JP2012040534A - Wastewater treatment system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a wastewater treatment system in which the enlargement preventing of an apparatus and the running cost increase preventing are possible, and which can process wastewater highly efficiently and stably.SOLUTION: The wastewater treatment system includes: an aeration tank 100 in which an organic compound is volatilization-removed from a wastewater containing the organic compound, the wastewater is made to discharge as a primary treated water, and an aeration gas containing the organic compound is discharged; a wastewater treatment apparatus 200 in which by contacting the primary treated water with adsorption elements 211, 221, the organic compound is made to be adsorbed and the primary treated water is discharged as a secondary treated water, the adsorption elements 211, 221 are supplied with a heated gas, thereby the organic compound is desorbed from the adsorption elements, and the gas is discharged as a desorption gas containing the organic compound; an activated sludge treatment apparatus 300 in which the secondary treated water is made contact with an activated sludge, thereby the organic compound is decomposed and removed, and the secondary treated water is discharged as a tertiary treated water; and a combustion apparatus 400 in which a mixed exhaust gas of the aeration gas and the desorption gas discharged from the aeration tank and the wastewater treatment apparatus is burned, and oxidation-decomposed, and the decomposed gas is discharged.

Description

  The present invention relates to a wastewater treatment system that normalizes the wastewater by removing the organic compound from the wastewater containing the organic compound, and in particular, the organic wastewater from the industrial wastewater containing the organic compound discharged from various factories and research facilities. The present invention relates to a wastewater treatment system that purifies industrial wastewater by efficiently removing compounds.

  Conventionally, an activated sludge treatment apparatus has been used as a wastewater treatment apparatus for purifying wastewater containing organic compounds. The activated sludge treatment apparatus is an apparatus for purifying waste water using activated sludge mainly containing aerobic microorganisms such as bacteria (bacteria), protozoa, metazoans, etc. It is disclosed.

  The activated sludge treatment apparatus supplies the wastewater to the above-mentioned activated sludge, and agitates and aerates it to decompose and remove the organic compounds contained in the wastewater using microorganisms, thereby separating the activated sludge. It is a device that cleans and discharges clean water.

  In the activated sludge treatment apparatus described above, since microorganisms are used for decomposing organic compounds, it is very difficult to continuously and stably maintain conditions suitable for the microorganisms to decompose organic compounds. In the case of a wastewater treatment system equipped with such an activated sludge treatment apparatus, there is a problem that it is difficult to stably maintain wastewater treatment capacity.

  In addition, when treating wastewater containing a high concentration of organic compounds that are hardly degradable to microorganisms or organic compounds that are highly toxic to microorganisms, it is very difficult to clean the wastewater only with an activated sludge treatment apparatus. For example, when wastewater containing 1,4-dioxane is treated, since a general microorganism cannot decompose 1,4-dioxane at all, a treatment method other than activated sludge treatment is required.

  As a method for removing an organic compound that is difficult to treat with activated sludge, a wastewater treatment apparatus using an adsorbent is widely known. For example, it is generally performed using an exchangeable wastewater treatment apparatus using cartridge-type activated carbon as an adsorbent. In this case, organic compounds contained in the wastewater are converted into cartridge-type activated carbon. It is removed and discharged from the exchangeable wastewater treatment device as clean water.

  However, in the exchangeable wastewater treatment device, if the adsorption capacity of the adsorbent reaches saturation by continuing to adsorb the organic compound for a certain period of time, the adsorption is not substantially performed thereafter, and replacement work with a new one, or once An operation of removing the adsorbent from the apparatus and performing a regeneration process is required. Therefore, in the case of a wastewater treatment system in which an exchangeable wastewater treatment device and an activated sludge treatment device are connected, the water cannot be treated continuously, and it is necessary to stop the wastewater treatment system itself each time. It was.

  In addition, unlike the purification of air, the purification of water inevitably causes the growth of microorganisms, and the life of the adsorbent is shortened. Therefore, in the case of a wastewater treatment system in which an exchangeable wastewater treatment device and an activated sludge treatment device are connected, it is necessary to frequently perform the above-described adsorption material replacement work and regeneration treatment work. There was also a problem that increased.

