description 6
- 230000005484 gravity Effects 0.000 claims abstract description 6
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 25
- 244000005700 microbiome Species 0.000 claims description 15
- 238000005192 partition Methods 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 11
- 229910052760 oxygen Inorganic materials 0.000 claims description 11
- 239000001301 oxygen Substances 0.000 claims description 11
- 238000011001 backwashing Methods 0.000 claims description 10
- 230000008719 thickening Effects 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 7
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 6
- 229910052698 phosphorus Inorganic materials 0.000 claims description 6
- 239000011574 phosphorus Substances 0.000 claims description 6
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 238000012545 processing Methods 0.000 claims description 5
- 239000010865 sewage Substances 0.000 claims description 5
- 238000004140 cleaning Methods 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 3
- 229910002651 NO3 Inorganic materials 0.000 claims description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 2
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous oxide Inorganic materials [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims description 2
- 238000005507 spraying Methods 0.000 claims description 2
- 238000012805 post-processing Methods 0.000 claims 1
- 238000009434 installation Methods 0.000 abstract description 4
- 238000012423 maintenance Methods 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract 1
- 230000009467 reduction Effects 0.000 abstract 1
- 238000013461 design Methods 0.000 description 20
- 238000012552 review Methods 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000006185 dispersion Substances 0.000 description 5
- 239000011368 organic material Substances 0.000 description 5
- 239000012528 membrane Substances 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 238000011109 contamination Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 238000007664 blowing Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 2
- 230000001939 inductive effect Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- 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 1
- PETJYVUYQZFDRC-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+](O)=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+](O)=O.[NH6+3] PETJYVUYQZFDRC-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000001404 mediated effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- 238000005406 washing Methods 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
- B01D35/02—Filters adapted for location in special places, e.g. pipe-lines, pumps, stop-cocks
-
- 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
- C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/103—Textile-type packing
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/20—Activated sludge processes using diffusers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/10—Temperature conditions for biological treatment
- C02F2301/106—Thermophilic treatment
Definitions
- the present invention relates to an advanced water treatment apparatus, and more particularly, a sponge filter material that is smaller in size, easier to install, and easier to operate by achieving a structure that does not require internal transport and changes in supply of external carbon sources through a change in the overall apparatus. It is related with the compacted altitude water treatment apparatus used.
- the internal transport facility has a problem that the aerobic tank and the anaerobic tank have to be made larger due to the excessive consumption of energy to increase the overall operating cost as well as to increase the capacity of the internal transport.
- the supply of external carbon sources is expensive and can lead to the inability to use the extra organic materials available in existing installations.
- the membranes are frequently clogged by high sludge (MLSS) to prevent membranes ( mbrane) Cleaning and replacement costs and discontinuance of treatment are frequently occurring.
- the present invention uses high MLSS in the denitrification apparatus and does not need internal transport according to the treatment system, and it is composed of a structure capable of rapid sedimentation in the solid-liquid separator and can remove excess nitrogen.
- the purpose is to provide a compact environment-exchanging water treatment device whose overall size is reduced to 1/3 to 1/5 of the existing facilities.
- An aerobic tank and a sponge filter is installed: a sponge connected to the rear end of the aerobic tank and provided with a heating member for maintaining a proper temperature for smooth denitrification of nitrous nitrate nitrated in the aerobic tank with nitrogen gas and containing a microbial media therein.
- a denitrification unit provided with a filter medium and performing denitrification of the oxidized contaminated water; The treated water passing through the denitrification unit flows into the sludge with an upward flow to separate the solid-liquid separation by gravity, and a part of the supernatant is returned to the aerobic tank, and the rest is discharged to one outside, and the sludge remaining at the bottom is discharged to the outside.
- a final processing unit for post-treatment and final discharge of the supernatant flowing out from the solid-liquid separation unit; and a heating member is provided to dephosphorize the sludge flowing out of the solid-liquid separation unit, and a portion of the sludge is returned to the denitrification unit side as an external carbon source.
- a hydrasieve screen (hydrasieve screen) for removing fine suspended solids, etc.
- the exhalation tank is made of a multi-stage by the partition wall is formed with a plurality of apertures Sponges are stacked on each of the partition walls, and oxygen is supplied upwards from the bottom of the bottom through an diffuser, and the heating member of the denitrification unit is configured to control a temperature of 35 to 45 ° C.
- the denitrification part is provided with a backwash water spraying member for backwashing from the bottom upward to prevent clogging of the sponge filter material, and treated backwash water containing contaminants after cleaning is delivered to the aerobic tank.
- the solid-liquid separator is provided with a multi-stage partition inclined downward on the inner wall and the inner cylinder formed on the upper side of the center, and a scraper is provided on the lower side of the rotating central shaft passing through the center of the inner cylinder, the upper side contains a plurality of microbial media Consists of a double structure of the outer cylinder provided with a support bar, the contaminated water passing through the denitrification portion is gravity-strained from the upper direction of the inner cylinder to the lower direction is delivered to the bottom surface of the outer cylinder in a state in which the flow velocity is reduced by the multi-stage partition wall sludge Is stacked on the lower surface, the separated water is transferred upward from the outer cylinder bottom to be treated with contaminated water by the rotating bar.
- the post-treatment facility unit and a sponge filtration tank in which chemical treatment is performed due to chemical injection;
- a sponge filter member which is physically treated with a sponge filter member and activated carbon;
- a backwash water spray member which is mixed with water and air to be sprayed with backwash to clean the sponge filter member, wherein the sponge filter member is composed of a compressed sponge member and an activated carbon member attached to the back side thereof.
- a return line for conveying the backwash water injected and injected through the water jet member to the flow rate adjusting unit is further provided.
- the dephosphorization unit Concentrating tank for concentrating the sludge delivered from the solid-liquid separator;
- the concentrated sludge passed through the thickening tank is made of an anaerobic thickening tank equipped with a heating member to dephosphorize under anaerobic conditions, and the thickening tank is provided with a return line for returning the supernatant remaining after the concentration to the flow adjusting tank, and the anaerobic thickening tank
- the heating member is temperature controlled to 55 to 65 °C, so that a line for conveying a portion of the sludge to the denitrification unit is provided.
- the facility with the entire water treatment system can be easily manufactured and sold, and the entire facility can be assembled and assembled, it is sold as a single device produced at the factory, not as a facility installation industry where civil works and design construction are performed on the existing site. As it can be done, there is another effect that can be sold by mass production regardless of domestic and foreign locations.
- FIG. 1 is a view showing the entire system of a compact high water treatment apparatus according to a preferred embodiment of the present invention.
- FIG. 2 is a flow diagram showing the flow of the system according to FIG.
- FIG. 3 is a side view showing an aerobic tank according to a preferred embodiment of the present invention.
- Figure 4 is a side view showing a denitrification unit according to a preferred embodiment of the present invention
- Figure 5 is a plan view showing a solid-liquid separator in accordance with a preferred embodiment of the present invention.
- the present invention can be more compact in size of the aerobic tank by eliminating the internal transport consisting of an oxygen-free tank in the aerobic tank made in the conventional biological treatment device, and also to concentrate the carbon source required in the denitrification apparatus rather than an external source, or a portion of raw water It is possible to make the denitrification device compact by increasing the denitrification efficiency by maintaining the proper temperature through internal utilization using a part of the sludge, and the overall device becomes more compact by simplifying the arrangement and treatment of the entire group. It is reduced to the size of 1/5, but the main point is to improve the processing efficiency.
- the flow adjustment tank 100, the high-loss screen tank 200, the aerobic tank 300, the denitrification unit 400, the solid-liquid separator 500, the final processing unit 600 and the dephosphorization unit In the order of 700, the biological treatment is performed under the organic connection of each component.
- the flow rate adjusting tank 100 is for adjusting the amount of contaminated water introduced for smooth treatment in the exhalation tank 300 and the denitrification unit 400.
- the absolute amount of contamination and the degree of contamination vary depending on the season and the environment. Therefore, the amount of contaminated water to be treated and the degree of contamination should be controlled, so that the supernatant of the concentration tank 700a in the dephosphorization unit 700 to be described later and the backwash water of the sponge-mediated filtration water tank 600b of the final treatment unit 600 are flow rate adjusting tank 100. )). Since the backwash water of the concentration tank 700a and the filtered water tank 600b is contaminated water, the flow rate adjustment tank 100 having an appropriate concentration can be maintained.
- the contaminated water of the flow rate adjustment tank 100 to pass through the hydro screen 200 This is because the aerobic tank 300 and the denitrification unit 400 to be described later to use the sponge filter medium to have a compact structure in the present invention, if possible blockage to the suspended solids and various foreign matter sponge filter medium should be supplied. Therefore, in order to remove the fine suspended solids that are not filtered out of the previous wood and fine screen 20 is to install the hydro screen 200.
- the aerobic tank 300 is basically a compact structure, that is to be configured to a size of less than half the size of the conventional aerobic tank used.
- the basic reason possible with this size is that in the prior art, the internal transport is made from the aerobic tank to the anaerobic tank, so the capacity for such internal transport is required, but in the present invention, the internal transport is not necessary in the configuration of the entire apparatus. Therefore, it can have a smaller size, and also to make the configuration more compact in order to more faithfully perform the inherent function of the aerobic tank (300).
- the function of the aerobic tank 300 plays a role of inducing phosphorus (P) luxuriant uptake, inducing nitrification and oxidizing excess organic material using microorganisms.
- the aerobic tank 300 should be configured to supply dissolved oxygen smoothly even at high MLVSS maintenance and low water depth.
- a sponge 310 in which the microorganisms inhabit, and put it in the mesh 320 to be installed between the partition wall 330 having a plurality of through holes to be fixed in multiple stages.
- oxygen supplied from the bottom of the bottom through the diffuser penetrates into the sponge 310 and is efficiently supplied with oxygen, so that the residence time of oxygen is long and sufficiently dissolved.
- Oxygen leakage to the furnace has the effect of being able to fully utilize this even in a small amount of oxygen supply. Therefore, the loss of oxygen supplied to the aerobic tank 300 as much as possible and many microorganisms inhabit not only faster nitrification and organic matter oxidation than conventional treatment facilities, but also can save energy and economic benefits by eliminating the internal transport. In total, the experimental results show that water treatment can be carried out with the size of 30-50% of the treated volume, about 50% of the existing height (depth).
- the denitrification unit 400 serves to denitrify the nitric acid nitrate nitrogen in the aerobic tank 300 with nitrogen gas, so as to achieve a compact structure
- the denitrification unit 400 has the following structure.
- the heating member 410 is shown installed on one side of the lower side, but in addition to the structure having a heating line in the entire outer tube can be made in various ways. However, it may be sufficient to allow an appropriate temperature control of 40 ° C. according to seasonal changes such as summer and winter or the temperature of the introduced contaminated water. Since the temperature control adjustment is a known technique, a detailed description thereof will be omitted.
- the microorganisms are inhabited using the sponge filter 420 to maintain a high specific denitrification rate and maintain a high MLVSS, thereby achieving higher efficiency of the microorganisms.
- the conventional denitrification facility requires 7 ⁇ 7 m2 facility site on the basis of 200 ton treatment, but in the present invention, 2 ⁇ Since only 2 m 2 of land is required, a very compact structure can be achieved.
- the denitrification unit 400 in the present invention is provided with a configuration for backwashing to remove the blockage of the sponge filter medium 420, and the like.
- This backwashing process is performed by backwashing from the lower side to the upper side so that the cleaning of the sponge filter material 420 is performed, and the backwashing water generated by the backwashing process is transmitted to the aerobic tank 300 side described above.
- This is to be delivered to the aerobic tank 300 to maintain the high MLSS in the aerobic tank because the microorganisms are delivered from the aerobic tank 300 in the backwash water by the backwash process.
