KR102561953B1 - Water treatment apparatus using biological activated carbon - Google Patents

Abstract

The present invention relates to a water treatment apparatus using a biological activated carbon process, wherein, in the treatment of concentrated water, which is generated from a sewage reuse process using a reverse osmosis membrane, through a biological activated carbon process, various bacteria, such as anaerobic bacteria, aerobic bacteria, and facultative anaerobic bacteria, coexist in activated carbon, and process conditions are selectively changed according to nitrogen properties of effluent, thereby effectively removing total organic carbon (TOC), total nitrogen (T-N), and total phosphorus (T-P) included in the concentrated water generated through sewage reuse even under low C/N ratio conditions. The water treatment apparatus using a biological activated carbon process, according to the present invention, comprises a first biological activated carbon reactor and a second biological activated carbon reactor that are arranged adjacent to each other and sequentially treat raw water, wherein the first biological activated carbon reactor and the second biological activated carbon reactor are alternatively operated under anoxic conditions and aerobic conditions, and the raw water is treated by sequentially passing through a reactor under the anaerobic conditions and a reactor under the aerobic conditions. As the first biological activated carbon reactor and the second biological activated carbon reactor are alternatively operated under the anoxic conditions and the aerobic conditions, anaerobic bacteria, aerobic bacteria, and facultative anaerobic bacteria coexist in biological activated carbon filled in each of the first biological activated carbon reactor and the second biological activated carbon reactor.

Description

Water treatment apparatus using biological activated carbon}

The present invention relates to a water treatment device using a bioactive carbon process, and more particularly, in treating concentrated water generated in a sewage recycling process using a reverse osmosis membrane through a bioactive carbon process, anaerobes, aerobic bacteria, and anaerobes under conditions on activated carbon In addition, by selectively changing the process conditions according to the nitrogen properties of the effluent, the total organic carbon (TOC), total nitrogen (T-N) and It relates to a water treatment device using a bioactive carbon process capable of effectively removing total phosphorus (TP).

Sewage treatment aims to remove contaminants contained in sewage and is largely classified into primary treatment, secondary treatment and tertiary treatment. The primary treatment is a method of physically removing floating substances or sedimentary substances in the sewage, and facilities such as gravity sedimentation and flotation separation are used, and the process from the sewage treatment plant to the first settling tank is usually applicable. As for the secondary treatment, a biological treatment method is mainly used for the purpose of removing organic matter dissolved in sewage and organic solids not treated in the primary treatment. The tertiary treatment is an advanced treatment process that combines physical, chemical, and biological treatment methods for the purpose of removing fine suspended matter and non-decomposable substances in order to comply with the effluent water quality standards and to secure the water quality of reused water.

In general, effluent discharged from sewage treatment plants refers to what has undergone secondary treatment, and various efforts are being made to reuse secondary treated water from sewage treatment plants. Reuse of secondary treated water includes cleaning water, sprinkling water, landscaping water, river maintenance water, agricultural water, cooling water, and industrial water.

Methods for performing the tertiary treatment process in which secondary treated water is reused include advanced oxidation, flocculation precipitation, rapid filtration, activated carbon adsorption, pressure flotation, reverse osmosis, membrane separation, and the like. The tertiary treatment process is determined according to the demand for water quality and the application. In particular, cooling water and industrial water are generally similar to drinking water quality standards, and in particular, salt substances contained in effluent must be removed. Therefore, when applied to industrial water, etc., a reverse osmosis membrane process capable of removing dissolved organic matter and inorganic matter is applied.

In the reverse osmosis membrane process, most of the organic and inorganic substances contained in the raw water are removed to produce water close to pure water. .

In order to reuse secondary treated water (effluent from sewage treatment plant) as industrial water, the reverse osmosis membrane process and technology are standardized to a large extent and there is no difficulty in application. It is known that there is a limit to field application due to low chemical treatment efficiency.

The secondary treated water (effluent from sewage treatment plant) discharged under the current effluent water treatment facility Ⅰ standard (TOC 15 mg/L, T-N 20 mg/L, T-P 0.2 mg/L) is replaced by the tertiary treatment facility (reverse osmosis membrane process, Recovery rate 70%), the concentration of concentrated water discharged from the reverse osmosis membrane process is approximately TOC 50 mg/L, T-N 67 mg/L, T-P 0.67 mg/L, based on effluent standards (TOC 25 mg/L, T-N 20 mg /L, T-P 2.0 mg/L, IV area) will be exceeded. Therefore, it is necessary to apply an additional wastewater treatment process in order to discharge the concentrated water generated in the reverse osmosis membrane process in accordance with the effluent water quality standards.

Most of the TOC substances in concentrated water are non-degradable, so the treatment efficiency is low when biological treatment, oxidation process, flocculation precipitation process, etc. are applied, and high concentration TDS components present in concentrated water are known to impair treatment efficiency. In particular, when applying the biological treatment process using the existing activated sludge to concentrated water, not only the TOC removal efficiency is low, but also the carbon source for the survival and growth of microorganisms is insufficient, so it is difficult to maintain an appropriate microbial population without an additional carbon source supply. For the same reason, even when treating NO ₃ -N present in concentrated water, an additional carbon source for microbial growth is required in addition to the organic carbon source for denitrification, so it is necessary to maintain an excessive C / N ratio compared to the existing one, resulting in an increase in operating costs.

Korea Patent Registration No. 683914 (2007. 2. 20. Publication) Korean Patent Publication No. 2019-85916 (published on July 19, 2019) Korean Registered Patent Publication No. 1268967 (Announced on May 29, 2013) Korean Registered Patent Publication No. 945457 (Announced on March 5, 2010)

The present invention was made to solve the above problems, and in treating concentrated water generated in a sewage recycling process using a reverse osmosis membrane through a bioactive carbon process, various bacteria such as anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria Total organic carbon (TOC), total nitrogen (T-N) and total phosphorus (T-P) contained in sewage reused concentrated water even under low C/N ratio conditions by selectively changing the process conditions according to the nitrogen properties of the effluent. ) The purpose is to provide a water treatment device using a bioactive carbon process that can effectively remove.

A water treatment device using a bioactive carbon process according to the present invention for achieving the above object includes a first bioactive carbon reactor and a second bioactive carbon reactor that are disposed adjacent to sequentially treat raw water, and include a first bioactive carbon reactor and Each of the second bioactive carbon reactors is operated alternately under anoxic conditions and aerobic conditions, and raw water is processed sequentially through the anoxic and aerobic reaction tanks, and each of the first and second bioactive carbon reactors It is characterized in that anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria coexist in the bioactive carbon filled in the first bioactive carbon reactor and the second bioactive carbon reactor, respectively, due to the alternating operation under anoxic conditions and aerobic conditions.