  In addition, when a large amount of wastewater containing organic compounds at high concentration is treated with activated sludge treatment equipment, the amount of activated sludge required will increase accordingly. The increase of becomes inevitable. In addition, in activated sludge treatment equipment, it is necessary to constantly adjust and optimize the amount of activated sludge according to the amount of organic compounds contained in the wastewater to be treated. It is necessary to always collect and discharge from the apparatus, and there is a problem that it takes time and money to dispose of this excess sludge. Therefore, when the amount of activated sludge is increased as described above, there is a problem that the amount of surplus sludge to be discarded also increases, and the running cost increases significantly.

JP-A-9-10791

  The present invention has been made to solve the above-described problems, and can prevent the increase in the size of the activated sludge treatment apparatus and increase in running cost. The organic compound has low biodegradability without stopping the system. It is an object of the present invention to provide a wastewater treatment system that can continuously purify wastewater and can efficiently and stably treat wastewater.

As a result of intensive studies in order to solve the above problems, the present inventors have finally completed the present invention. That is, the present invention is as follows.
1. A wastewater treatment system for purifying wastewater by removing organic compounds from wastewater containing organic compounds,
By aeration treatment of wastewater containing organic compounds, it is discharged as primary treated water from which organic compounds are volatilized and removed from the wastewater, and an aeration tank for discharging aeration gas containing organic compounds,
It includes an adsorbing element that adsorbs the organic compound by contacting the primary treated water containing the organic compound and desorbs the adsorbed organic compound by contacting the heated gas, and supplies the primary treated water to the adsorbing element. The organic compound is adsorbed on the adsorption element and discharged as secondary treated water, and the heated gas is supplied to the adsorption element so that the organic compound is desorbed from the adsorption element and discharged as a desorption gas containing the organic compound. The portion where the adsorption element has been desorbed is transferred to the portion where the adsorption process is performed, and the portion where the adsorption process of the adsorption element is completed is shifted to the portion where the desorption process is performed, so that the secondary treated water is continuously obtained. Wastewater treatment equipment capable of treating
Activated sludge treatment that has activated sludge containing microorganisms that decompose organic compounds, and decomposes and removes organic compounds by microorganisms by bringing the secondary treated water into contact with the activated sludge and discharges it as tertiary treated water Equipment,
Combustion connected to the aeration tank and the wastewater treatment apparatus, and combusting a mixed exhaust gas of an aeration gas and a desorption gas containing an organic compound discharged from the aeration tank and the wastewater treatment apparatus to oxidatively decompose and discharge decomposition gas Wastewater treatment system equipped with a device.
2. 2. The waste water treatment system according to 1 above, wherein the waste water treatment apparatus blows off excess waste water adhering to the adsorption element by blowing gas to the adsorption element and discharges it as removed waste water.
3. 3. The waste water treatment system according to 2 above, wherein the removed waste water discharged from the waste water treatment device is again supplied to the waste water treatment device as waste water.
4). 4. The wastewater treatment system according to any one of 1 to 3, wherein the adsorption element includes at least one adsorbent selected from the group consisting of activated carbon, activated carbon fiber, and zeolite.
5. 5. The wastewater treatment system according to any one of 1 to 4 above, wherein the cracked gas discharged from the combustion device is subjected to heat exchange, and the heated gas of the wastewater treatment device is preheated.

  According to the present invention, it is possible to prevent the activated sludge treatment apparatus from increasing in size and to prevent an increase in running cost, and it is possible to continuously purify drainage without stopping the system. It can be set as the waste water treatment system which can process the waste_water | drain containing in high concentration highly efficiently and stably.