- the denitrification unit 400 is not supplied from an external carbon source, but is controlled by the anaerobic condensation member 720 that forms part of the dephosphorization part 700 so as to be connected to the dephosphorization part 700 which will be described later to receive a carbon source.
- the WRT denitrification system is installed at the rear of the aeration tank in the existing activated sludge biological treatment facility, and the HRT of the basic denitrification tank is at least 2 ⁇ 3hr, whereas the denitrification part is reduced to around 5 ⁇ 10min. have.
- the solid-liquid separator 500 serves to separate the sludge (sludge) and the treated water, the partition wall 512 in the inner cylinder 510 in the process of separating the sludge and the upper portion into the treated water in the configuration of the solid-liquid separator )
- the outer cylinder 520 is made of a double structure of the scraper 522 and the rotating bar 524. The flow of water is first transmitted from the outside of the contaminated water is delivered to the inner cylinder 510 side, and the delivered water is allowed to flow down slowly through the multi-stage partition wall 512 so that the solid liquid separation is sufficiently performed at the bottom. Sludge builds up on the bottom and the separated water is transported to the upper layer by the wall of the outer cylinder.
- the scraper 522 and the rotating bar 524 of the outer cylinder is configured to move slowly at the same or different speed, the reason is that the scraper 522 is stirred slowly and evenly distributed sludge, the rotating bar ( 524 is to remove nitrogen remaining in the water. That is, the inside of the rotating bar 524 is filled with microorganisms so that water is brought into contact with the stirring rotating bar 524 to remove nitrogen. Therefore, sludge dispersion is performed by the partition wall 512 structure of the inner cylinder 510 as a whole, and nitrogen is removed from the lower and middle layers more effectively by rising water upward toward the outer cylinder 520 so that solid-liquid separation can be achieved.
- the HRT of the existing facility is 3 to 4 hr
- the HRT is lowered to about 0.5 to 1 hr, so that the same effect can be achieved even if the size is reduced to a smaller size.
- the final treatment unit 600 is made of a wastewater treatment water filtration device using a sponge filter medium for the treatment of the extra SS, organic materials, nitrogen and phosphorus.
- the sponge filtration tank 610 uses chemicals to decompose the remaining microorganisms and organic substances, and then passes through a sponge filtration member 620 (WWAY) made of a sponge filter medium.
- WWAY sponge filtration member 620
- the sponge filtration member (WWAY) 620 is a final apparatus for treating what is not treated in biological and chemical treatment, and is a solid-liquid separator for treating PO4, SS, NH4, Fe, surfactants and other organic materials. Its structure is a sponge filter material is compressed, the rear end of the structure is filled with activated carbon. Therefore, the solid components are adsorbed while passing through the compressed sponge filter material, and then the contaminants are finally removed through the activated carbon. Water contaminated with these contaminants is discharged to the outside because it turns into water that meets environmental standards.
- the sponge filtration device (wway) 620 is to be backwashed from the bottom to the top to be washed to prevent the phenomenon such as clogging.
- decontamination of internal contaminants with backwashing water is not carried out, and the contaminated water and residual water are not discharged to the outside as it is. Return to).
- the sludge discharged from the solid-liquid separator 500 is delivered to a separate dephosphorization unit 700 to be treated.
- This concentrating device is to go through the two stages of the concentration tank 710 and anaerobic concentration member 720, the concentration tank 710 will be sufficient to use the conventionally used thickening tank 710.
- the supernatant after concentration in the concentration tank 710 is returned to the above-described flow rate adjustment tank 100.
- the sludge concentrated in the concentration tank 710 is delivered to the anaerobic thickening member 720, and anaerobic operation by having a heating member for maintaining the interior at 60 °C ⁇ 80 °C for rapid deoxygenation and anaerobic Make this easier. Due to the implementation of such a heating member, the size of the anaerobic concentration member 720 can also be reduced. In addition, since there are abundant carbon sources due to the decomposition of many organic substances in the anaerobic sludge, some of the sludge and some of the raw water are used as carbon sources of the denitrification unit 400. Therefore, as described above, the carbon source required by the denitrification unit 400 does not need to be separately introduced from the outside.
- Dispersion device DISK TYPE diffuser 0.12m3 / min ⁇ 4ea (0.48m3 / min)
- ⁇ is the efficiency of the pump
- the electric motor output of a pump shall be 0.75 Kw which is a standard specification.
- Air O 2 (kg / day) ⁇ 0.277 (kg O 2 / m3)
- Dispersing device DISK TYPE diffuser 0.12m3 / min ⁇ 12ea (1.44m3 / min)
- NO 3i is the incoming nitrate nitrogen (mg / l)
- V 180m3 / d ⁇ 24hr ⁇ 60min ⁇ 30min
- Sludge conveying pump (sedimentation tank ⁇ aerobic tank)
- Sludge transfer pump (sedimentation tank ⁇ concentration tank)
- Inner cylinder 1 set: ⁇ 350mm ⁇ H700mm
- Dispersion device DISK TYPE diffuser 0.12m3 / min ⁇ 1ea (0.12m3 / min)
- Dispersion device DISK TYPE diffuser 0.12m3 / min ⁇ 4ea (0.48m3 / min)
- the required carbon source in the denitrification zone is 38.03 mg / l.
- Dispersion device DISK TYPE diffuser 0.12m3 / min ⁇ 1ea (0.12m3 / min)
- Super water feed pump (anaerobic concentrator ⁇ flow tank): 20A-40A air-lift pump
- Blowing volume volume according to disk type diffuser 0.12m3 / min + air lift pump blowing volume
- Air lift pump 20A-40A Required air volume: 2 ⁇ 0.38m3 / min
- the present invention relates to a compact advanced water treatment apparatus using a sponge filter medium, which can be installed in an aerobic tank and a denitrification unit of a sewage treatment plant.
- the aerobic tank may be equipped with a sponge uptake containing microbial media such that luxury uptake of phosphorus-treated microorganisms, nitrification from ammonia nitrogen to nitrate nitrogen, and partial oxidation of the contained organic matter are performed.
- a sponge filter medium containing microbial media may be installed therein.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
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Abstract
The technical feature of the present invention is to provide a compact advanced water treatment apparatus using sponge filter media and comprising: a flow control tank for storing contaminated water, which flows in via a screen for filtering floating substances, at a predetermined concentration; an aerobic tank having, installed therein, a sponge filter medium containing microbial media for biologically treating the contaminated water transferred to the flow control tank; a denitrification unit which is provided with a heating member for maintaining an optimum temperature for smoothly reducing nitrate nitrogen, which has been nitrified in the aerobic tank, to nitrogen gas and is also provided with a sponge filter medium containing microbial media therein and denitrifies the oxidized contaminated water; a solid-liquid separation unit for carrying out solid-liquid separation by means of gravity as the water being treated and having passed through the denitrification unit flows in upwards together with sludge; a final treatment unit for post-treating a supernatant discharged outside from the solid-liquid separation unit and finally discharging same; and a dephosphorization unit which is provided with a heating member so as to dephosphorize the sludge discharged from the solid-liquid separation unit and returns a part of the sludge as an external carbon source towards the denitrification unit.Configured as such, the present invention treats a large number of contaminants on a significantly reduced scale in comparison with conventional facilities and thus generates a large number of economic benefits, such as reductions in a facility site, installation costs, and operation and maintenance costs.
Description
본 발명은 고도 수처리 장치에 관한 것으로, 보다 상세하게는 전체적인 장치의 변화를 통하여 내부반송이 필요 없으며 외부탄소원 공급이 없는 구조를 달성하여 보다 규모가 작고 설치가 용이하며 운영이 편리하도록 한 스펀지 여재를 이용한 컴팩트화 한 고도 수처리 장치에 관한 것이다. The present invention relates to an advanced water treatment apparatus, and more particularly, a sponge filter material that is smaller in size, easier to install, and easier to operate by achieving a structure that does not require internal transport and changes in supply of external carbon sources through a change in the overall apparatus. It is related with the compacted altitude water treatment apparatus used.
현재 대부분의 하폐수처리시설의 생물학적 고도수처리시설은 혐기조, 무산소조, 호기조 및 침전조를 갖추고 질소와 인을 제거하기 위하여 여러 가지 공법을 사용하고 있는 실정이다. 가장 기초적인 A2/O공법, UCT공법, 5 stage bardenpo공법, VIP공법 등은 기본적으로 탈질을 위하여 호기조에서 무산소조로 내부반송을 하거나 혹은 내부반송 없이 외부 탄소원을 일정 공급하여 호기조 후단에 탈질시설을 이루고 있다. 또한 침전조 없이 호기조에서 막(membrane)으로 처리수를 배출하는 시설 등 많은 공법들이 있다. 하지만 내부반송과 외부 탄소원 공급 및 막(membrane) 공법 등은 많은 문제점을 내포하고 있다. At present, most biological wastewater treatment facilities of sewage treatment facilities are equipped with anaerobic tanks, anaerobic tanks, aerobic tanks and sedimentation tanks, and various methods are used to remove nitrogen and phosphorus. The most basic A 2 / O method, UCT method, 5 stage bardenpo method, VIP method, etc. basically carry out internal return from an aerobic tank to an anoxic tank for denitrification, or supply an external carbon source without internal transport to provide a denitrification facility at the back of the aerobic tank. It is coming true. There are also many methods, such as a facility to discharge treated water from an aerobic tank to a membrane without a settling tank. However, internal conveyance, external carbon source supply, and membrane process have many problems.
즉, 내부반송시설은 에너지가 과다하게 소모되어 전체적인 운영비용을 증가시킬 뿐 아니라 이러한 내부반송에 의한 용량증가로 호기조 및 무산소조가 보다 크게 이루어져야 하는 문제점이 있다. 또한, 외부 탄소원 공급은 비용이 과다하게 소요되고 기존의 시설에서 이용할 수 있는 여분의 유기물을 이용하지 못하는 우를 범할 수 있으며, 막(membrane)은 높은 슬러지(MLSS)로 인하여 공극이 자주 막혀 막(mbrane) 청소 및 교체비용과 처리의 단절 현상이 자주 나타나고 있는 실정이다. In other words, the internal transport facility has a problem that the aerobic tank and the anaerobic tank have to be made larger due to the excessive consumption of energy to increase the overall operating cost as well as to increase the capacity of the internal transport. In addition, the supply of external carbon sources is expensive and can lead to the inability to use the extra organic materials available in existing installations. The membranes are frequently clogged by high sludge (MLSS) to prevent membranes ( mbrane) Cleaning and replacement costs and discontinuance of treatment are frequently occurring.
따라서 본 발명은 이러한 문제점을 해소하기 위하여 탈질장치에 높은 MLSS를 이용하고 처리 시스템에 따른 내부반송이 불필요하며, 고액분리장치에 급속침전이 가능한 구조로 구성하고 여분의 질소를 제거 할 수 있는 탈질처리시설을 갖추도록 하여 전체적인 규모가 기존의 시설규모보다 1/3 ~ 1/5정도로 축소된 컴팩트화 환 고도 수처리 장치를 제공하는데 그 목적이 있다.Therefore, in order to solve this problem, the present invention uses high MLSS in the denitrification apparatus and does not need internal transport according to the treatment system, and it is composed of a structure capable of rapid sedimentation in the solid-liquid separator and can remove excess nitrogen. The purpose is to provide a compact environment-exchanging water treatment device whose overall size is reduced to 1/3 to 1/5 of the existing facilities.
본 발명의 목적은 이상에서 언급한 목적으로 제한되지 않으며, 언급되지 않은 또 다른 목적들은 아래의 기재로부터 명확하게 이해될 수 있을 것이다The object of the present invention is not limited to the above-mentioned object, and other objects which are not mentioned will be clearly understood from the following description.