An air supply pump supplying air to the raw water inflow path of the reaction tank operated under aerobic conditions; An organic carbon source supply device for supplying an organic carbon source to a raw water inflow path of a reactor operated under anoxic conditions; Fe ³⁺ supply device for supplying Fe ³⁺ to the raw water inflow path of the reactor operated under anoxic conditions; and the Fe ³⁺ supply device supplies a biodegradable chelate material and Fe ³⁺ together, or It may be supplied by mixing Fe ³⁺ with feed water having a pH of 2 or less.

It may further include a circulation water tank for storing raw water that has passed through the reaction tank under anoxic conditions, and a circulation pump for supplying raw water from the circulation water tank to the reaction tank under aerobic conditions.

A dissolved air flotation separation tank is further provided on the path between the first bioactive carbon reactor and the second bioactive carbon reactor, and the dissolved air flotation separation tank is supplied with raw water that has passed through the reaction tank under anoxic conditions and is a coagulant applied to the dissolved air flotation separation process. Organic matter and phosphorus in the raw water are treated through, and the raw water discharged from the dissolved air flotation separation tank is supplied to the reaction tank under aerobic conditions.

The bioactive carbon is obtained by supplying raw water mixed with an organic carbon source to the first bioactive carbon reactor and the second bioactive carbon reactor in a state in which granular activated carbon is filled in each of the first bioactive carbon reactor and the second bioactive carbon reactor, and the surface of the granular activated carbon and the process of adsorbing the organic carbon source into the internal pores, and supplying the raw water mixed with the activated sludge to the first bioactive carbon reactor and the second bioactive carbon reactor to obtain anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria on the surface and internal pores of the granular activated carbon. and supplying raw water to the first bioactive carbon reactor and the second bioactive carbon reactor, and intermittently supplying air to each of the first and second bioactive carbon reactors to form the surface and internal pores of the granular activated carbon. It is prepared through the process of growing attached anaerobic bacteria, aerobic bacteria and conditional anaerobic bacteria.

In addition, the water treatment device using bioactive carbon according to the present invention includes a first bioactive carbon reactor and a second bioactive carbon reactor that are disposed adjacent to each other and sequentially treat raw water, and the first bioactive carbon reactor and the second bioactive carbon reactor, respectively. is operated alternately under anoxic and aerobic conditions, and if the concentration of ammonia nitrogen in the raw water is higher than the preset reference value, the raw water is treated sequentially through the reaction tank under aerobic conditions and the reaction tank under anoxic conditions, and ammonia nitrogen in the raw water If the concentration of is lower than the preset reference value, the raw water is treated by sequentially passing through the anoxic condition reaction tank and the aerobic condition reaction tank, and the first bioactive carbon reaction tank and the second bioactive carbon reaction tank are alternately operated under anoxic conditions and aerobic conditions, respectively. Another feature is that anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria coexist in the bioactive carbon filled in each of the first bioactive carbon reactor and the second bioactive carbon reactor due to the operation.

Ammonia nitrogen measuring device for measuring the concentration of ammonia nitrogen in raw water; An air supply pump supplying air to the raw water inflow path of the reaction tank operated under aerobic conditions; An organic carbon source supply device for supplying an organic carbon source to a raw water inflow path of a reactor operated under anoxic conditions; Fe ³⁺ supply device for supplying Fe ³⁺ to the raw water inflow path of the reactor operated under anoxic conditions; and the Fe ³⁺ supply device supplies a biodegradable chelate material and Fe ³⁺ together, or It may be supplied by mixing Fe ³⁺ with feed water having a pH of 2 or less.

The water treatment device using the bioactive carbon process according to the present invention has the following effects.

Total organic carbon (TOC), total nitrogen (T-N) as well as total phosphorus (TP) can be effectively removed by operating two bioactive carbon reactors alternately under anoxic and aerobic conditions. In addition, by selectively changing the order of anoxic operation and aerobic operation according to the concentration of ammonia nitrogen contained in the raw water, stable removal efficiency of total nitrogen (T-N) can be secured.

1 is a block diagram of a water treatment device using a bioactive carbon process according to a first embodiment of the present invention.
2a and 2b are reference views for explaining a water treatment process according to a first embodiment of the present invention.
3 is a block diagram of a water treatment device using a bioactive carbon process according to a second embodiment of the present invention.
4a and 4b are reference views for explaining a water treatment process in a case where the concentration of ammonia nitrogen is higher than the reference value in the second embodiment of the present invention.
5A and 5B are reference views for explaining a water treatment process in a case where the concentration of ammonia nitrogen is lower than the reference value in the second embodiment of the present invention.
6 is a block diagram of a water treatment device using a bioactive carbon process according to a third embodiment of the present invention.

In the present invention, in treating concentrated water generated in the process of recycling effluent from a sewage treatment plant through a reverse osmosis membrane process, total organic carbon (TOC) and total nitrogen (total organic carbon (TOC), total nitrogen ( T-N) and total phosphorus (T-P) are presented.

As mentioned above in 'Technology behind the Invention', the concentrated water discharged during the tertiary treatment through the application of the reverse osmosis membrane process contains total organic carbon (TOC) and total nitrogen (T-N) above the effluent water quality standard, so it is concentrated. It is necessary to introduce a wastewater treatment facility for water treatment. However, in the case of total organic carbon (TOC) in the concentrated water, a large amount of non-degradable organic matter is included, so the treatment efficiency in wastewater treatment facilities is low, making it difficult to comply with water quality standards. This is necessary and has a problem of rising operating costs.

The present invention proposes a process configuration capable of effectively removing total organic carbon (TOC) and total nitrogen (T-N) while maintaining a C/N ratio of about 2.5 in raw water.

In general, in the case of a process using microorganisms such as an activated sludge process to treat recycled concentrated water, the organic carbon source available to microorganisms in the raw water is small, but the total nitrogen (T-N) is relatively high, so the organic carbon source required for denitrification is low. In addition, excessive injection of an external organic carbon source is required for proper MLSS maintenance and microbial growth. Considering the sedimentation of microorganisms, the general activated sludge method requires a larger amount of microorganisms to be maintained than the biofilm method, so a relatively high C/N ratio must be maintained to secure denitrification efficiency above an appropriate level. Existing bioactive carbon processes (see Patent Documents 1 to 3) are mostly applied as one unit process among all water treatment processes, and are somewhat unrelated to the removal of recalcitrant organic matter and denitrification.