1 is a system configuration diagram of a wastewater treatment system according to Embodiment 1 of the present invention. It is a schematic diagram which shows the example of the other waste water treatment equipment which can be utilized in the waste water treatment system in Embodiment 1 of this invention. It is a schematic diagram which shows the example of the further another waste water treatment apparatus which can be utilized in the waste water treatment system in Embodiment 1 of this invention. It is a system block diagram of the waste water treatment system in Embodiment 2 of this invention. It is a system block diagram of the waste water treatment system in Embodiment 3 of this invention.

  Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings. In the following embodiments, the same or corresponding parts are denoted by the same reference numerals in the drawings, and description thereof will not be repeated.

(Embodiment 1)
FIG. 1 is a system configuration diagram of a wastewater treatment system according to Embodiment 1 of the present invention. Below, with reference to this FIG. 1, the structure of the waste water treatment system 1A in this Embodiment is demonstrated.

  As shown in FIG. 1, the wastewater treatment system 1A in the present embodiment mainly includes an aeration tank 100, a wastewater treatment device 200, an activated sludge treatment device 300, and a combustion device 400.

  The aeration tank 100 includes an aeration device 111 that generates bubbles and a heating device 112 that heats drainage to a predetermined temperature. The aeration tank 100 supplies wastewater containing an organic compound from the piping line L1, whereby the organic compound in the wastewater is volatilized and the wastewater from which the organic compound is volatilized is discharged from the piping line L2. The piping lines L3 and L4 are piping lines for removing the organic compound from the waste water by volatilizing and removing it as aerated gas containing the organic compound by introducing the gas into the aeration device 111.

  In the aeration tank 100, it is preferable that the waste water is heated to a predetermined temperature using the heating device 112 and aerated. This is because the volatilization amount of the organic compound in the wastewater is further increased by heating, and the organic compound can be removed from the wastewater. The method for heating wastewater in the aeration tank 100 is not particularly limited. A piping line may be provided to directly feed steam into the aeration tank 100, or an aeration tank structure may be used in which the waste water is heated indirectly using steam, or the waste water is discharged using an electric heater. It may be heated.

  The wastewater treatment apparatus 200 has a first treatment tank 210 and a second treatment tank 220 in which adsorbents 211 and 221 as adsorption elements are accommodated, respectively. The adsorbents 211 and 221 adsorb the organic compound contained in the primary treated water by contacting the primary treated water containing the organic compound. Therefore, in the waste water treatment apparatus 200, the organic compound is adsorbed by the adsorbents 211 and 221 by supplying the adsorbents 211 and 221 with waste water containing an organic compound, whereby the waste water is cleaned and the secondary treatment is performed. It will be discharged as water. Moreover, the adsorbents 211 and 221 desorb the adsorbed organic compound by contacting the heated gas. Therefore, in the wastewater treatment apparatus 200, the organic compound is desorbed from the adsorbents 211 and 221 by supplying the heating gas to the adsorbents 211 and 221. Thereby, the heated gas is discharged as a desorption gas containing the organic compound. It will be.

  Piping lines L2, L5, L6, and L7 are connected to the first processing tank 210 and the second processing tank 220, respectively. The piping line L2 is a piping line for supplying primary treatment water containing organic compounds discharged from the aeration tank 100 to the first treatment tank 210 and the second treatment tank 220. The first line is provided by valves V201 and V202. The connection / disconnection state with respect to the processing tank 210 and the second processing tank 220 is switched. The piping line L6 is a piping line for supplying heated gas to the first processing tank 210 and the second processing tank 220, and is connected / disconnected to the first processing tank 210 and the second processing tank 220 by valves V203 and V204. The state is switched. The pipe line L5 is a pipe for discharging secondary treated water from the first treatment tank 210 and the second treatment tank 220, and is connected / not connected to the first treatment tank 210 and the second treatment tank 220 by valves V205 and V206. The connection status is switched. The piping line L7 is a piping line for discharging the desorption gas from the first processing tank 210 and the second processing tank 220, and is connected / disconnected to the first processing tank 210 and the second processing tank 220 by valves V207 and V208. The state is switched.