상기 목적을 달성하기 위한 본 발명에 따른 오염된 하폐수를 물리화학적 및 생물학적으로 처리하는 고도 수처리 장치는, 부유물질 등을 걸러내는 스크린을 거쳐 유입되는 오염수를 일정 농도로 저장하는 유량조정조와; 상기 유량조정조로 전달되는 오염수를 생물학적으로 처리하되, 인처리 미생물의 럭셔리 업테이크(luxury uptake), 암모니아성 질소에서 질산성질소로 질산화 및 함유된 유기물의 일정부분 산화가 이루어지도록 미생물미디어가 함유된 스폰지여재가 설치되는 호기조와: 상기 호기조 후단에 연결되고 상기 호기조에서 질산화된 질산헝질소를 질소가스로 원활한 탈질작용을 위한 적정온도를 유지하기 위한 히팅부재가 구비되고 내부에 미생물미디어가 함유된 스펀지여재가 구비되어 산화된 오염수의 탈질작용을 수행하는 탈질부와; 상기 탈질부를 통과한 처리수는 슬러지와 함께 상향류식으로 유입되어 중력으로 고액분리를 하며, 상등수의 일부는 상기 호기조로 반송하고, 나머지는 일측 외부로 유출하며, 하부에 남는 슬러지를 타측외부로 유출하는 침전식으로 이루어지는 고액분리부와; 상기 고액분리부에서 외부로 유출되는 상등수를 후처리하여 최종방류하는 최종처리부;그리고 상기 고액분리부에서 유출되는 슬러지를 탈인하도록 히팅부재가 구비되고, 슬러지의 일부를 외부탄소원으로 상기 탈질부측으로 반송하는 탈인부;를 포함하여 이루어지는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치를 제공하는데 그 기술적 특징이 있다.An advanced water treatment apparatus for physically and chemically treating contaminated sewage water according to the present invention for achieving the above object comprises: a flow rate adjustment tank for storing contaminated water introduced through a screen for filtering suspended solids and the like at a predetermined concentration; Biologically treating the contaminated water delivered to the flow rate adjustment tank, containing microorganism media such that luxury uptake of phosphorus-treated microorganisms, nitrification from ammonia nitrogen to nitrate nitrogen, and partial oxidation of organic matters are contained. An aerobic tank and a sponge filter is installed: a sponge connected to the rear end of the aerobic tank and provided with a heating member for maintaining a proper temperature for smooth denitrification of nitrous nitrate nitrated in the aerobic tank with nitrogen gas and containing a microbial media therein. A denitrification unit provided with a filter medium and performing denitrification of the oxidized contaminated water; The treated water passing through the denitrification unit flows into the sludge with an upward flow to separate the solid-liquid separation by gravity, and a part of the supernatant is returned to the aerobic tank, and the rest is discharged to one outside, and the sludge remaining at the bottom is discharged to the outside. And solid-liquid separation unit consisting of a precipitation; A final processing unit for post-treatment and final discharge of the supernatant flowing out from the solid-liquid separation unit; and a heating member is provided to dephosphorize the sludge flowing out of the solid-liquid separation unit, and a portion of the sludge is returned to the denitrification unit side as an external carbon source. There is a technical feature to provide a compact advanced water treatment apparatus using a sponge filter medium comprising a dephosphorization unit.
그리고 바람직 하기로는, 상기 유량조정조와 상기 호기조 사이에는 미세부유물질 등을 제거하기 위한 하이드라시브 스크린(hydrasieve screen)이 더 설치되고,상기 호기조는 내부가 다수개의 통공이 형성된 격벽에 의해 다단으로 이루어지고 상기 각 격벽상에 스폰지여재가 적층되어 이루어지고, 산기관을 통해 바닥 저부로 부터 상방향으로 산소가 공급되도록 하고, 상기 탈질부의 히팅부재는 35 내지 45℃의 온도조절이 이루어지도록 한다.And preferably, between the flow rate adjustment tank and the exhalation tank is further provided with a hydrasieve screen (hydrasieve screen) for removing fine suspended solids, etc. The exhalation tank is made of a multi-stage by the partition wall is formed with a plurality of apertures Sponges are stacked on each of the partition walls, and oxygen is supplied upwards from the bottom of the bottom through an diffuser, and the heating member of the denitrification unit is configured to control a temperature of 35 to 45 ° C.
더욱 바람직 하기로는 상기 탈질부에는 스펀지여재의 막힘 방지를 위해 하부로 부터 상방향으로 역세수 처리가 이루어지는 역세수분사부재가 구비되고, 청소후 오염물질을 함유하는 처리된 역세수는 상기 호기조로 전달되도록 한다.More preferably, the denitrification part is provided with a backwash water spraying member for backwashing from the bottom upward to prevent clogging of the sponge filter material, and treated backwash water containing contaminants after cleaning is delivered to the aerobic tank. Be sure to
또한, 상기 고액분리부는 내벽에 하향 경사지게 다단으로 격벽이 구비되어 중앙 상부측에 형성된 내통과, 내통의 중심을 관통하는 회전하는 중심축의 하부측에는 스크래퍼가 구비되고, 상부측에는 미생물미디어를 함유하는 다수개의 지지바가 구비된 외통의 2중구조로 이루어지고,탈질부를 통과한 오염수는 상기 내통의 상방향에서 하방향으로 중력식으로 정달되어 다단 격벽에 의해 유속이 저감된 상태로 상기 외통의 저면으로 전달되어 슬러지가 하부면에 쌓이도록 하고, 분리된 물은 외통저면에서 상방향으로 전달되면서 상기 회전바에 의해 오염수의 처리가 이루어지도록 한다.In addition, the solid-liquid separator is provided with a multi-stage partition inclined downward on the inner wall and the inner cylinder formed on the upper side of the center, and a scraper is provided on the lower side of the rotating central shaft passing through the center of the inner cylinder, the upper side contains a plurality of microbial media Consists of a double structure of the outer cylinder provided with a support bar, the contaminated water passing through the denitrification portion is gravity-strained from the upper direction of the inner cylinder to the lower direction is delivered to the bottom surface of the outer cylinder in a state in which the flow velocity is reduced by the multi-stage partition wall sludge Is stacked on the lower surface, the separated water is transferred upward from the outer cylinder bottom to be treated with contaminated water by the rotating bar.
상기 후처리시설부는,약품주입으로 인한 화학적 처리가 이루어지는 스펀지여과수조와; 스펀지여재와 활성탄으로 물리적 처리가 이루어지는 스펀지여재부재; 그리고 스펀지여재부재를 청소하도록 물과 공기가 혼합되어 역세로 분사되는 역세수분사부재;로 이루어지도록 하고,상기 스펀지여재부재는 압착된 스펀지부재와 이의 뒷면에 부착되는 활성탄부재로 이루어지고, 상기 역세수분사부재를 통해 분사되어 치리된 역세수를 상기 유량조정부로 반송되도로 하는 반송라인이 더 구비되도록 한다.The post-treatment facility unit, and a sponge filtration tank in which chemical treatment is performed due to chemical injection; A sponge filter member which is physically treated with a sponge filter member and activated carbon; And a backwash water spray member which is mixed with water and air to be sprayed with backwash to clean the sponge filter member, wherein the sponge filter member is composed of a compressed sponge member and an activated carbon member attached to the back side thereof. A return line for conveying the backwash water injected and injected through the water jet member to the flow rate adjusting unit is further provided.
상기 탈인부는,상기 고액분리부에서 전달된 슬러지를 농축하는 농축조와;The dephosphorization unit, Concentrating tank for concentrating the sludge delivered from the solid-liquid separator;
상기 농축조를 거쳐온 농축슬러지를 혐기조건하에서 탈인이 이루어지도록 히팅부재가 구비된 혐기성농축조로 이루어지며, 상기 농축조에는 농축후 남는 상등수를 상기 유량조정조로 반송하는 반송라인이 구비되고, 상기 혐기성 농축조의 히팅부재는 55 내지 65℃로 온도 조절이 이루어지고, 슬러지의 일부를 상기 탈질부로 반송하는 라인이 구비되도록 한다.The concentrated sludge passed through the thickening tank is made of an anaerobic thickening tank equipped with a heating member to dephosphorize under anaerobic conditions, and the thickening tank is provided with a return line for returning the supernatant remaining after the concentration to the flow adjusting tank, and the anaerobic thickening tank The heating member is temperature controlled to 55 to 65 ℃, so that a line for conveying a portion of the sludge to the denitrification unit is provided.
상기의 구성에 의한 본 발명은,The present invention by the above configuration,
기존시설에 비하여 대폭 축소된 규모에서 많은 오염물질을 처리함으로써 시설 부지의 경감 설치비의 경감 및 운영유지비의 경담 등 많은 경제적 이익이 발생하는 효과가 있다.By treating a lot of pollutants on a scale which has been greatly reduced compared to the existing facilities, there are many economic benefits such as reducing the installation cost of the facility and reducing the cost of operating maintenance.
또한, 전체적인 수처리 시스템을 갖춘 시설을 간편하게 제작하여 판매 할 수 있고 전체 시설을 집약하여 조립 할 수 있기 때문에 기존부지에 토목공사, 설계 시공 등이 이루어지는 시설 설치산업이 아니라 공장에서 생산되는 단일 장치로 판매 할 수 있으므로 국,내외의 장소의 구애없이 대량생산에 의한 판매가 가능한 다른 효과가 있다.In addition, since the facility with the entire water treatment system can be easily manufactured and sold, and the entire facility can be assembled and assembled, it is sold as a single device produced at the factory, not as a facility installation industry where civil works and design construction are performed on the existing site. As it can be done, there is another effect that can be sold by mass production regardless of domestic and foreign locations.
도 1은 본 발명의 바람직한 실시 예에 따른 컴팩트화 한 고도수처리 장치의 전체 시스템을 나타낸 도.1 is a view showing the entire system of a compact high water treatment apparatus according to a preferred embodiment of the present invention.
도 2는 도1에 의한 시스템의 흐름을 보여주는 플로우2 is a flow diagram showing the flow of the system according to FIG.
도 3은 본 발명의 바람직한 실시 예에 따른 호기조를 도시한 측면도3 is a side view showing an aerobic tank according to a preferred embodiment of the present invention
도 4는 본 발명의 바람직한 실시 예에 따른 탈질부를 도시한 측면도Figure 4 is a side view showing a denitrification unit according to a preferred embodiment of the present invention
도 5는 본 발명의 바람직한 실시 예에 따른 고액분리부를 도시한 평면도.Figure 5 is a plan view showing a solid-liquid separator in accordance with a preferred embodiment of the present invention.
본 발명은 기본적으로 종래 생물학적 처리장치에서 이루어지는 호기조에서 무산소조로 이루어지는 내부반송을 없앰으로써 호기조의 크기를 보다 컴팩트화 할 수 있으며, 또한, 탈질장치에서 필요로 하는 탄소원을 외부 공급원이 아닌 원수 일부 또는 농축슬러지 일부를 이용하는 내부 활용을 통하고 적정온도를 유지하여 탈질효율을 높임으로써 탈질장치의 컴팩트화가 가능하며, 전체적인, 각 조의 배치 및 처리를 보다 단순히 함으로써 전체 장치가 보다 컴팩트화 함으로써 기존 처리시설의 약 1/5의 크기로 축소되되, 처리효율이 보다 향상되도록 하는데 그 주안점이 있음을 알 수있다. The present invention can be more compact in size of the aerobic tank by eliminating the internal transport consisting of an oxygen-free tank in the aerobic tank made in the conventional biological treatment device, and also to concentrate the carbon source required in the denitrification apparatus rather than an external source, or a portion of raw water It is possible to make the denitrification device compact by increasing the denitrification efficiency by maintaining the proper temperature through internal utilization using a part of the sludge, and the overall device becomes more compact by simplifying the arrangement and treatment of the entire group. It is reduced to the size of 1/5, but the main point is to improve the processing efficiency.