The present invention is equipped with two bioactive carbon reactors, allows anaerobic bacteria, aerobic bacteria and anaerobes to grow together in each reactor tank, and operates each reactor alternately under aerobic conditions and anoxic conditions, resulting in a low C/N ratio. It improves the removal efficiency of total organic carbon (TOC), total nitrogen (T-N), and total phosphorus (TP) even under conditions. In addition, the present invention can secure stable nitrogen treatment efficiency by changing the order of anoxic operation and aerobic operation according to the concentration value of ammonia nitrogen contained in effluent.

Hereinafter, the water treatment apparatus using the bioactive carbon process according to the first and second embodiments of the present invention will be described in detail with reference to the drawings. The first embodiment relates to alternating and repeating the operating conditions of the two reactors in operating the process in the order of anoxic conditions and aerobic conditions, and the second embodiment relates to the level of ammonia nitrogen contained in raw water. It is about changing the order of anoxic operation and expiratory operation according to Both the first embodiment and the second embodiment utilize two bioactive carbon reactors.

Referring to FIG. 1 , a water treatment apparatus using a bioactive carbon process according to a first embodiment of the present invention includes a raw water tank 110, a first bioactive carbon reactor 120, and a second bioactive carbon reactor 130.

The raw water tank 110 supplies secondary treated raw water, for example, effluent from a sewage treatment plant to the first bioactive carbon reactor 120 or the second bioactive carbon reactor 130, and the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 are operated under anoxic conditions or aerobic conditions, and serve to remove total organic carbon (TOC), total nitrogen (T-N), and total phosphorus (TP) contained in raw water. In addition, an intermediate water tank 14 and a circulation pump 15 may be further provided on a path between the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 . Raw water that has passed through the first bioactive carbon reactor 120 or the second bioactive carbon reactor 130 under anoxic conditions is stored in the intermediate water tank 14 and operated under aerobic conditions through the circulation pump 15. The second bioactive carbon reactor ( 130) or the first bioactive carbon reactor 120.

In a path between the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, for example, an air supply pump 12 is provided at a front end or a rear end of the intermediate water tank 14. As air is supplied by the air supply pump 12 to raw water that has passed through the first bioactive carbon reactor 120 under anoxic conditions, the second bioactive carbon reactor 130 can be operated under aerobic conditions. As air is supplied by the air supply pump 12 to the raw water that has passed through the second bioactive carbon reactor 130 under anoxic conditions, the first bioactive carbon reactor 130 can be operated under aerobic conditions.

On the other hand, an organic carbon source supplying device 13 for supplying an organic carbon source to raw water is further provided, and the organic carbon source supplying device 13 is a raw water supply passage of the first bioactive carbon reactor 120 operated under anoxic conditions or a second biological The organic carbon source is selectively supplied to the raw water supply passage of the activated carbon reactor 130. The organic carbon source is adsorbed on the surface and internal pores of the granular activated carbon filled in the first bioactive carbon reactor 120 or the second bioactive carbon reactor 130.

Along with this, an Fe ³⁺ supply device 16 for supplying Fe ³⁺ to the raw water is further provided. The Fe ³⁺ supplying device supplies Fe ³⁺ to the raw water supply passage of the first bioactive carbon reactor 120 or the raw water supply passage of the second bioactive carbon reactor 130 operated under anoxic conditions. Such Fe ³⁺ is reduced to Fe ²⁺ by the bacteria reducing the recalcitrant organic matter in the reaction vessel serving as an electron shuttle, and the recalcitrant organic matter is decomposed in the process of reducing Fe ³⁺ to Fe ²⁺ . In addition, Fe ³⁺ that is not reduced to Fe ²⁺ acts as a coagulant and removes non-decomposable organic substances and total phosphorus (TP) in raw water. Fe ²⁺ produced by the reduction reaction in the reactor under anoxic conditions flows into the reactor under aerobic conditions, and under aerobic conditions, Fe ²⁺ is oxidized to Fe ³⁺ to aggregate and remove non-decomposable organic substances and total phosphorus (TP).

A biodegradable chelate that suppresses insolubilization of Fe ³⁺ to prevent Fe ³⁺ from being aggregated and flocculated before reaching the reaction tank under anoxic conditions when Fe ³⁺ is supplied to raw water through the Fe ³⁺ supply device It is preferable to supply the material and Fe ³⁺ together or to supply raw water by mixing Fe ³⁺ with supply water having a pH of 2 or less. In addition, in the case of using a biodegradable chelate material, the amount of external denitrification organic matter injected can be reduced by the amount of the organic matter concentration of the chelate.

Each of the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 is operated under anoxic or aerobic conditions. In the first embodiment of the present invention, the overall water treatment process is performed in anoxic operation followed by aerobic operation method, and the sequence of anaerobic operation and expiratory operation is repeated.

Raw water is alternately introduced into the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 . In the first step, raw water flows into the first bioactive carbon reactor 120, and raw water that has passed through the first bioactive carbon reactor 120 is supplied to the second bioactive carbon reactor 130 through the intermediate water tank 14 (FIG. 2a). Reference), in the second step, the raw water flows into the second bioactive carbon reactor 130, and the raw water passing through the second bioactive carbon reactor 130 is supplied to the first bioactive carbon reactor 120 through the intermediate water tank 14. (See Fig. 2b). The first step and the second step are independent water treatment processes. When the first step process and the second step process are completed, treated water is produced, respectively.

For the inflow and supply of raw water, a flow path is provided between the raw water tank 110, the first bioactive carbon reactor 120, and the bioactive carbon reactor. Looking at this path, the path through which raw water is moved in the first step is referred to as the first path, The path through which the enemy moves in the second step may be referred to as the second path. The first path is a path connecting the raw water tank 110, the first bioactive carbon reactor 120, the intermediate water tank 14, and the second bioactive carbon reactor 130 in order, and the second path is the raw water tank 110 , The second bioactive carbon reactor 130, the intermediate water tank 14, and the first bioactive carbon reactor 120 are sequentially connected. A flow path satisfying the first path and the second path can be designed in various forms, and FIG. 1 shows an embodiment of a flow path satisfying the first path and the second path. As shown in FIG. 1, the first path and the second path use a common flow path, and the flow path can be selectively opened or blocked by opening and closing the valve.

As described above, the overall water treatment process of the first embodiment proceeds in the order of anoxic operation and aerobic operation, and the first step process and the second step process proceed sequentially and repeatedly. Both steps proceed in the order of anoxic operation and expiratory operation.

The first step and the second step are described in detail as follows.