  The first treatment tank 210 and the second treatment tank 220 function alternately as an adsorption tank and a desorption tank by operating the above-described opening and closing of the valves V201 to V208. Specifically, the first treatment tank 210 is adsorbed. When functioning as a tank, the second processing tank 220 functions as a desorption tank, and when the first processing tank 210 functions as a desorption tank, the second processing tank 220 functions as an adsorption tank. . That is, the waste water treatment apparatus 200 in the present embodiment is configured such that the adsorption tank and the desorption tank are alternately switched over time. The pipe line L2 is connected to a tank functioning as an adsorption tank among the first treatment tank 210 and the second treatment tank 220, and supplies primary treated water to the adsorption tank. Of the first treatment tank 210 and the second treatment tank 220, the heated gas is supplied to the desorption tank connected to a tank functioning as a desorption tank. In addition, the piping line L5 is connected to a tank functioning as an adsorption tank among the first treatment tank 210 and the second treatment tank 220, and discharges secondary treated water from the adsorption tank. The first treatment tank 210 and the second treatment tank 220 are connected to a tank functioning as a desorption tank, and the desorption gas is discharged.

  The adsorbents 211 and 221 are made of an adsorbent containing at least one of activated carbon, activated carbon fiber, and zeolite. As suitable adsorbents 211 and 221, activated carbon or zeolite having a granular shape, a granular shape, or a honeycomb shape is used. More preferably, activated carbon fibers are used. Since the activated carbon fiber has a fibrous structure having micropores on the surface, the contact efficiency with water is high, and the adsorption rate of organic compounds in water is particularly high, which is extremely high compared to other adsorption elements. It is a member that can realize adsorption efficiency.

The physical properties of the activated carbon fibers that can be used as the adsorbents 211 and 221 are not particularly limited, but the BET specific surface area is 700 to 2000 m ² / g, and the pore volume is 0.4 to 0.9 cm ³ / g. The average pore diameter is preferably 17 to 18 mm. This is because when the BET specific surface area is less than 700 m ² / g, the pore volume is less than 0.4 m ³ / g, and the average pore diameter is less than 17 mm, the adsorption amount of the organic compound is lowered, and the BET ratio When the surface area exceeds 2000 m ² / g, the pore volume exceeds 0.9 m ³ / g, and the average pore diameter exceeds 18 mm, the adsorption capacity for substances with small molecular weight decreases due to the large pore diameter. This is because the strength becomes weak, the cost of the material becomes high, and it becomes economically disadvantageous.

  The activated sludge treatment apparatus 300 mainly includes an aeration tank 310 and a sedimentation tank 320. The aeration tank 310 includes an aeration apparatus 311 and an agitation apparatus (not shown), and the inside of the aeration tank 310 is filled with activated sludge containing aerobic microorganisms such as bacteria, protozoa, and metazoans. Has been. The aeration tank 310 supplies the secondary treated water discharged from the waste water treatment apparatus 200 to the activated sludge described above to bring the activated sludge into contact with the secondary treated water, and then agitates and aerates the secondary sludge. This is a treatment tank for decomposing and removing organic compounds contained in treated water. On the other hand, the sedimentation tank 320 is a treatment tank for separating the water containing activated sludge treated in the aeration tank 310 into activated sludge and tertiary treated water by solid-liquid separation.

  Piping lines L5, L9, L10, L11, L12, and L13 are connected to the activated sludge treatment apparatus 300. The piping line L5 is a piping line for supplying secondary treated water to the aeration tank 310, and the piping line L9 is a piping line for supplying oxygen to the aeration apparatus 311. The piping line L <b> 10 is a piping line for discharging water containing activated sludge from the aeration tank 310 and supplying it to the sedimentation tank 320. The piping line L11 is a piping line for discharging the surplus of the activated sludge discharged from the settling tank 320 as excess sludge, and the piping line L12 is the activated sludge discharged from the settling tank 320. This is a piping line for returning the necessary amount to the aeration tank 310 as return sludge. The piping line L13 is a piping line for discharging tertiary treated water from the sedimentation tank 320.