이하에서는 이러한 본 발명의 바람직한 실시예에 따른 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치의 구성을 첨부한 도면을 참조하여 상세하게 설명하면 다음과 같다.Hereinafter, with reference to the accompanying drawings the configuration of a compact high water treatment apparatus using a sponge filter medium according to a preferred embodiment of the present invention will be described in detail as follows.
도1과 도2를 참조하여 전체적인 장치의 구성 및 플로우를 설명하기로 한다. 도시된 바와 같이, 외부에서 유입되며, 처리되어야 할 폐수(10)는 스크린조(20)를 거쳐 일차적으로 이물질을 걸러내며, 이러한 부분은 종래에서 사용되는 것과 동일하므로 이하 자세한 설명은 생략하기로 한다.1 and 2 will be described the configuration and flow of the overall apparatus. As shown, the wastewater 10 to be introduced from outside and to be treated is first filtered through the screen tank 20, and this part is the same as that used in the prior art, so the following detailed description will be omitted. .
본 발명에서는 종래의 배치와는 달리 크게 유량조정조(100), 하이즈로시브 스크린조(200), 호기조(300), 탈질부(400) 고액분리부(500), 최종처리부(600) 및 탈인부(700)의 순서로 이루어지며, 각 구성요소들의 유기적인 연결하에 생물학적 처리가 이루어지도록 한다.In the present invention, unlike the conventional arrangement, the flow adjustment tank 100, the high-loss screen tank 200, the aerobic tank 300, the denitrification unit 400, the solid-liquid separator 500, the final processing unit 600 and the dephosphorization unit In the order of 700, the biological treatment is performed under the organic connection of each component.
유량조정조(100)는 호기조(300) 및 탈질부(400)에서 원활한 처리를 위하여 투입되는 오염수의 양을 조절하기 위한것이다. 통상적으로 계절 및 환경에 따라 유입되는 폐수의 절대적인 양 및 오염정도는 다르다. 따라서 처리되는 오염수의 양 및 오염정도를 조절되어야 하므로 후술되는 탈인부(700)중 농축조(700a)의 상등수와 최종처리부(600)중 스펀지여재 여과수조(600b)의 역세수를 유량조정조(100)에 연결되도록 한다. 이러한 농축조(700a)와 여과수조(600b)의 역세수는 오염처리된 수 이므로 적정 농도를 가지는 유량조정조(100)를 유지할 수가 있다.The flow rate adjusting tank 100 is for adjusting the amount of contaminated water introduced for smooth treatment in the exhalation tank 300 and the denitrification unit 400. Typically, the absolute amount of contamination and the degree of contamination vary depending on the season and the environment. Therefore, the amount of contaminated water to be treated and the degree of contamination should be controlled, so that the supernatant of the concentration tank 700a in the dephosphorization unit 700 to be described later and the backwash water of the sponge-mediated filtration water tank 600b of the final treatment unit 600 are flow rate adjusting tank 100. )). Since the backwash water of the concentration tank 700a and the filtered water tank 600b is contaminated water, the flow rate adjustment tank 100 having an appropriate concentration can be maintained.
다음, 이러한 유량조정조(100)의 오염수는 하이드로시브 스크린(200)을 거치도록 한다. 이는 후술하는 호기조(300) 및 탈질부(400)은 본 발명에서 컴팩트한 구조를 가지도록 스펀지 여재를 이용하게 되므로 가능하면 부유물질 및 각종 이물질 스펀지 여재에 막힘이 제거되어 공급되어야 한다. 따라서 이전의 조목 및 세목 스크린(20)에서 걸러지지 않은 미세한 부유물질 까지 제거하기 위하여 하이드로시브 스크린(200)을 설치하는 것이다.Next, the contaminated water of the flow rate adjustment tank 100 to pass through the hydro screen 200. This is because the aerobic tank 300 and the denitrification unit 400 to be described later to use the sponge filter medium to have a compact structure in the present invention, if possible blockage to the suspended solids and various foreign matter sponge filter medium should be supplied. Therefore, in order to remove the fine suspended solids that are not filtered out of the previous wood and fine screen 20 is to install the hydro screen 200.
다음은 도 3을 참조하여 호기조(300)의 구조 및 기능을 설명하기로 한다. 본 발명에서 호기조(300)는 기본적으로 컴팩트한 구조 즉, 종래 사용되는 호기조의 크기보다 절반 이하의 크기로 구성되도록 한다. 이러한 크기로 가능한 기본적인 이유는 종래에서는 호기조에서 무산소조로 내부반송이 이루어지므로 이러한 내부반송을 위한 용량이 필요하나, 본 발명에서는 전체 장치의 구성에서 내부반송이 필요없어지게 된다. 따라서 보다 적은 크기를 가질 수 있으며, 또한, 호기조(300)의 고유의 기능을 보다 충실히 이루어지도록 하기 위하여 구성을 보다 컴팩트화 하게 이루어지도록 한다. Next, the structure and function of the aerobic tank 300 will be described with reference to FIG. 3. In the present invention, the aerobic tank 300 is basically a compact structure, that is to be configured to a size of less than half the size of the conventional aerobic tank used. The basic reason possible with this size is that in the prior art, the internal transport is made from the aerobic tank to the anaerobic tank, so the capacity for such internal transport is required, but in the present invention, the internal transport is not necessary in the configuration of the entire apparatus. Therefore, it can have a smaller size, and also to make the configuration more compact in order to more faithfully perform the inherent function of the aerobic tank (300).
즉, 호기조(300)의 기능은 미생물을 이용하여 오염원인 인(P) 럭서려 업테이크(luxury uptake)를 유도하고 질산화를 유도하며 여분의 유기물질을 산화시키는 역활을 한다. 크기가 컴팩트화 하기 위해서 호기조(300)의 구성은 높은 MLVSS 유지와 낮은 수심에서도 용존산소의 공급이 원활하여야 하며, 많은 미생물이 서식하도록 함으로써 질산화와 유기물의 산화를 신속하게 이루어 지도록 하여야 한다. 이를 위해서 도3에 도시된 바와 같이, 미생물이 서식하는 스펀지(310)를 준비하고, 이를 그물망(320)에 넣어서 다수개의 통공이 구비된 격벽(330) 사이사이에 설치하여 다단으로 고정되도록 한다. 이럴 경우 산기관(미도시)를 통해 저면 바닥에서 공급되는 산소는 스펀지(310)내부에 스며들어 산소가 효율적으로 공급되어 산소의 체류시간이 길어져 충분히 용해되며, 이는 미생물이 충분히 활용가능하고 또한 외부로의 산소유출이 방지되는 효과를 가지므로 적은 양의 산소 공급에도 이를 충분히 활용할 수 있게 되는 잇점이 있다. 따라서 호기조(300)로 공급되는 산소의 손실을 최대한 줄이고 많은 미생물이 서식하여 기존 처리시설보다 질산화와 유기물 산화를 신속하게 이루어 질 뿐만 아니라, 내부반송의 생략으로 에너지절약과 경제적 이익을 초래할 수 있다. 전체적으로 기존의 높이(수심)보다 50%정도로 처리물량대비 30 ~ 50%정도의 크기로도 수처리가 가능함을 실험결과 알 수 있었다.That is, the function of the aerobic tank 300 plays a role of inducing phosphorus (P) luxuriant uptake, inducing nitrification and oxidizing excess organic material using microorganisms. In order to make the size compact, the aerobic tank 300 should be configured to supply dissolved oxygen smoothly even at high MLVSS maintenance and low water depth. To this end, as shown in Figure 3, to prepare a sponge 310 in which the microorganisms inhabit, and put it in the mesh 320 to be installed between the partition wall 330 having a plurality of through holes to be fixed in multiple stages. In this case, oxygen supplied from the bottom of the bottom through the diffuser (not shown) penetrates into the sponge 310 and is efficiently supplied with oxygen, so that the residence time of oxygen is long and sufficiently dissolved. Oxygen leakage to the furnace has the effect of being able to fully utilize this even in a small amount of oxygen supply. Therefore, the loss of oxygen supplied to the aerobic tank 300 as much as possible and many microorganisms inhabit not only faster nitrification and organic matter oxidation than conventional treatment facilities, but also can save energy and economic benefits by eliminating the internal transport. In total, the experimental results show that water treatment can be carried out with the size of 30-50% of the treated volume, about 50% of the existing height (depth).
다음 도시한 도4를 참조하여 탈질부(400)을 설명하기로 한다. 탈질부(400)은 상술한 호기조(300)에서 질산화된 질산성질소를 질소가스로 탈질 역할을 수행하는 것으로서, 컴팩트한 구조를 달성하기 위해서는 다음과 같은 구조를 가지도록 한다. 먼저, 첫째, 종래에서와 달리 내부반송이 없으므로 그 만큼 크기가 적어지며, 둘째, 탈질의 효율을 증대시키기 위하여 수온을 40℃내외로 유지시키는 히팅(heating)부재(410)을 구비하도록 한다. 실험에 따르면, 미생물의 탈질작용은 40℃ 내외가 가장 활발하므로 이를 위해 히팅부재(410)을 구비하도록 한다. 도시된 도면상에서는 하부 일측에 히팅부재(410)가 설치된 것으로 나타나나, 이 이외에도 외통 전체에 히팅선을 구비하는 구조 등 다양하게 이루어질 수 있다. 다만, 여름 및 겨울과 같은 계절변화 또는 유입되는 오염수의 온도에 따라 적정한 40℃의 온도제어가 가능하도록 하면 족할 것이다. 이러한 온도제어 조절은 공지기술이므로 이하 자세한 설명은 생략하기로 한다. Next, the denitrification unit 400 will be described with reference to FIG. 4. The denitrification unit 400 serves to denitrify the nitric acid nitrate nitrogen in the aerobic tank 300 with nitrogen gas, so as to achieve a compact structure, the denitrification unit 400 has the following structure. First, since there is no internal transport unlike in the prior art, the size is reduced by that, and second, to provide a heating member 410 for maintaining the water temperature to about 40 ℃ to increase the efficiency of denitrification. According to the experiment, since the denitrification of the microorganism is most active around 40 ° C to provide a heating member 410 for this. In the illustrated figure, the heating member 410 is shown installed on one side of the lower side, but in addition to the structure having a heating line in the entire outer tube can be made in various ways. However, it may be sufficient to allow an appropriate temperature control of 40 ° C. according to seasonal changes such as summer and winter or the temperature of the introduced contaminated water. Since the temperature control adjustment is a known technique, a detailed description thereof will be omitted.
또한, 셋째, 비(specific)탈질율이 높은 상태를 유지시키고 높은 MLVSS를 유지시키도록 스폰지여재(420)를 이용하여 미생물이 서식하도록 함으로써 미생물의 보다 높은 효율성이 이루어지도록 한다. 상기와 같이, 세가지 기본요인으로 탈질장치를 구성시 본 발명자들의 실험 및 테스트에 따르면, 200톤 처리기준으로 종래 탈질시설의 구비는 7×7 ㎡의 시설부지를 필요로 하나, 본 발명에서는 2×2 ㎡의 부지만 필요하므로 매우 컴팩트한 구조를 달성할 수 있다. Third, the microorganisms are inhabited using the sponge filter 420 to maintain a high specific denitrification rate and maintain a high MLVSS, thereby achieving higher efficiency of the microorganisms. As described above, according to the experiments and tests of the present inventors when constructing the denitrification apparatus with three basic factors, the conventional denitrification facility requires 7 × 7 ㎡ facility site on the basis of 200 ton treatment, but in the present invention, 2 × Since only 2 m 2 of land is required, a very compact structure can be achieved.