First, referring to Figure 2a, in the first step, the raw water of the raw water tank 110 is introduced into the first bioactive carbon reactor 120 through the raw water supply pump 11. Raw water flows into the first bioactive carbon reactor 120 upstream, and raw water that has passed through the first bioactive carbon reactor 120 is discharged through the top of the first bioactive carbon reactor 120 and passes through the intermediate water tank 14. It is moved toward the second bioactive carbon reactor 130 through the circulation pump 14 . For reference, among the valves provided on the raw water flow path, the air supply path, the organic carbon source supply path, and the Fe ³⁺ supply path in FIG. 2a and FIGS. 2a, 4a, 4b, 5a, and 5b described below, the valve filled in black is open. indicates the closed state, and the valve filled with white means the closed state.

The first bioactive carbon reactor 120 is filled with bioactive carbon, and the second bioactive carbon reactor 130 also forms a behavior in which the bioactive carbon is filled in the same way as the first bioactive carbon reactor 120 . The bioactive carbon filled in the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 is obtained by combining microorganisms with granular activated carbon, and both the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 are biologically active. Anaerobic bacteria, aerobic bacteria and conditional anaerobic bacteria coexist in activated carbon. Usually, anaerobic bacteria are dominant in the anaerobic reactor, and aerobic bacteria are dominant in the aerobic reactor and grow. In the present invention, the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, respectively, As the aerobic conditions proceed alternately, anaerobic bacteria, aerobic bacteria and conditional anaerobic bacteria can coexist in the bioactive carbon of each reactor. Here, the anaerobes are microorganisms that are activated under both anoxic and aerobic conditions.

In addition, bioactive carbon is prepared by combining microorganisms with granular activated carbon. Before proceeding in the first step, the organic carbon source is supplied to the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 filled with granular activated carbon to obtain bioactive carbon. can be prepared, which will be described later.

In the first step, the first bioactive carbon reactor 120 is operated under anoxic conditions, and the second bioactive carbon reactor 130 is operated under aerobic conditions. While air is not supplied to the first bioactive carbon reactor 120 in the first step, organic carbon source and Fe ³⁺ are supplied, and air is supplied to the second bioactive carbon reactor 130 in the first step, while organic carbon source and Fe 3+ are supplied. Carbon source and Fe ³⁺ are not supplied. The organic carbon source, Fe ³⁺ , and air are supplied by the organic carbon source supply device 13 , the Fe ³⁺ supply device 16 , and the air supply pump 12 , respectively.

In a state where the first bioactive carbon reactor 120 maintains anoxic conditions, raw water passes through the first bioactive carbon reactor 120 filled with bioactive carbon, thereby reducing total organic carbon (TOC) and total nitrogen (T-N) contained in the raw water. ) is removed. Total organic carbon (TOC) is adsorbed on bioactive carbon and decomposed/ingested by microorganisms attached to the activated carbon to be removed, and total nitrogen (T-N) is organic matter available in raw water and an external organic carbon source supplied from an organic carbon source supply device. It is removed by denitrifying bacteria.

In addition, Fe ³⁺ is supplied to the first bioactive carbon reactor 120 operated under anoxic conditions in the first step, and Fe ³⁺ is produced by the bacteria in the reactor serving as electron shuttles to reduce Fe 3+. It is reduced to ²⁺ , and in the process of reducing Fe ³⁺ to Fe ²⁺ by bacteria reducing non-degradable organic matter, the non-degradable organic matter is decomposed. In addition, Fe ³⁺ that is not reduced to Fe ²⁺ acts as a coagulant to remove non-decomposable organic substances and total phosphorus (TP).

Raw water that has passed through the first bioactive carbon reactor 120 is supplied upstream to the second bioactive carbon reactor 130 through the intermediate water tank 14 along the first path, and as described above, the second bioactive carbon reactor 130 ) must be operated under aerobic conditions, an air supply pump 12 for supplying air to raw water is provided in the first path between the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130. Accordingly, the second bioactive carbon reactor 130 is operated under aerobic conditions, and as the raw water passes through the second bioactive carbon reactor 130, total organic carbon (TOC) and total phosphorus (TP) contained in the raw water are removed. . Total organic carbon (TOC) is adsorbed on bioactive carbon and decomposed/ingested by microorganisms adhering to activated carbon to be removed. Microorganisms (PAO, Phosphorous Accumulating Organism) are removed by luxury uptake greater than the amount released from the second bioactive carbon reactor under aerobic conditions.

In the process of removing total organic carbon (TOC) and total phosphorus (TP) by bioactive carbon in the second bioactive carbon reactor 130 under aerobic conditions, microorganisms inhabit not only the surface of the bioactive carbon but also the internal pores of the bioactive carbon, and biological Since the air supply to the internal pores of the activated carbon is relatively poor, the surface of the bioactive carbon is in an aerobic state, while the internal pores of the bioactive carbon are in an anaerobic or anaerobic state. As such, on the surface of bioactive carbon, total organic carbon (TOC) and total phosphorus (TP) removal and nitrification reaction by heterotrophic bacteria (organic matter removal, phosphorus accumulation, etc.) and autotrophic bacteria (nitrification) proceed. In the internal pore, for total organic carbon (TOC) removal and denitrification by heterotrophic bacteria (removal of organic matter, dephosphorization, denitrification, etc.), it is injected into the bioactive carbon reactor under anoxic conditions in the previous step, adsorbed to the bioactive carbon, and the remaining organic carbon source is used. Denitration occurs continuously. Therefore, in the second bioactive carbon reactor 130 under aerobic conditions, a mechanism for removing not only total organic carbon (TOC) and total phosphorus (TP) but also total nitrogen (T-N) proceeds.

In addition, Fe ²⁺ generated by the reduction reaction in the reaction tank under anoxic conditions flows into the reaction tank under aerobic conditions, and under aerobic conditions, Fe ²⁺ is oxidized to Fe ³⁺ while coagulating recalcitrant organic substances and total phosphorus (TP). Remove.

The first step as described above, that is, a process in which the raw water of the raw water tank 110 sequentially passes through the first bioactive carbon reactor 120 under anoxic conditions and the second bioactive carbon reactor 130 under aerobic conditions along the first path. Through this, total organic carbon (TOC), total nitrogen (TP), and total phosphorus (TP) contained in raw water are removed to produce treated water.

When the treatment water production process through the first step is completed, the treated water production process proceeds through the second step.

As mentioned above, anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria coexist in the bioactive carbon filled in the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, respectively, and these coexisting microorganisms of different characteristics In order to be activated, each of the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 should not be operated only under the same conditions. That is, each of the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 must be operated alternately under anoxic conditions and aerobic conditions. To this end, a second step is carried out, which operates in reverse to the first step.