  In the activated sludge treatment apparatus 300, the secondary treated water supplied to the aeration tank 310 via the piping line L5 is mixed with the activated sludge in the aeration tank 310, and the mixed waste water and the activated sludge are connected to the piping line. The organic compound is decomposed by being agitated while being aerated by oxygen supplied to the aeration apparatus 311 through L9 and discharged from the aeration apparatus 311, and water containing activated sludge after decomposition passes through the piping line L10. To the sedimentation tank 320, solid-liquid separation is performed in the sedimentation tank 320, and the supernatant liquid is discharged as tertiary treated water through the piping line L13. The tertiary treated water discharged from the activated sludge treatment apparatus 300 has a significantly reduced organic compound content compared to the secondary treated water supplied to the activated sludge treatment apparatus 300, and can be discharged into rivers and sewage. It has been cleaned to the level.

  The combustion device 400 is a device for burning and oxidizing and decomposing a mixed exhaust gas of the aeration gas discharged from the aeration tank 100 and the desorption gas discharged from the waste water treatment device 200, and piping lines L8, L14, L15, L16. It is connected to the. The combustion apparatus 400 includes a heat exchanger 410 and a heating furnace 420. The heat exchanger 410 is for preheating a mixed exhaust gas of aeration gas and desorption gas introduced into the heating furnace 420. The heating furnace 420 is for burning the mixed exhaust gas introduced using the electric heater 421. The piping line L8 is used for mixing the aeration gas discharged from the piping line L4 of the aeration tank 100 and the desorption gas discharged from the piping line L7 of the waste water treatment apparatus 200, and supplying the mixed gas to the heat exchanger 410. The piping line L14 is a piping line for introducing the desorption gas preheated by the heat exchanger 410 into the heating furnace 420. In addition, the piping lines L15 and L16 are piping lines for discharging cracked gas generated when the mixed exhaust gas burns in the heating furnace 420 to the outside via the heat exchanger 410.

  The type of the combustion apparatus 400 is not particularly limited. For example, a direct combustion apparatus that directly oxidatively decomposes mixed exhaust gas at a high temperature of 650 to 800 ° C. or a mixed exhaust gas using a platinum catalyst or the like is used. A catalytic combustion device that oxidatively decomposes by catalytic oxidation reaction, a heat storage direct combustion device that performs direct oxidative decomposition economically while performing heat recovery using a heat storage body, and a combination of a platinum catalyst and a heat storage body efficiently It is possible to use a regenerative catalytic combustion apparatus that oxidizes and decomposes the mixed exhaust gas through a catalytic oxidation reaction. The organic compound is completely removed by oxidizing and decomposing the mixed exhaust gas using the combustion apparatus 400.

  Next, with reference to FIG. 1, the details of the waste water cleaning process performed in the waste water treatment system 1A in the present embodiment will be described. The following description is based on the state where the first treatment tank 210 of the waste water treatment apparatus 200 functions as an adsorption tank and the second treatment tank 220 functions as a desorption tank. The same process is performed when the desorption tank is replaced.

  As shown in FIG. 1, the waste water containing an organic compound is introduced into the aeration tank 100 via a piping line L1. The introduced waste water is heated and aerated, and the organic compound is removed from the waste water by volatilizing from the waste water. The water after the organic compound is removed is introduced into the piping line L2 as primary treated water. It is discharged from the aeration tank 100.

  The primary treated water discharged from the aeration tank 100 is introduced into the waste water treatment apparatus 200 via the piping line L2. The introduced primary treated water is sent to the first treatment tank 210 and comes into contact with the adsorbent 211, and the organic compound contained in the primary treated water is adsorbed by the adsorbent 211. The water after the organic compound is adsorbed by the adsorbent 211 is introduced into the piping line L5 and discharged from the waste water treatment apparatus 200 as secondary treated water.