또한, 본 발명에서 탈질부(400)에서는 스폰지여재(420)의 막힘현상 등을 제거하기 위하여 역세처리를 위한 구성이 구비된다. 이러한 역세처리는 하부에서 상부측으로 역세처리를 행함으로써 스폰지여재(420)의 청소가 이루어지도록 하며, 이러한 역세처리에 의해 발생한 역세수는 상술한 호기조(300)측으로 전달되도록 한다. 이는 역세처리에 의한 역세수에는 호기조(300)에서 전달되 미생물들이 서식하고 있으므로 호기조에서 높은 MLSS를 유지할 수 있도록 호기조(300)측으로 전달되도록 하는 것이다. 또한 탈질부(400)은 외부 탄소원의 공급이 아니라 자제척은 탄소원을 공급 받을 수 있도록 후술하는 탈인부(700)과 연결되도록 하여 탈인부(700)의 일부를 이루는 혐기성농축부재(720)에서 생성된 유기물질과 일부 원수를 carbon source로 이용하도록 한다. 상기와 같은 시설로 구성하여 기존의 활성슬러지 생물학적처리 시설에서 폭기조 후단에 WWAY 탈질장치를 설치하여 기본 탈질조의 HRT가 최소 2 ~ 3hr인데 반하여 본 탈질부는 HRT 5 ~ 10min 내외로 줄어들어 보다 효과적임을 알 수 있다.In addition, the denitrification unit 400 in the present invention is provided with a configuration for backwashing to remove the blockage of the sponge filter medium 420, and the like. This backwashing process is performed by backwashing from the lower side to the upper side so that the cleaning of the sponge filter material 420 is performed, and the backwashing water generated by the backwashing process is transmitted to the aerobic tank 300 side described above. This is to be delivered to the aerobic tank 300 to maintain the high MLSS in the aerobic tank because the microorganisms are delivered from the aerobic tank 300 in the backwash water by the backwash process. In addition, the denitrification unit 400 is not supplied from an external carbon source, but is controlled by the anaerobic condensation member 720 that forms part of the dephosphorization part 700 so as to be connected to the dephosphorization part 700 which will be described later to receive a carbon source. Use the organic materials and some raw water as carbon sources. The WRT denitrification system is installed at the rear of the aeration tank in the existing activated sludge biological treatment facility, and the HRT of the basic denitrification tank is at least 2 ~ 3hr, whereas the denitrification part is reduced to around 5 ~ 10min. have.
다음, 고액분리부(500)는 슬러지(sludge)와 처리수를 분리시키는 역할을 하는 것으로, 고액분리부의 구성으로 하부는 sludge와 상부는 처리수로 분리되는 과정에서 내통(510)에 격벽(512)이 다단식으로 구성되도록 하고, 외통(520)에는 스크레파(522) 및 회전바(524) 2중 구조로 이루어 지도록 한다. 물의 흐름은 먼저 외부에서 전달되는 오염수는 내통(510)측으로 전달되고, 전달된 물은 다단식 격벽(512)를 통해 유속이 감속되어 천천히 흘러 내리도록 하여 하부에서 고액 분리가 충분히 이루어지도록 한다. 그리고 하부에 슬러지가 쌓이고 분리된 물은 외통의 벽을 타고 상층으로 이동되도록 한다. 이때, 외통의 스크래파(522) 및 회전바(524)가 동시또는 다른 속도로 천천히 움직이도록 구성하는데, 그 이유는 스크래퍼(522)는 천천히 저어면서 슬러지의 고른 분산이 이루어지도록 하고, 회전바(524)는 물속에 잔존한 질소를 제거하도록 하기 위함이다. 즉, 회전바(524) 내부에는 미생물이 충진되어 있어 교반되는 회전바(524)에 물이 접촉되어 질소제거가 이루어 질 수 있게 된다. 따라서 전체적으로 내통(510)의 격벽(512)구조에 의한 슬러지 분산이 이루어지고, 외통(520)측으로 상향식 물의 상승에 의해 하부 및 중층에서 질소가 보다 효과적으로 제거 되어 고액분리가 이루어 질 수 있게 된다. 이러한 구성으로 고액분리가 이루어질 경우 기존시설의 HRT가 3 ~ 4hr인데 반하여 본 발명에서는 HRT가 0.5 ~ 1hr정도로 낮아져 보다 적은 사이즈로 축소하여도 동일한 효과를 달성할 수 있게 된다.Next, the solid-liquid separator 500 serves to separate the sludge (sludge) and the treated water, the partition wall 512 in the inner cylinder 510 in the process of separating the sludge and the upper portion into the treated water in the configuration of the solid-liquid separator ) To be configured in a multi-stage, the outer cylinder 520 is made of a double structure of the scraper 522 and the rotating bar 524. The flow of water is first transmitted from the outside of the contaminated water is delivered to the inner cylinder 510 side, and the delivered water is allowed to flow down slowly through the multi-stage partition wall 512 so that the solid liquid separation is sufficiently performed at the bottom. Sludge builds up on the bottom and the separated water is transported to the upper layer by the wall of the outer cylinder. At this time, the scraper 522 and the rotating bar 524 of the outer cylinder is configured to move slowly at the same or different speed, the reason is that the scraper 522 is stirred slowly and evenly distributed sludge, the rotating bar ( 524 is to remove nitrogen remaining in the water. That is, the inside of the rotating bar 524 is filled with microorganisms so that water is brought into contact with the stirring rotating bar 524 to remove nitrogen. Therefore, sludge dispersion is performed by the partition wall 512 structure of the inner cylinder 510 as a whole, and nitrogen is removed from the lower and middle layers more effectively by rising water upward toward the outer cylinder 520 so that solid-liquid separation can be achieved. When the solid-liquid separation is made in such a configuration, while the HRT of the existing facility is 3 to 4 hr, in the present invention, the HRT is lowered to about 0.5 to 1 hr, so that the same effect can be achieved even if the size is reduced to a smaller size.
그리고 이러한 고액분리부(500)에 분리된 물중 일부는 다시 호기조(300)로 반송되도록 하여 전체적인 호기조의 MLSS가 유지되도록 하고, 나머지는 최종처리부(600)로 이송되어 후처리를 실시한다. And some of the water separated in the solid-liquid separator 500 to be returned to the aerobic tank 300 to maintain the MLSS of the overall aerobic tank, the remainder is transferred to the final processing unit 600 to perform the post-treatment.
최종처리부(600)는 여분의 SS, 유기물질, 질소 및 인의 처리를 위한 스펀지 여재를 이용한 하폐수 처리수 여과 장치로 이루어지도록 한다. 이를 위해 먼저 스펀지여과수조(610)에서 화학약품을 이용하여 잔존미생물 및 유기물질의 분해가 이루어지도록 하고, 이후 스펀지 여재로 이루어진 스펀지 여과부재(620)( WWAY)를 거치도록 한다.The final treatment unit 600 is made of a wastewater treatment water filtration device using a sponge filter medium for the treatment of the extra SS, organic materials, nitrogen and phosphorus. To this end, first, the sponge filtration tank 610 uses chemicals to decompose the remaining microorganisms and organic substances, and then passes through a sponge filtration member 620 (WWAY) made of a sponge filter medium.
스펀지여과부재(WWAY)(620)은 생물학적 및 화학적 처리에서 미처 처리하지 못한 것을 처리하기 위한 최종장치로써, PO4, SS, NH4, Fe, 계면활성제 및 기타 유기물등을 처리하기 위한 고액 분리장치이다. 이의 구성은 스펀지여재가 압축되어 잇으며, 이의 후단에는 활성탄이 충진된 구조를 이루고 있다. 따라서 압축된 스펀지여재를 통과하면서 고상성분들이 흡착되고, 이후 활성탄을 거치면서 최종적으로 오염물질이 제거되도록 한다. 이러한 오염물질이 최종정리된 물은 환경기준에 적합한 물로 변하므로 외부로 방류하게 된다. The sponge filtration member (WWAY) 620 is a final apparatus for treating what is not treated in biological and chemical treatment, and is a solid-liquid separator for treating PO4, SS, NH4, Fe, surfactants and other organic materials. Its structure is a sponge filter material is compressed, the rear end of the structure is filled with activated carbon. Therefore, the solid components are adsorbed while passing through the compressed sponge filter material, and then the contaminants are finally removed through the activated carbon. Water contaminated with these contaminants is discharged to the outside because it turns into water that meets environmental standards.
한편, 일정시간이 지나 스펀지여과장치(wway)(620)는 막힘 등의 현상을 방지하기 위해 세척을 할 수 있도록 저면에서 상부방향으로 역세 세척이 이루어지도록 한다. 역세를 통하여 여과장치의 세척은 물론 역세수로 내부 오염물질을 탈리시키고 발생된 오염수 및 잔류수는 그대로 외부로 방출하는 것이 아니라 유량조정조(100) 또는 후술하는 탈인부(700)의 농축조(710)으로 반류되도록 한다. On the other hand, after a certain time, the sponge filtration device (wway) 620 is to be backwashed from the bottom to the top to be washed to prevent the phenomenon such as clogging. In addition to washing the filtration apparatus through backwashing, decontamination of internal contaminants with backwashing water is not carried out, and the contaminated water and residual water are not discharged to the outside as it is. Return to).
한편 고액분리부(500)에서 배출된 슬러지는 별도의 탈인부(700)로 전달되어 처리되도록 한다. 이러한 슬러지는 그대로 배출시 환경오염을 야기시키므로 오염원을 제거할 필요가 있으며, 무엇보다도 탈인과정이 필요하다. 이러한 농축장치는 농축조(710)과 혐기성농축부재(720)의 두단계를 거치도록 하며, 농축조(710)은 종래 일반적으로 사용되는 농축조(710)을 이용하면 족할 것이다. 그리고 , 이러한 농축조(710)에서 농축후 상등수는 상술한 유량조정조(100)로 반송되도록 한다. Meanwhile, the sludge discharged from the solid-liquid separator 500 is delivered to a separate dephosphorization unit 700 to be treated. As such sludge causes environmental pollution when discharged as it is, it is necessary to remove the pollutant, and above all, dephosphorization process is necessary. This concentrating device is to go through the two stages of the concentration tank 710 and anaerobic concentration member 720, the concentration tank 710 will be sufficient to use the conventionally used thickening tank 710. In addition, the supernatant after concentration in the concentration tank 710 is returned to the above-described flow rate adjustment tank 100.
다음, 농축조(710)에서 농축된 슬러지는 혐기성농축부재(720)으로 전달되며, 빠른 탈산소와 혐기화를 위하여 내부를 60℃ ~ 80℃로 유지시키는 히팅(heating)부재를 구비하도록 하여 혐기작업이 보다 수월하게 이루어지도록 한다. 이러한 히팅부재의 구현으로 인하여 혐기성농축부재(720)의 크기 또한 줄어들 수 있게 된다. 그리고, 혐기화된 슬러지(sludge) 내부에는 많은 유기물질의 분해에 따른 탄소원이 풍부하므로 이러한 슬러지의 일부 및 원수의 일부를 탈질부(400)의 탄소원(carbon sources)으로로 이용하도록 한다. 따라서 상술한 바와 같이 탈질부(400)에서 필요로 하는 탄소원은 외부로 부터 별도 유입이 필요없게 된다.Next, the sludge concentrated in the concentration tank 710 is delivered to the anaerobic thickening member 720, and anaerobic operation by having a heating member for maintaining the interior at 60 ℃ ~ 80 ℃ for rapid deoxygenation and anaerobic Make this easier. Due to the implementation of such a heating member, the size of the anaerobic concentration member 720 can also be reduced. In addition, since there are abundant carbon sources due to the decomposition of many organic substances in the anaerobic sludge, some of the sludge and some of the raw water are used as carbon sources of the denitrification unit 400. Therefore, as described above, the carbon source required by the denitrification unit 400 does not need to be separately introduced from the outside.