In the first step, the first bioactive carbon reactor 120 was operated under anoxic conditions and the second bioactive carbon reactor 130 was operated under aerobic conditions. 2 The bioactive carbon reactor 130 is operated under anoxic conditions.

The second step proceeds as follows in detail.

Referring to FIG. 2B, the raw water of the raw water tank 110 in the second step is sequentially passed through the raw water tank 110, the second bioactive carbon reactor 130, the intermediate water tank 14, and the first bioactive carbon reactor 120. It moves along the second path that connects it.

Raw water from the raw water tank 110 is introduced into the second bioactive carbon reactor 130 through the raw water supply pump 11 . Raw water flows upward into the second bioactive carbon reactor 130, and raw water that has passed through the second bioactive carbon reactor 130 is discharged through the top of the second bioactive carbon reactor 130 and flows into the intermediate water tank 14. and is moved toward the first bioactive carbon reactor 120 through the circulation pump 15.

Contrary to the first step, as the second bioactive carbon reactor 130 is operated under anoxic conditions and the first bioactive carbon reactor 120 is operated under aerobic conditions, raw water passes through the second bioactive carbon reactor 130 under anoxic conditions. In the process, total organic carbon (TOC) and total nitrogen (T-N) are removed, and in the first bioactive carbon reactor 120 under aerobic conditions, total organic carbon (TOC), total nitrogen (T-N) and Total phosphorus (TP) is removed. Through this process, the treated water is discharged through the top of the first bioactive carbon reactor 120 .

The mechanism generated in the second bioactive carbon reactor 130 under anoxic conditions is the same as that in the first bioactive carbon reactor 120 under anoxic conditions in the first step, and the first bioactive carbon reactor 120 under aerobic conditions The mechanism generated in is the same as the mechanism that proceeds in the second bioactive carbon reactor 130 under anoxic conditions in the first step.

Through the progress of the first step and the second step, the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 form a form in which the anoxic and aerobic conditions are alternately operated, respectively, and the anoxic conditions of the same reactor are achieved. Through the alternating operation of aerobic and aerobic conditions, various microorganisms, such as anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria, etc. exist in the bioactive carbon of each reaction tank so that nitrogen and phosphorus can be removed, and the amount of microorganisms is smaller than that of the existing activated sludge method Since it is maintained as , it is possible to effectively remove total nitrogen (T-N) even if the C/N ratio of the raw water is maintained low.

In using the water treatment device according to the first embodiment of the present invention, the above-described alternation of the first step and the second step is repeated.

Previously, it was mentioned that the process of preparing bioactive carbon by binding microorganisms to the granular activated carbon filled in the first bioactive carbon tank 120 and the second bioactive carbon tank 130, respectively, before proceeding with the first step, proceeded. If you do the following In addition, only the preparation of bioactive carbon has been mentioned, but not only the preparation of bioactive carbon, but also the process of supplying organic matter to the bioactive carbon is required before proceeding with the first step. Hereinafter, the process of supplying organic matter and preparing bioactive carbon, which is performed before proceeding with the first step, will be referred to as a 'pretreatment step'.

First, the organic carbon source is mixed in the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 while the granular activated carbon is filled in the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, respectively. supply raw water Accordingly, the organic carbon source is adsorbed on the surface and internal pores of the granular activated carbon. At this time, as the organic carbon source, any one or a combination of raw sewage water, molasses, glucose, methanol, ethanol, citric acid, and acetic acid may be used, and the organic carbon source may be supplied from a separate organic carbon source supply device 13 there is.

When the supply of the organic carbon source and the adsorption to the granular activated carbon are completed, the activated sludge is injected into the raw water tank 110, and the raw water mixed with the activated sludge is fed into the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130. supply The activated sludge mixed with the raw water includes anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria, and accordingly, the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 due to the supply of the raw water mixed with the activated sludge Anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria are attached to each granular activated carbon.

In a state in which anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria are attached to each granular activated carbon of the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, the first bioactive carbon reactor 120 and the second bioactive carbon While supplying raw water to each of the reaction tanks 130, air is intermittently injected into the raw water. As air is intermittently injected into the raw water supplied to the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, each of the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 is oxygen-free. state and exhalation state are repeated. In this way, in the process of repeating anoxic and aerobic conditions in each of the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130, anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria attached to the granular activated carbon of each reactor are respectively It grows using organic carbon sources as nutrients under the conditions of, and through this, the preparation of bioactive carbon is completed.

The conversion of granular activated carbon into bioactive carbon is completed through the above-described supply of organic carbon source, supply of activated sludge, and intermittent aeration. When the pretreatment step is completed, the first step is performed, and when the production of the treated water is completed, the second step is performed.

In the above, the water treatment device using the bioactive carbon process according to the first embodiment of the present invention has been described.

On the other hand, when it is determined that the supply of air to make the bioactive carbon reactor into an aerobic state is difficult due to the pressure applied to the lower part of the reactor, or when it is necessary to secure additional phosphorus and organic matter removal efficiency, the first embodiment is modified and, as in the third embodiment, can be configured. As shown in FIG. 6, in the third embodiment, the configuration of the intermediate water tank 14 and the air supply pump 12 of the first embodiment is replaced with a dissolved air flotation (DAF) 140 will be. Raw water that has passed through the first bioactive carbon reactor 120 or the second bioactive carbon reactor 130 under anoxic conditions flows into the dissolved air flotation separation tank 140, and the dissolved air in the dissolved air flotation separation tank 140 After the removal of organic matter and phosphorus is performed by the flotation separation process by, raw water is introduced into the first bioactive carbon reactor 120 or the second bioactive carbon reactor 130 operated under aerobic conditions to obtain the air of the first embodiment. The configuration of the supply pump 12 can be omitted. The operation of the third embodiment is identical to that of the first embodiment, except that the configuration of the air supply pump 12 is omitted. Here, although not shown in the drawing, a micro-bubble generating device for supplying micro-bubbles to the dissolved air flotation separation tank 140 is provided at one side of the dissolved air flotation separation tank 140 . A part of the dissolved air flotation separation tank 140 may be defined as a flocculation tank, and the removal efficiency of organic matter and phosphorus may be increased by introducing a coagulant into the coagulation tank.

Hereinafter, a water treatment device using a bioactive carbon process according to a second embodiment will be described.

Like the first embodiment, the second embodiment is based on two bioactive carbon reactors 220 and 230 as shown in FIG. 3 . While the first embodiment proceeds the process in the order of anoxic operation - aerobic operation in both the first and second steps, the second embodiment proceeds in the order of anoxic operation - aerobic operation according to the concentration of ammonia nitrogen contained in the raw water. Alternatively, it is characterized in that it proceeds in the order of aerobic operation - anoxic operation.