  On the other hand, a heating gas is introduced into the waste water treatment apparatus 200 via the piping line L6 in parallel with the introduction of the primary treated water. The introduced heated gas is sent to the second treatment tank 220 and comes into contact with the adsorbent 221 to desorb the organic compound adsorbed on the adsorbent 221. The heated gas containing the organic compound desorbed from the adsorbent 221 is introduced into the piping line L7 and discharged from the waste water treatment apparatus 200 as a desorbed gas.

  The secondary treated water discharged from the waste water treatment apparatus 200 is introduced into the activated sludge treatment apparatus 300 via the piping line L5. The introduced secondary treated water is brought into contact with activated sludge so that the organic compound contained in the wastewater is decomposed and removed, and the water after the organic compound is removed is introduced into the piping line L13. It is discharged from the activated sludge treatment apparatus 300 as tertiary treated water. The discharged tertiary treated water is then treated as river discharge or normal sewage.

  The aerated gas discharged from the aeration tank 100 and the desorbed gas discharged from the waste water treatment device 200 are sent to the combustion device 400 as mixed exhaust gas in the piping line L8, and are oxidatively decomposed by burning in the heating furnace 420. . The cracked gas generated in the heating furnace 420 is introduced into the piping line L16 and discharged from the combustion device 400. This cracked gas is harmless to the human body mainly containing carbon dioxide and water vapor.

  By using the wastewater treatment system 1A as described above, the aeration tank 100 and the wastewater treatment device 200 function as pretreatment devices for the activated sludge treatment device 300, and a wastewater treatment system is constructed using only the activated sludge treatment device 300. Compared with the case where the activated sludge treatment apparatus 300 does not reduce the load of the organic compound in the wastewater, the biodegradation by the activated sludge is particularly difficult, or the organic compound highly toxic to microorganisms is aerated. Since it is removed by the tank 100 and the waste water treatment apparatus 200, the processing capacity of the cleaning treatment as the whole waste water treatment system 1A can be improved. Therefore, the activated sludge treatment apparatus 300 can be prevented from increasing in size and running costs can be prevented, and a wastewater treatment system capable of treating wastewater with high efficiency and stability can be obtained.

  In addition, by using the wastewater treatment system 1A as described above, primary treated water discharged from the wastewater treatment device 200 can be continuously treated in the activated sludge treatment device 300, and therefore the system is stopped. It is possible to continuously clean the waste water. Therefore, compared with the case where an exchangeable wastewater treatment apparatus equipped with a cartridge-type adsorbent is used as a pretreatment device for the activated sludge treatment apparatus 300, the cartridge-type adsorbent is replaced with a new one or removed and regenerated. Is not required, and the labor and running costs are not increased.

  Moreover, by using the wastewater treatment system 1A as described above, the adsorption treatment and the desorption treatment are alternately and continuously repeated in the first treatment tank 210 and the second treatment tank 220 of the wastewater treatment apparatus 200. Thus, by comprising so that adsorption | suction processing and desorption processing may be repeated alternately and continuously, the organic compound contained in waste_water | drain can be removed stably with high capability at low cost. Therefore, by adopting the above configuration, it is possible to provide a wastewater treatment system capable of cleaning wastewater with high efficiency and stability. In particular, by using the wastewater treatment apparatus 200 as described above, it is possible to suppress the growth of microorganisms, thereby preventing the generation of algae and the like.

  Furthermore, the wastewater treatment system 1A as in the present embodiment can be easily realized simply by adding an aeration tank 100, a wastewater treatment device 200, etc. to an existing wastewater treatment system having only an activated sludge treatment device. Therefore, existing facilities can be used effectively and the economy is excellent.

  Moreover, in the waste water treatment system 1A in the above-described embodiment, the case where the waste water treatment apparatus 200 having a configuration in which the first treatment tank 210 and the second treatment tank 220 are alternately replaced with the adsorption tank and the desorption tank is illustrated. However, a waste water treatment apparatus having a different configuration may be employed. Hereinafter, an example thereof will be described with reference to FIGS.