다음은, 이러한 컴팩트한 구조로 이루어진 고도 수처리 장치를 실지 테스트한 실시예를 설명하기로 한다.Next, an embodiment in which the advanced water treatment apparatus having such a compact structure is actually tested will be described.
실시예Example
1. 시설 개요1. Facility Outline
(1) 시설명 : 하폐수처리시설(1) Facility name: Sewage and Wastewater Treatment Facility
(2) 설계용량 : 120㎥/d(2) Design capacity: 120㎥ / d
(3) 처리방법 : 스펀지여재(WWAY)를 이용한 컴팩트화 한 고도수처리 공법(3) Treatment method: Compact water treatment method using sponge media (WWAY)
ㆍ 수질기준(청정지역기준)ㆍ Water Quality Standards (Clean Area Standards)
2. 설계사양서2. Design specification
(1) 스크린조(1) screen
① 유효용량① Effective capacity
·500W × 1000L × 800H = 0.4㎥ 500 W × 1000 L × 800 H = 0.4 m3
② 부대설비② Additional Equipment
·조목 스크린, 세목 스크린 : 각 1set Wood screen, detail screen: 1set each
(2) 유량조정조 (2) flow adjustment tank
① 설계용량① Design capacity
V = 7.5㎥ V = 7.5㎥
② 유효용량② Effective capacity
·1750W × 2200L × 2000He(2300H) = 7.7㎥ 1750W × 2200L × 2000He (2300H) = 7.7㎥
③ 용량검토 ③ capacity review
·설계용량 7.5㎥ < 유효용량 7.7㎥ Design capacity 7.5㎥ <Effective capacity 7.7㎥
④ 부대설비④ Additional Equipment
·산기장치 : DISK TYPE 산기관 0.12㎥/min × 4ea (0.48㎥/min) Dispersion device: DISK TYPE diffuser 0.12㎥ / min × 4ea (0.48㎥ / min)
·유량조정조 펌프 (2set) Flow adjustment tank pump (2 sets)
120㎥/d ÷ 24hr/d ÷ 60min/hr = 0.083㎥/min ≒ 0.1㎥/min 120㎥ / d ÷ 24hr / d ÷ 60min / hr = 0.083㎥ / min ≒ 0.1㎥ / min
·사양 : Specifications
이므로 34.3A ≒ 40A 34.3 A ≒ 40 A
= 0.14Kw = 0.14 Kw
여기서, P : 전동기출력(Kw) Where P: motor output (Kw)
γ : 폐수의비중, 1.0 γ: specific gravity of wastewater, 1.0
Q : 유량, 0.1 Q: flow rate, 0.1
H : 전양정, 5m H: Whole head, 5m
η : 펌프의 효율, 0.9 η is the efficiency of the pump, 0.9
α : 안전율, 1.5 α: safety factor, 1.5
따라서, 펌프의 전동기 출력은 표준 규격인 0.75Kw로 한다. Therefore, the electric motor output of a pump shall be 0.75 Kw which is a standard specification.
50A × 0.75Kw × 0.16㎥/min × 10mH(2set) 50A × 0.75Kw × 0.16㎥ / min × 10mH (2set)
(3) 호기조(3) aerobic tank
① 설계용량① Design capacity
*F/M비 이용 * F / M Ratio
∴ V = 8.4㎥ ∴ V = 8.4㎥
② 유효용량② Effective capacity
·1000W × 2200L × 2000He(2300H) = 4.4㎥ 1000W × 2200L × 2000He (2300H) = 4.4㎥
·1000W × 2200L × 2000He(2300H) = 4.4㎥ 1000W × 2200L × 2000He (2300H) = 4.4㎥
③ 용량검토 ③ capacity review
·설계용량 8.4㎥ < 유효용량 8.8㎥ Design capacity 8.4㎥ <Effective capacity 8.8㎥
④ 충진 MEDIA 산출계산④ Calculation of filling media
☞ HBC Ring 으로 충진 시 ☞ Filling with HBC Ring
= 5093 ~ 7639m = 5093-7639 m
∴ HBC Ring 필요량 : 6000m BC Required HBC Ring: 6000m
< H.B.C. 사용량 산정표 [제조사 발췌] > <H.B.C. Usage Estimation Table [Excerpt from Manufacturer]>
⑤ 공기량 산정 ⑤ Air volume calculation
여기서, O2 : 필요산소량(㎏/day)O 2 : required oxygen (㎏ / day)
α : BOD 분해계수(0.5㎎VSS/㎎·BOD)α: BOD decomposition coefficient (0.5 mg VSS / mg BOD)
Lr : BOD 제거량(㎏/day)L r : BOD removal amount (㎏ / day)
a′ : 질산화 분해계수(대표값 0.2) a ': nitrification factor (representative value 0.2)
Nr : 질산화량(㎏)N r : Nitrification amount (㎏)
b : 자산화 계수(0.07d-1)b: assetization factor (0.07d -1 )
b′ : 질산화 내생호흡계수(0.05d-1)b ′: Nitrification endogenous respiration coefficient (0.05d -1 )
Sa : MLVSS량(㎏)S a : MLVSS amount (㎏)
O2 = 0.5 × 120㎥/day × 630㎎/ℓ × 0.6 × 10-3
O 2 = 0.5 × 120 ㎥ / day × 630 mg / L × 0.6 × 10 -3
+ 0.2 × 4.57 × 142.5㎎/ℓ × 0.95 × 120㎥/day × 10-3
+ 0.2 × 4.57 × 142.5mg / L × 0.95 × 120㎥ / day × 10 -3
+ 0.06 × 8.8㎥ × 15000㎎/ℓ × 10-3
+ 0.06 × 8.8㎥ × 15000mg / L × 10 -3
= 22.68㎏/day + 14.85㎏/day + 7.92㎏/day = 22.68㎏ / day + 14.85㎏ / day + 7.92㎏ / day
≒ 25.5㎏/day 5.5 25.5㎏ / day
Air =O2(㎏/day) ÷ 0.277(㎏ O2/㎥)에서Air = O 2 (㎏ / day) ÷ 0.277 (㎏ O 2 / ㎥)
= 25.5㎏/day ÷ 0.277㎏ O2/㎥ ≒ 92.06㎥/day= 25.5㎏ / day ÷ 0.277㎏ O 2 / ㎥ ≒ 92.06㎥ / day
산소이용률 5%로 가산하면 If you add at 5% oxygen utilization
92.06㎥/day ÷ 0.05 = 1841.2㎥/day ≒ 1.28㎥/min 92.06㎥ / day ÷ 0.05 = 1841.2㎥ / day ≒ 1.28㎥ / min
산기관개수 : 1.28㎥/min ÷ 0.12㎥/minea = 10.7ea ≒ 11ea Number of diffuser: 1.28㎥ / min ÷ 0.12㎥ / minea = 10.7ea ≒ 11ea
※ 산기관은 DEAD SPACE가 생기지 않기 위해서 호기조는 12개가 적당 ※ As for the diffuser, 12 aerobic tanks are suitable so that a dead space does not occur
∴ 실제 개수 : 12ea 개수 Actual number: 12ea
⑥ 부대설비 ⑥ Additional facilities
·산기장치 : DISK TYPE 산기관 0.12㎥/min × 12ea (1.44㎥/min) Dispersing device: DISK TYPE diffuser 0.12㎥ / min × 12ea (1.44㎥ / min)
·고정식 접촉담체(Media) : 6000m Fixed contact carrier (Media): 6000m
(4) 탈질부(4) denitrification
① 설계 근거 ① Design Basis
·투입해야 할 CH3OH 량CH 3 OH content
C/N = 2.47a + 1.53b + 0.87c C / N = 2.47a + 1.53b + 0.87c
(질산화율 95%, 탈질율 55%) (95% nitrification rate, 55% denitrification rate)
여기서, a : 질산성 질소량 Where a is the amount of nitrate nitrogen
b : 아질산성 질소량 b: nitrite nitrogen content
c : 탈질장치 유입 DO 량 c: Denitrification inflow DO amount
C/N = (2.47 × 123.6 ×0.95)+(1.53 × 123.6 × 0.05)+(0.87 × 2.0) C / N = (2.47 × 123.6 × 0.95) + (1.53 × 123.6 × 0.05) + (0.87 × 2.0)
= 290.03㎎/ℓ + 9.46㎎/ℓ + 1.74㎎/ℓ = 290.03 mg / l + 9.46 mg / l + 1.74 mg / l
= 301.23㎎/ℓ × 120㎥/d × 10-3
= 301.23 mg / l × 120㎥ / d × 10 -3
= 36.15kg/d = 36.15 kg / d
→ 290.03㎎/ℓ의 CH3OH가 필요하므로 38.03㎎/ℓ의 CH3OH를 외부에서 공급해야 한다. 외부 탄소원은 혐기성농축장치에서 공급하는 것으로 하고 부족할 경우 원수에서 5~10% 공급하는 것으로 한다.→ 29.03 mg / l of CH 3 OH is required, so 38.03 mg / l of CH 3 OH must be supplied externally. External carbon sources will be supplied by anaerobic concentrators and, if insufficient, 5 to 10% of raw water.
·탈질부 부피 Denitrification volume
여기서, NO3i : 유입 질산성 질소(㎎/ℓ) Where NO 3i is the incoming nitrate nitrogen (mg / l)
NO3O : 유출 질산성 질소(㎎/ℓ) NO 3O : outflow nitrate nitrogen (mg / l)
U'= 0.5[메탄]×1.09(40-20)×(1-0.1)U '= 0.5 [methane] × 1.09 (40-20) × (1-0.1)
≒ 2.522 ≒ 2.522
∴ HRT = 1.61×10-3day = 2.32minRT HRT = 1.61 × 10 -3 day = 2.32min
탈질부의 물량은 (반송 50%고려) Quantity of denitrification part (consideration 50%)
120㎥/d + (120㎥/d×0.5) = 180㎥/d 120㎥ / d + (120㎥ / d × 0.5) = 180㎥ / d
탈질부의 부피는 The volume of denitrification
180㎥/d × 1.61 ×10-3day = 0.3㎥180㎥ / d × 1.61 × 10 -3 day = 0.3㎥
② 유효용량 ② Effective capacity
·탈질부는 WWAY-200(V=1.3㎥) 으로 한다. The denitrification part is WWAY-200 (V = 1.3㎥).