Since raw water, which is concentrated water from the reverse osmosis process, has undergone sewage treatment processes such as nitrification and denitrification, the concentration of ammonia nitrogen is low. However, when a high amount of ammonia nitrogen is introduced into raw water concentrated in the reverse osmosis process due to a problem during the sewage treatment process, ammonia nitrogen needs to be treated with priority. Ammonia nitrogen contained in raw water is converted into nitrate nitrogen and then removed as nitrogen (N ₂ ) by denitrification by anaerobic bacteria. A conversion process needs to be selectively applied. In consideration of this point, the second embodiment of the present invention, when the concentration of ammonia nitrogen is greater than the preset reference value, first sends raw water under aerobic conditions to convert it to nitrate nitrogen and then sends it under anoxic conditions so that denitrification is achieved, and ammonia If the concentration of nitrogenous nitrogen is less than the standard value, the denitrification reaction is induced directly through the anoxic condition for the corresponding raw water. That is, when the ammonia nitrogen is higher than the reference value, the aerobic operation - anoxic operation is performed in the order, and when the ammonia nitrogen is lower than the reference value, the anoxic operation - anoxic operation is performed in the order.

In addition, in order to ensure that anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria exist in each of the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230, the two reactors 220 and 230 each have anoxic conditions and The aerobic condition is operated alternately. This is for the same reason that the first bioactive carbon reactor 120 and the second bioactive carbon reactor 130 are alternately operated under anoxic conditions and aerobic conditions in the first embodiment.

In summary, the second embodiment selectively changes the order of anoxic operation and aerobic operation according to the concentration of ammonia nitrogen in raw water based on the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230, and each In order to ensure that anaerobic bacteria, aerobic bacteria, and conditioned anaerobic bacteria exist in the reactor, the two reactors 220 and 230 are alternately operated under anoxic conditions and aerobic conditions, both when the concentration of ammonia nitrogen is high and low. .

In order to implement this, the water treatment device using the bioactive carbon process according to the second embodiment of the present invention, as shown in FIG. (22), an organic carbon source supply device (23), an ammonia nitrogen measuring device (24), and an Fe ³⁺ supply device (27).

The ammonia nitrogen measuring device 24 is provided on one side of the raw water tank 210 and serves to measure the concentration of ammonia nitrogen contained in the raw water, and the ammonia measured by the ammonia nitrogen measuring device 24 The order of aerobic operation-anoxic operation or anoxic operation-expiratory operation order of the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230 is determined according to the concentration value of nitrogen. As described above, when the concentration of ammonia nitrogen is higher than the preset reference value, the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230 are operated in the order of aerobic operation-anoxic operation, and the concentration of ammonia nitrogen If is lower than the preset reference value, the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230 are operated in the order of anoxic operation-expiratory operation. In addition, in proceeding with the sequence of aerobic operation-anoxic operation or anoxic operation-expiratory operation, the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230 are operated alternately between aerobic and anoxic conditions, respectively. do. This will be described in detail with reference to FIGS. 4a and 4b and FIGS. 5a and 5b to be described later.

On the other hand, as each of the first bioactive carbon reactor 220 and the second bioactive carbon reactor 230 must be operated under anoxic or aerobic conditions, the air supply pump 22 controls the inflow of raw water into the first bioactive carbon reactor 220. Air is selectively supplied to the pathway or the raw water inflow path of the second bioactive carbon reactor 230, and the organic carbon source supply device 23 is also the first bioactive carbon reactor 220 to induce a denitrification reaction in the reactor operated under anoxic conditions. It operates in the form of selectively supplying the organic carbon source to the raw water inflow path of the second bioactive carbon reactor or the raw water inflow path of the second bioactive carbon reactor (230). In addition, the Fe ³⁺ supplying device operates in a form of selectively supplying Fe ³⁺ to a reaction tank operated under anoxic conditions, similarly to the organic carbon source supplying device 23 .

In order to selectively supply air, organic carbon source, and Fe ³⁺ , an air injection opening/closing valve and an organic carbon source are installed in the raw water inflow path of the first bioactive carbon reactor 220 and the raw water inflow path of the second bioactive carbon reactor 230, respectively. An on/off valve for injection and an on/off valve for Fe ³⁺ injection may be provided. For example, when the first bioactive carbon reactor 220 is anoxic operation and the second bioactive carbon reactor 230 is an aerobic operation, air is supplied only to the second bioactive carbon reactor 230, and the organic carbon source and Fe ^{3 +} is supplied only to the first bioactive carbon reactor 220.

In the above, the water treatment device using bioactive carbon according to the second embodiment of the present invention has been described. Next, the operation of the water treatment device using bioactive carbon according to the second embodiment, that is, the operation of the water treatment device according to the concentration of ammonia nitrogen will be described.

4A and 4B show that two reactors are alternately operated between aerobic and anoxic conditions under conditions satisfying that the order of aerobic operation-anoxic operation is performed when the concentration of ammonia nitrogen is higher than the reference value, FIG. 5a and 5b show that the two reactors are alternately operated between anoxic and aerobic conditions under conditions satisfying that the order of anoxic operation and aerobic operation is satisfied when the concentration of ammonia nitrogen is lower than the reference value.

First, the case where the concentration of ammonia nitrogen is higher than the reference value will be described with reference to FIGS. 4A and 4B. Both FIGS. 4A and 4B proceed in the order of aerobic operation and anoxic operation, and FIG. 4a shows a case in which the first bioactive carbon reactor 220 is in the aerobic operation and the second bioactive carbon reactor 230 is in the anoxic operation. 4B shows a case where the second bioactive carbon reactor 230 is in an aerobic operation and the first bioactive carbon reactor 220 is in an anaerobic operation.

Referring to FIG. 4A , the raw water of the raw water tank 210 flows upward into the first bioactive carbon reactor 220 . At this time, air is injected into the raw water supply passage of the first bioactive carbon reactor 220 by the air supply pump 22, and thus the first bioactive carbon reactor 220 is operated under aerobic conditions.

Raw water that has passed through the first bioactive carbon reactor 220 is supplied to the second bioactive carbon reactor 230 through the intermediate water tank 25 and the circulation pump 26 . At this time, air is not supplied to the raw water supply passage of the second bioactive carbon reactor 230, and the organic carbon source supply device 23 and the Fe ³⁺ supply device are installed in the raw water supply passage of the second bioactive carbon reactor 230. Through this, organic carbon source and Fe ³⁺ are supplied. Therefore, the second bioactive carbon reactor 230 is operated under an anoxic condition.