③ 용량검토 ③ capacity review
·설계용량 0.3㎥ < 유효용량 1.3㎥ Design capacity 0.3㎥ <Effective capacity 1.3㎥
(5) 고액분리부 (5) solid-liquid separator
① 설계용량 ① Design capacity
·HRT : 30min HRT: 30min
V = 180㎥/d ÷ 24hr ÷ 60min × 30min V = 180㎥ / d ÷ 24hr ÷ 60min × 30min
= 3.75㎥= 3.75㎥
② 유효용량 ② Effective capacity
·Ø1600 × 2000He(2300H) = 4.02㎥ Ø1600 × 2000He (2300H) = 4.02㎥
③ 용량검토 ③ capacity review
·설계용량 3.75㎥ < 유효용량 4.02㎥ Design capacity 3.75㎥ <Effective capacity 4.02㎥
④ 부대설비 ④ Additional Equipment
·슬러지 반송 펌프(침전조 → 호기조) Sludge conveying pump (sedimentation tank → aerobic tank)
: 40A × 0.75Kw × 0.1㎥/min × 8mH(2set) : 40A × 0.75Kw × 0.1㎥ / min × 8mH (2set)
·슬러지 이송 펌프(침전조 → 농축조) Sludge transfer pump (sedimentation tank → concentration tank)
: 40A × 0.75Kw × 0.1㎥/min × 8mH(2set) : 40A × 0.75Kw × 0.1㎥ / min × 8mH (2set)
·교반기 : 0.5HP, 1식 Agitator: 0.5HP, 1 set
·스크래퍼 : 1식 Scraper: 1 set
·월류 웨어 : 1식 Monthly wear: 1 set
·내통 1식 : Φ350mm × H700mm Inner cylinder 1 set: Φ350mm × H700mm
·내통유속 < 0.01m/s Inner cylinder flow rate <0.01 m / s
(6) 스펀지 여과수조(6) sponge filtered water tank
① 설계용량 ① Design capacity
·체류시간(HRT) : 10min HRT: 10min
V = 0.83㎥ V = 0.83㎥
② 유효용량 : 650W × 700L × 1900He(2300H) = 0.86㎥ ② Effective Capacity: 650W × 700L × 1900He (2300H) = 0.86㎥
③ 용량검토 ③ capacity review
·설계용량 0.83㎥ < 유효용량 0.86㎥ Design capacity 0.83㎥ <Effective capacity 0.86㎥
④ 부대설비 ④ Additional Equipment
·여과 펌프 : 50A × 1.5Kw × 0.2㎥/min × 12mH(2set) Filtration pump: 50A × 1.5Kw × 0.2㎥ / min × 12mH (2 sets)
·산기장치 : DISK TYPE 산기관 0.12㎥/min × 1ea (0.12㎥/min) Dispersion device: DISK TYPE diffuser 0.12㎥ / min × 1ea (0.12㎥ / min)
·약품정량주입펌프 : 1~360cc/min × 10kg/㎠ × 0.2Kw Chemical injection pump: 1 ~ 360cc / min × 10kg / ㎠ × 0.2Kw
·약품탱크와 Agitator : 1set Chemical tank and Agitator: 1set
(7) 스펀지여과부재(WWAY)(7) Sponge filtration member (WWAY)
① 설계용량 ① Design capacity
·MODEL : WWAY-200 MODEL: WWAY-200
·처리용량 : 8.3㎥/hr Treatment capacity: 8.3㎥ / hr
·규격 : 내통 Ø550 × 1270H/외통 Ø900 × 2136H Specifications: Inner cylinder Ø550 × 1270H / Outer cylinder Ø900 × 2136H
② 부대시설 ② Facilities
·역세용 Blower : 32A × 4.0㎥/min × 0.3kg/㎠ × 2.2kW Backwash Blower: 32A × 4.0㎥ / min × 0.3kg / ㎠ × 2.2kW
·Compressor : 1.5Kw × 259L/min Compressor: 1.5Kw × 259L / min
·Control Panel(AUTO) Control Panel (AUTO)
(8) 방류조 (8) discharge tank
① 설계용량 ① Design capacity
·체류시간(HRT) : 3min HRT: 3min
V = 0.42㎥V = 0.42㎥
② 유효용량 : 450W × 500L × 2000He(2300H) = 0.45㎥ ② Effective Capacity: 450W × 500L × 2000He (2300H) = 0.45㎥
③ 용량검토 ③ capacity review
설계용량 0.42㎥ < 유효용량 0.45㎥ Design capacity 0.42㎥ <Effective capacity 0.45㎥
④ 부대설비 ④ Additional Equipment
·유량계 Flowmeter
(9) 농축조 (9) thickening tank
① 설계용량 ① Design capacity
·체류시간(HRT) : 3.0day HRT: 3.0day
1. 생물학적 처리 sludge 발생량 1. Generation of biological treatment sludge
여기서, W : 슬러지 발생량(㎏/day) Where W = sludge generation amount (㎏ / day)
α: BOD 분해계수(0.5㎎VSS/㎎·BOD) α: BOD decomposition coefficient (0.5 mg VSS / mg BOD)
Lr : BOD 제거량(㎏/day)L r : BOD removal amount (㎏ / day)
b : 자산화계수(0.07d-1)b: assetization factor (0.07d -1 )
Sa: MLVSS량(㎏)S a : MLVSS amount (㎏)
I : SS 제거량(㎏) I: SS removal amount (㎏)
W = 0.5 × 120㎥/day × 630㎎/ℓ × 0.6 × 10-3
W = 0.5 × 120 ㎥ / day × 630 mg / L × 0.6 × 10 -3
- 0.07 × 8.8㎥ × 15000㎎/ℓ × 10-3
-0.07 × 8.8㎥ × 15000mg / L × 10 -3
+ 120㎥/day × 375㎎/ℓ × 0.48 × 10-3
+ 120㎥ / day × 375mg / ℓ × 0.48 × 10 -3
= (22.68㎏/day - 9.24㎏/day + 21.6㎏/day) = (22.68㎏ / day-9.24㎏ / day + 21.6㎏ / day)
≒ 35.04kg/day ≒ 35.04kg / day
함수율을 99%, 비중을 1.0라고 할 때 When the moisture content is 99% and the specific gravity is 1.0
2. WWAY 역세수 발생량 2.WWAY backwash
·1.0㎥/d × 6회/d = 6㎥/d 1.0 ㎥ / d × 6 times / d = 6 ㎥ / d
총 sludge 및 역세수 발생량 : 9.5㎥/d Total sludge and backwash amount: 9.5㎥ / d
∴ V = 9.5㎥/d × 3.0d = 28.5㎥ ∴ V = 9.5㎥ / d × 3.0d = 28.5㎥
② 유효용량 ② Effective capacity
·2700W × 2700L × 4000H(4400He) = 29.2㎥ 2700W × 2700L × 4000H (4400He) = 29.2㎥
③ 용량검토 ③ capacity review
·설계용량 28.5㎥ < 유효용량 29.2㎥ Design capacity 28.5㎥ <Effective capacity 29.2㎥
④ 부대설비 ④ Additional Equipment
·산기장치 : DISK TYPE 산기관 0.12㎥/min × 4ea (0.48㎥/min) Dispersion device: DISK TYPE diffuser 0.12㎥ / min × 4ea (0.48㎥ / min)
·상등수 이송펌프(농축조 → 유량조) : 20A-40A air-lift pump Upper water feed pump (concentration tank → flow tank): 20A-40A air-lift pump
·sludge 이송펌프(농축조 → 혐기성 농축장치) Sludge transfer pump (concentration tank → anaerobic concentrator)
: 40A × 0.75Kw × 0.1㎥/min × 8mH(2set) : 40A × 0.75Kw × 0.1㎥ / min × 8mH (2set)
(9) 혐기성 농축부재(9) anaerobic thickening members
① 설계용량 ① Design capacity
·체류시간(HRT) : 0.5day HRT: 0.5day
총 sludge 발생량 : 35.04kg/day Total sludge incidence: 35.04kg / day
함수율을 97%, 비중을 1.0 이라고 할 때 When the moisture content is 97% and the specific gravity is 1.0
∴V = 1.2㎥/d × 0.5day = 0.6㎥∴V = 1.2㎥ / d × 0.5day = 0.6㎥
·탈질장치 탄소원 공급 Supply denitrification carbon source
*탈질부에서 필요한 탄소원은 38.03㎎/ℓ이다. * The required carbon source in the denitrification zone is 38.03 mg / l.
38.03㎎/ℓ × 120㎥/d = 4.6kg/d 38.03mg / ℓ × 120㎥ / d = 4.6kg / d
*혐기성 농축부재 슬러지의 COD 농도가 4000㎎/ℓ라고 한다면, * If the COD concentration of anaerobic thickener sludge is 4000 mg / l,
1.2㎥/d × 4000㎎/ℓ = 4.8kg/d 1.2 m3 / d × 4000 mg / l = 4.8 kg / d
4.8kg/d - 4.6kg/d = 0.2kg/d 4.8kg / d-4.6kg / d = 0.2kg / d
(탈질부에서 탄소원이 부족한 경우에는 원수를 탄소원으로 대체한다.) (If the denitrification section lacks a carbon source, replace the raw water with a carbon source.)
② 유효용량 : 600W × 600L × 2000He(2300H) = 0.72㎥ ② Effective Capacity: 600W × 600L × 2000He (2300H) = 0.72㎥
③ 용량검토 ③ capacity review
설계용량 0.6㎥ < 유효용량 0.72㎥ Design Capacity 0.6㎥ <Effective Capacity 0.72㎥
④ 부대설비 ④ Additional Equipment
·산기장치 : DISK TYPE 산기관 0.12㎥/min × 1ea (0.12㎥/min) Dispersion device: DISK TYPE diffuser 0.12㎥ / min × 1ea (0.12㎥ / min)
·상등수 이송펌프(혐기성 농축장치 → 유량조) : 20A-40A air-lift pump Super water feed pump (anaerobic concentrator → flow tank): 20A-40A air-lift pump
·sludge 이송펌프(혐기성 농축장치 → 탈질장치) Sludge transfer pump (anaerobic concentrator → denitrification unit)
: 40A × 0.75Kw × 0.1㎥/min × 8mH(2set) : 40A × 0.75Kw × 0.1㎥ / min × 8mH (2set)
(10) 브로워 (10) Brow
① 브로워 풍압 ① Wind pressure
각 조의 물의 높이 The height of each pair of water
(유량조정조, 호기조, 탈질장치, WWAY여과수조, 혐기성 농축장치) (Flow control tank, aerobic tank, denitrification unit, WWAY filtration tank, anaerobic concentrator)
→ (2000, 2000, 2136, 1900, 2000)mmH 이므로 → (2000, 2000, 2136, 1900, 2000) mmH
물의 높이가 가장 높은 것을 선택하면 2136mmH이다. If you choose the tallest water, it is 2136mmH.
∴총 풍압 = 2136mm = 2.2mH Total wind pressure = 2136 mm = 2.2 mH
② 송풍량: disk type 산기관 0.12㎥/min의 개수에 따른 량 + air lift 펌프 송풍량 ② Blowing volume: volume according to disk type diffuser 0.12㎥ / min + air lift pump blowing volume
·집수조 및 유량조정조 : 4 × 0.12㎥/min Collection tank and flow adjustment tank: 4 × 0.12㎥ / min
·호기조 : 12 × 0.12㎥/min Exhalation tank: 12 × 0.12㎥ / min
·WWAY 여과수조 : 1 × 0.12㎥/min WWAY filtered water tank: 1 × 0.12㎥ / min
·농축조 : 4× 0.12㎥/min Concentration tank: 4 × 0.12㎥ / min
·혐기성 농축부재 : 1 × 0.12㎥/min Anaerobic thickening member: 1 × 0.12㎥ / min
·air lift pump 20A-40A 필요 공기량 : 2 × 0.38㎥/min Air lift pump 20A-40A Required air volume: 2 × 0.38㎥ / min
∴ 총 송풍량 = disk type 22 × 0.12㎥/min (2.64㎥/min) ∴ Total air flow = disk type 22 × 0.12㎥ / min (2.64㎥ / min)
+ air lift 2 × 0.38㎥/min (0.76㎥/min) + air lift 2 × 0.38㎥ / min (0.76㎥ / min)
= 3.4㎥/min = 3.4㎥ / min
·사양 : 80 × 2.2Kw × 5㎥/min × 4000mmAq(2set) Specifications: 80 × 2.2Kw × 5㎥ / min × 4000mmAq (2set)
상기 실시예와 같이 각각의 용량 및 제반규격을 설계하고 제작한 후, 실지 테스트 한 결과는 아래 표와 같이 나타났다.After designing and fabricating each capacity and standard as in the above embodiment, the results of the actual test are shown in the table below.