Since the mechanism of the reactor under aerobic conditions and the mechanism of the reactor under anoxic conditions are the same as those of the first embodiment, a detailed description thereof will be omitted.

When the aerobic operation of the first bioactive carbon reactor 220 and the anoxic operation of the second bioactive carbon reactor 230 are completed time-sequentially as shown in FIG. 4A, the second bioactive carbon reactor as shown in FIG. 4B ( The aerobic operation of 230) and the anoxic operation of the first bioactive carbon reactor 220 proceed sequentially.

Referring to FIG. 4B, raw water from the raw water tank 210 flows into the second bioactive carbon reactor 230 and is supplied to the first bioactive carbon reactor 220 via the intermediate water tank 25 and the circulation pump 26, Air is supplied only to the second bioactive carbon reactor 230 operated under aerobic conditions, and organic carbon source and Fe ³⁺ are supplied only to the first bioactive carbon reactor 220 operated under anoxic conditions.

Next, the case where the concentration of ammonia nitrogen is lower than the reference value will be described with reference to FIGS. 5A and 5B. Both FIGS. 5A and 5B proceed in the order of anoxic operation-expiratory operation, and FIG. 5A shows a case in which the first bioactive carbon reactor 220 is anoxic operation and the second bioactive carbon reactor 230 is an aerobic operation. 5B shows a case where the second bioactive carbon reactor 230 is anoxic operation and the first bioactive carbon reactor 220 is an aerobic operation.

Referring to FIG. 5A , the raw water of the raw water tank 210 is introduced into the first bioactive carbon reactor 220 as an upstream flow. At this time, since the raw water supply passage of the first bioactive carbon reactor 220 is not supplied, the first bioactive carbon reactor 220 is operated in an oxygen-free condition, and the raw water supply passage of the first bioactive carbon reactor 220 also contains an organic carbon source. The organic carbon source and Fe ³⁺ are supplied through the supply device 23 and the Fe ³⁺ supply device 27 .

Raw water that has passed through the first bioactive carbon reactor 220 is supplied to the second bioactive carbon reactor 230 through the intermediate water tank 25 and the circulation pump 26 . At this time, air is injected into the raw water supply passage of the second bioactive carbon reactor 230 by the air supply pump 22, and thus the second bioactive carbon reactor 230 is operated under aerobic conditions.

When the anoxic operation of the first bioactive carbon reactor 220 and the aerobic operation of the second bioactive carbon reactor 230 are completed time-sequentially as shown in FIG. 5A, the second bioactive carbon reactor as shown in FIG. 5B ( The anoxic operation of 230) and the aerobic operation of the first bioactive carbon reactor 220 proceed sequentially.

Referring to FIG. 5B, the raw water of the raw water tank 210 flows into the second bioactive carbon reactor 230 and is supplied to the first bioactive carbon reactor 220 via the intermediate water tank 25 and the circulation pump 26, Air is supplied only to the first bioactive carbon reactor 220 operated under aerobic conditions, and organic carbon source and Fe ³⁺ are supplied only to the second bioactive carbon reactor 230 operated under anoxic conditions.

Meanwhile, in the water treatment apparatus of the second embodiment, as in the first embodiment, a pretreatment step is applied before proceeding with the water treatment process according to the ammonia nitrogen concentration, and bioactive carbon is prepared in advance by the pretreatment step. In the pretreatment step of the second embodiment, bioactive carbon is prepared through the process of supplying organic carbon source, supplying activated sludge, and intermittent aeration in the same manner as the pretreatment step of the first embodiment.

In the above, the water treatment apparatus using the bioactive carbon according to the first to third embodiments of the present invention has been described.

In the process of performing the water treatment process according to the first to third embodiments, backwashing is required at regular intervals for the first bioactive carbon reactor and the second bioactive carbon reactor. To this end, an aeration pipe is provided in each of the first bioactive carbon reactor and the second bioactive carbon reactor, and the backwashing process proceeds as follows. When air at a certain pressure is injected into the first bioactive carbon reactor and the second bioactive carbon reactor, respectively, a layer separation phenomenon occurs in the bioactive carbon. In such a state, when backwashing water is supplied upstream to the reaction tank along with injecting air through the diffuser pipe, suspended solids and overgrown microorganisms present in the bioactive carbon are desorbed. The reason for inducing the layer separation phenomenon in the bioactive carbon is to facilitate the desorption of suspended matter and overgrown microorganisms.

Hereinafter, the present invention will be described in more detail through experimental examples.

First, with the C/N ratio fixed at 3.5, the pollutant treatment efficiency of each of the water treatment device according to the first embodiment of the present invention and the water treatment device according to the prior art was examined. Table 1 below shows the results of comparing the pollutant treatment efficiency of the prior art SBR process with the pollutant treatment efficiency of the water treatment device according to the first embodiment of the present invention. Also, in Table 1, the alternating operation is the average value of the number of processes in the first stage and the number of processes in the second stage, and the one-way operation shows a case in which only the first stage is applied. In addition, the prior art SBR process consists of an aerobic operation and an anoxic operation.

division invention technology Existing SBR process
(HRT 8hrs) alternating driving one-way driving process Alternating Operation (Anoxic/Expiratory) anoxic → expiratory expiratory → anoxic removal rate
(%) TOC 50% 50% 13% T-N 85% 50% 50% T-P 40% 25% 35%

Referring to Table 1, it can be seen that the water treatment apparatus according to the first embodiment of the present invention is superior to the prior art SBR process in all of total organic carbon (TOC), total nitrogen (T-N) and total phosphorus (TP). In particular, when the alternating operation is applied, it can be confirmed that the total nitrogen (T-N) and total phosphorus (TP) removal characteristics are significantly improved.

Next, the total nitrogen (T-N) treatment efficiency of each water treatment device according to the C/N ratio was examined. Referring to Table 2 below, it can be seen that the water treatment apparatus according to the first embodiment of the present invention is superior to the prior art SBR process at C/N ratios of 1.2, 2.5, 3.5, and 5.3, respectively. In addition, in this experiment, it can be confirmed that the pollutant treatment efficiency is further improved when the alternating operation is applied. In particular, in the case of alternating operation, the total nitrogen (T-N) removal efficiency was 75% even when the C/N ratio was set at 2.5, which was superior to the existing SBR process applied at the C/N ratio of 5.3.

division C/N ratio 1.2 2.5 3.5 5.3 invention technology alternating driving 50% 75% 85% 99%
(C/N ratio 4.4) one-way driving 40% 44% 50% 88% Existing SBR process - 23% 50% 70%

11, 21: raw water supply pump 12, 22: air supply pump
13, 23: organic carbon source supply device 14, 25: intermediate water tank
15, 26: circulation pump 16, 27: Fe ³⁺ supply device
24: ammonia nitrogen measuring device
110, 210: raw water tank 120, 220: first bioactive carbon reactor
130, 230: second bioactive carbon reactor 140: dissolved air flotation separation tank

Claims (8)

A first bioactive carbon reactor and a second bioactive carbon reactor that are disposed adjacent to each other and sequentially treat raw water,
The first bioactive carbon reactor and the second bioactive carbon reactor are operated alternately under anoxic conditions and aerobic conditions, respectively.
Raw water is treated sequentially through an anoxic reaction tank and an aerobic reaction tank.
Since each of the first and second bioactive carbon reactors is alternately operated under anoxic conditions and aerobic conditions, the bioactive carbon filled in the first and second bioactive carbon reactors can generate anaerobic bacteria, aerobic bacteria, and anaerobic conditions. fungi coexist,
An air supply pump supplying air to the raw water inflow path of the reaction tank operated under aerobic conditions;
An organic carbon source supply device for supplying an organic carbon source to a raw water inflow path of a reactor operated under anoxic conditions;
Fe ³⁺ supply device for supplying Fe ³⁺ to the raw water inflow path of the reactor operated under anoxic conditions; further comprising;
The Fe ³⁺ supply device is a water treatment device using bioactive carbon, characterized in that for supplying a biodegradable chelate material and Fe ³⁺ together or by mixing Fe ³⁺ with supply water of pH 2 or less.
delete The water treatment device using bioactive carbon according to claim 1, further comprising a circulation water tank for storing raw water that has passed through the reaction tank under anoxic conditions, and a circulation pump for supplying raw water from the circulation water tank to the reaction tank under aerobic conditions.
A first bioactive carbon reactor and a second bioactive carbon reactor that are disposed adjacent to each other and sequentially treat raw water,
The first bioactive carbon reactor and the second bioactive carbon reactor are operated alternately under anoxic conditions and aerobic conditions, respectively.
Raw water is treated sequentially through an anoxic reaction tank and an aerobic reaction tank.
Since each of the first and second bioactive carbon reactors is alternately operated under anoxic conditions and aerobic conditions, the bioactive carbon filled in the first and second bioactive carbon reactors can generate anaerobic bacteria, aerobic bacteria, and anaerobic conditions. fungi coexist,
An organic carbon source supply device for supplying an organic carbon source to a raw water inflow path of a reactor operated under anoxic conditions;
Fe ³⁺ supply device for supplying Fe ³⁺ to the raw water inflow path of the reactor operated under anoxic conditions; further comprising;
The Fe ³⁺ supply device supplies a biodegradable chelate material and Fe ³⁺ together or mixes and supplies Fe ³⁺ with supply water having a pH of 2 or less,
A dissolved air flotation separation tank is further provided on the path between the first bioactive carbon reactor and the second bioactive carbon reactor,
The dissolved air flotation separation tank is supplied with raw water that has passed through a reaction tank under anoxic conditions, and uses dissolved air to treat organic matter and phosphorus in the raw water,
A water treatment device using bioactive carbon, characterized in that the raw water discharged from the dissolved air flotation separation tank is supplied to the reaction tank under aerobic conditions.
The method of claim 1 or 4, wherein the bioactive carbon,
While the first and second bioactive carbon reactors are filled with granular activated carbon, raw water mixed with an organic carbon source is supplied to the first and second bioactive carbon reactors to form organic compounds on the surface and internal pores of the granular activated carbon. A process of adsorbing a carbon source;
Supplying raw water mixed with activated sludge to a first bioactive carbon reactor and a second bioactive carbon reactor to attach anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria to the surface and internal pores of the granular activated carbon;
In addition to supplying raw water to the first and second bioactive carbon reactors, air is intermittently supplied to each of the first and second bioactive carbon reactors to generate anaerobic bacteria and aerobic aerobic bacteria attached to the surface and internal pores of the granular activated carbon. Water treatment device using a bioactive carbon process, characterized in that prepared through the process of growing sexual bacteria and condition anaerobic bacteria.
A first bioactive carbon reactor and a second bioactive carbon reactor that are disposed adjacent to each other and sequentially treat raw water,
The first bioactive carbon reactor and the second bioactive carbon reactor are operated alternately under anoxic conditions and aerobic conditions, respectively.
If the concentration of ammonia nitrogen in the raw water is higher than the preset reference value, the raw water is treated by sequentially passing through a reaction tank under aerobic conditions and a reaction tank under anoxic conditions,
If the concentration of ammonia nitrogen in the raw water is lower than the preset reference value, the raw water is treated by sequentially passing through a reactor under anoxic conditions and a reactor under aerobic conditions,
Since each of the first and second bioactive carbon reactors is alternately operated under anoxic conditions and aerobic conditions, the bioactive carbon filled in the first and second bioactive carbon reactors can generate anaerobic bacteria, aerobic bacteria, and anaerobic conditions. A water treatment device using bioactive carbon, characterized in that bacteria coexist.
According to claim 6, Ammonia nitrogen measuring device for measuring the concentration of ammonia nitrogen in raw water;
An air supply pump supplying air to the raw water inflow path of the reaction tank operated under aerobic conditions;
An organic carbon source supply device for supplying an organic carbon source to a raw water inflow path of a reactor operated under anoxic conditions;
Fe ³⁺ supply device for supplying Fe ³⁺ to the raw water inflow path of the reactor operated under anoxic conditions; further comprising;
The Fe ³⁺ supply device is a water treatment device using bioactive carbon, characterized in that for supplying a biodegradable chelate material and Fe ³⁺ together or by mixing Fe ³⁺ with supply water of pH 2 or less.
The method of claim 6, wherein the bioactive carbon,
While the first and second bioactive carbon reactors are filled with granular activated carbon, raw water mixed with an organic carbon source is supplied to the first and second bioactive carbon reactors to form organic compounds on the surface and internal pores of the granular activated carbon. A process of adsorbing a carbon source;
Supplying raw water mixed with activated sludge to a first bioactive carbon reactor and a second bioactive carbon reactor to attach anaerobic bacteria, aerobic bacteria, and conditional anaerobic bacteria to the surface and internal pores of the granular activated carbon;
In addition to supplying raw water to the first and second bioactive carbon reactors, air is intermittently supplied to each of the first and second bioactive carbon reactors to generate anaerobic bacteria and aerobic aerobic bacteria attached to the surface and internal pores of the granular activated carbon. Water treatment device using a bioactive carbon process, characterized in that prepared through the process of growing sexual bacteria and condition anaerobic bacteria.

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