(농도:㎎/ℓ, 제거율:%)(Concentration: mg / L, removal rate:%)
상기 처리효율표에서 나타난 바와 같이, 본 발명에서는 보다 컴팩트화 한 장치로서도 최종처리의 결과를 보면, 기존의 대규모 장치시설에서 보다도 높은 효율로 고도수처리가 이루어짐을 알 수 있었다. As shown in the above treatment efficiency table, in the present invention, as a result of the final treatment as a more compact device, it can be seen that the high-water treatment is performed at a higher efficiency than that of the existing large-scale equipment facilities.
상기한 실시예는 예시적인 것에 불과한 것으로, 당해 기술분야에 대한 통상의 지식을 가진 자라면 이로부터 다양하게 변형된 다른 실시예가 가능하다.The above embodiments are merely exemplary, and those having ordinary skill in the art may have other embodiments modified in various ways.
따라서 본 발명의 진정한 기술적 보호범위에는 하기의 특허청구범위에 기재된 발명의 기술적 사상에 의해 상기의 실시예뿐만 아니라 다양하게 변형된 다른 실시예가 포함되어야 함을 알 수 있다.Therefore, it can be seen that the true technical protection scope of the present invention should include not only the above-described embodiment but also various other embodiments modified by the technical spirit of the invention described in the claims below.
본 발명은 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치에 관한 것으로, 하폐수처리시설의 호기조와 탈질부에 설치할 수 있다.The present invention relates to a compact advanced water treatment apparatus using a sponge filter medium, which can be installed in an aerobic tank and a denitrification unit of a sewage treatment plant.
호기조에는 인처리 미생물의 럭셔리 업테이크(luxury uptake), 암모니아성 질소에서 질산성질소로 질산화 및 함유된 유기물의 일정부분 산화가 이루어지도록 미생물미디어가 함유된 스폰지여재가 설치할 수 있다.The aerobic tank may be equipped with a sponge uptake containing microbial media such that luxury uptake of phosphorus-treated microorganisms, nitrification from ammonia nitrogen to nitrate nitrogen, and partial oxidation of the contained organic matter are performed.
탈질부에는 내부에 미생물미디어가 함유된 스펀지여재를 설치할 수 있다.In the denitrification unit, a sponge filter medium containing microbial media may be installed therein.
Claims (11)
- 오염된 하폐수를 물리화학적 및 생물학적으로 처리하는 고도 수처리 장치에 있어서,In the advanced water treatment apparatus for treating contaminated sewage water physicochemically and biologically,부유물질 등을 걸러내는 스크린을 거쳐 유입되는 오염수를 일정 농도로 저장하는 유량조정조와;A flow rate adjusting tank for storing the contaminated water flowing in a predetermined concentration through a screen for filtering the suspended substances;상기 유량조정조로 전달되는 오염수를 생물학적으로 처리하되, 인처리 미생물의 럭셔리 업테이크(luxury uptake), 암모니아성 질소에서 질산성질소로 질산화 및 함유된 유기물의 일정부분 산화가 이루어지도록 미생물미디어가 함유된 스폰지여재가 설치되는 호기조와:Biological treatment of contaminated water delivered to the flow adjustment tank, containing microorganism media such that luxury uptake of phosphorus-treated microorganisms, nitrification from ammonia nitrogen to nitrate nitrogen, and partial oxidation of organic matters The aerobic tank with sponge media installed:상기 호기조 후단에 연결되고 상기 호기조에서 질산화된 질산헝질소를 질소가스로 원활한 탈질작용을 위한 적정온도를 유지하기 위한 히팅부재가 구비되고 내부에 미생물미디어가 함유된 스펀지여재가 구비되어 산화된 오염수의 탈질작용을 수행하는 탈질부와;The contaminated water oxidized by a sponge member which is connected to the back end of the aerobic tank and maintains a proper temperature for smooth denitrification of nitrous nitrate nitrified in the aerobic tank with nitrogen gas and a microorganism media containing therein is provided therein. Denitrification unit performing the denitrification of;상기 탈질부를 통과한 처리수는 슬러지와 함께 상향류식으로 유입되어 중력으로 고액분리를 하며, 상등수의 일부는 상기 호기조로 반송하고, 나머지는 일측 외부로 유출하며, 하부에 남는 슬러지를 타측외부로 유출하는 침전식으로 이루어지는 고액분리부와;The treated water passing through the denitrification unit flows into the sludge with an upward flow to separate the solid-liquid separation by gravity, and a part of the supernatant is returned to the aerobic tank, and the rest is discharged to one outside, and the sludge remaining at the bottom is discharged to the outside. And solid-liquid separation unit consisting of a precipitation;상기 고액분리부에서 외부로 유출되는 상등수를 후처리하여 최종방류하는 최종처리부;그리고The final processing unit for the final discharge by treating the supernatant outflowed to the outside in the solid-liquid separator; And상기 고액분리부에서 유출되는 슬러지를 탈인하도록 히팅부재가 구비되고, 슬러지의 일부를 외부탄소원으로 상기 탈질부측으로 반송하는 탈인부;를 포함하여 이루어지는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.Compacted advanced water treatment using a sponge filter medium comprising a; heating member is provided to dephosphorize the sludge flowing out of the solid-liquid separation unit, the dephosphorization unit for conveying a portion of the sludge to the denitrification unit side as an external carbon source Device.
- 제 1항에 있어서,The method of claim 1,상기 유량조정조와 상기 호기조 사이에는 미세부유물질 등을 제거하기 위한 하이드라시브 스크린(hydrasieve screen)이 더 설치됨을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치Compact water treatment apparatus using a sponge filter medium characterized in that the hydrasieve screen is further installed between the flow rate adjustment tank and the exhalation tank to remove the fine suspended solids, etc.
- 제 1항에 있어서, The method of claim 1,상기 호기조는 내부가 다수개의 통공이 형성된 격벽에 의해 다단으로 이루어지고, 상기 각 격벽상에 스폰지여재가 적층되어 이루어지고, 산기관을 통해 바닥 저부로 부터 상방향으로 산소가 공급되는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치. The exhalation tank is made of a multi-stage by the partition wall is formed with a plurality of holes, the sponge filter is laminated on each of the partition wall, characterized in that the oxygen is supplied upward from the bottom bottom through the diffuser pipe Compact water treatment device using sponge filter media.
- 제 1항에 있어서,The method of claim 1,상기 탈질부의 히팅부재는 35 내지 45℃의 온도조절이 이루어지는 것을 특징으로 하는 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치The heating member of the denitrification unit compact water treatment apparatus using a sponge filter medium, characterized in that the temperature control of 35 to 45 ℃
- 제 4항에 있어서, The method of claim 4, wherein상기 탈질부에는 스펀지여재의 막힘 방지를 위해 하부로 부터 상방향으로 역세수 처리가 이루어지는 역세수분사부재가 구비되고, 청소후 오염물질을 함유하는 처리된 역세수는 상기 호기조로 전달되도록 하는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치..The denitrification unit is provided with a backwash water spraying member for backwashing from the bottom to prevent clogging of the sponge filter material, and the treated backwashing water containing contaminants after cleaning is delivered to the aerobic tank. Compact water treatment device using a sponge filter ..
- 제 1항에 있어서,The method of claim 1,상기 고액분리부는 내벽에 하향 경사지게 다단으로 격벽이 구비되어 중앙 상부측에 형성된 내통과,The solid-liquid separator is provided with a multi-stage partition inclined downward on the inner wall, the inner passage formed on the upper side of the center,내통의 중심을 관통하는 회전하는 중심축의 하부측에는 스크래퍼가 구비되고, 상부측에는 미생물미디어를 함유하는 다수개의 지지바가 구비된 외통의 2중구조로 이루어지고, The lower side of the rotating central shaft passing through the center of the inner cylinder is provided with a scraper, the upper side is made of a double structure of the outer cylinder provided with a plurality of support bars containing microbial media,탈질부를 통과한 오염수는 상기 내통의 상방향에서 하방향으로 중력식으로 정달되어 다단 격벽에 의해 유속이 저감된 상태로 상기 외통의 저면으로 전달되어 슬러지가 하부면에 쌓이도록 하고, 분리된 물은 외통저면에서 상방향으로 전달되면서 상기 회전바에 의해 오염수의 처리가 이루어지도록 하는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.The contaminated water passing through the denitrification portion is gravitationally fed from the upper direction of the inner cylinder to the lower direction, and is delivered to the bottom of the outer cylinder in a state in which the flow velocity is reduced by the multi-stage partition wall so that the sludge accumulates on the lower surface. The compact water treatment apparatus using a sponge filter material, characterized in that the treatment of the contaminated water by the rotating bar while being transmitted upward from the outer cylinder bottom.
- 제 1항 내지 제6항 중 어느 하나의 항에 있어서,The method according to any one of claims 1 to 6,상기 후처리시설부는,The post-processing facility unit,약품주입으로 인한 화학적 처리가 이루어지는 스펀지여과수조와;A sponge filtration tank in which chemical treatment is performed by chemical injection;스펀지여재와 활성탄으로 물리적 처리가 이루어지는 스펀지여과부재; 그리고A sponge filter member which is physically treated with a sponge filter medium and activated carbon; And스펀지여재부재를 청소하도록 물과 공기가 혼합되어 역세로 분사되는 역세수분사부재;로 이루어짐을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.Compact water treatment apparatus using a sponge filter medium, characterized in that consisting of; a backwash water injection member is mixed with water and air to be sprayed with backwash to clean the sponge filter member.
- 제 7항에 있어서,The method of claim 7, wherein상기 스펀지여과부재는 압착된 스펀지부재와 이의 뒷면에 부착되는 활성탄부재로 이루어지고,The sponge filtration member is composed of a compressed sponge member and an activated carbon member attached to the back of the sponge member,상기 역세수분사부재를 통해 분사되어 치리된 역세수를 상기 유량조정부로 반송되도로 하는 반송라인이 더 구비되는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.And a conveying line for conveying the backwash water injected through the backwash water injection member to the flow rate adjusting unit.
- 제1항 내지 제6항중 어느 하나의 항에 있어서,The method according to any one of claims 1 to 6,상기 탈인부는,The dephosphorization unit,상기 고액분리부에서 전달된 슬러지를 농축하는 농축조와;A concentration tank for concentrating the sludge delivered from the solid-liquid separator;상기 농축조를 거쳐온 농축슬러지를 혐기조건하에서 탈인이 이루어지도록 히팅부재가 구비된 혐기성농축부재 이루어지는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.The compact water treatment apparatus using a sponge filter medium, characterized in that the anaerobic condensing member is provided with a heating member so that dephosphorization is carried out under anaerobic conditions.
- 제9항에 있어서, The method of claim 9,상기 농축조에는 농축후 남는 상등수를 상기 유량조정조로 반송하는 반송라인이 구비되는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.The condensing tank compact water treatment apparatus using a sponge filter, characterized in that the conveying line for conveying the remaining supernatant water after the concentration to the flow rate adjustment tank.
- 제9항에 있어서, The method of claim 9,상기 혐기성 농축부재의 히팅부재는 55 내지 65℃로 온도 조절이 이루어지고, The heating member of the anaerobic thickening member is made of a temperature control to 55 to 65 ℃,슬러지의 일부를 상기 탈질부로 반송하는 라인이 구비되는 것을 특징으로 하는 스펀지 여재를 이용한 컴팩트화 한 고도수처리 장치.A compact advanced water treatment device using a sponge filter material, characterized in that a line for conveying part of the sludge to the denitrification portion is provided.
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