  2 and 3 are schematic views showing examples of other waste water treatment apparatuses that can be used in the waste water treatment system according to the present embodiment. 2 and 3, only the adsorbent provided in the waste water treatment apparatus and the components arranged in the vicinity of the adsorbent are shown, and the other components are not shown.

  FIG. 2 shows a case where an adsorbent 250 having a cylindrical outer shape is used. As shown in FIG. 2, when using an adsorbent 250 having a cylindrical outer shape, a rotation shaft 261 is provided at the axial center of the adsorbent 250 configured to allow fluid to flow in the axial direction. The rotary shaft 261 is rotationally driven by an actuator or the like. Then, piping lines L2, L5, L6, and L7 (see FIG. 1) not shown in FIG. 2 are connected close to both end surfaces of the adsorbent 250 in the axial direction, and a part of the adsorbent 250 is subjected to an adsorption process. 2 is used as a portion (indicated by reference numeral 251 in FIG. 2), and another part of the adsorbent 250 is used as a portion for performing desorption processing (indicated by reference numeral 252 in FIG. 2). That is, the primary treated water is introduced from one side in the axial direction into the portion indicated by the reference numeral 251 of the adsorbent 250 and the secondary treated water is derived from the other in the axial direction. In the portion shown, the heating gas is introduced from one side in the axial direction, and the desorption gas is led out from the other side in the axial direction.

  Here, in the waste water treatment apparatus shown in FIG. 2, the adsorbent 250 rotates at a predetermined speed in the direction of arrow A in the figure with the rotation shaft 261 as the center of rotation. As a result, the portion where the adsorption process of the adsorbent 250 is completed moves to the zone where the desorption process is performed, and the portion where the desorption process of the adsorbent 250 is completed moves to the zone where the adsorption process is performed. Therefore, in the waste water treatment apparatus, the adsorption process and the desorption process are simultaneously performed, and the cleaning process can be continuously performed.

  FIG. 3 shows a case where an adsorbent 270 having a cylindrical outer shape is used. As shown in FIG. 3, when using an adsorbent 270 having a cylindrical outer shape, for example, a unit adsorbing unit 275 surrounded by a metal frame 285 so that fluid can flow in the radial direction. Are arranged in the circumferential direction into a cylindrical shape, and this is rotationally driven around the axis by an actuator (not shown). Then, piping lines L2, L5, L6, and L7 (see FIG. 1) not shown in FIG. 3 are connected in the vicinity of the adsorbent 270, and a part of the unit adsorbing unit of the adsorbent 270 is adsorbed. It is used as a portion (a portion indicated by reference numeral 271 in FIG. 3), and another part of the unit adsorption unit is used as a portion (a portion indicated by reference numeral 272 in FIG. 3) for performing a desorption process. That is, to the unit adsorption unit indicated by reference numeral 271 of the adsorbent 270, the primary treated water is introduced from the radially outer side, the secondary treated water is led toward the radially inner side, and discharged toward one of the axial directions. Thus, a heating gas is introduced into the unit adsorption unit indicated by reference numeral 272 of the adsorbent 270 from the inside in the radial direction via the introduction pipe 281, and the desorption gas is led out toward the outside in the radial direction to lead out the extraction pipe 282. It will be discharged through.

  Here, in the wastewater treatment apparatus shown in FIG. 3, the adsorbent 270 rotates stepwise at a predetermined speed in the direction of arrow A in the figure around the axis. As a result, the unit adsorption unit for which the adsorption process of the adsorbent 270 is completed moves to the zone for performing the desorption process, and the unit adsorption unit for which the desorption process for the adsorbent 270 is completed moves to the zone for performing the adsorption process. become. Therefore, in the waste water treatment apparatus, the adsorption process and the desorption process are simultaneously performed, and the cleaning process can be continuously performed.

  When the adsorbents 250 and 270 having the shapes as shown in FIGS. 2 and 3 are used, the adsorbents 250 and 270 are configured to be filled with granular materials or filled with fibrous materials. Although it is good, it is more preferable to comprise a honeycomb structure. This is because the adsorbents 250 and 270 are made of a honeycomb-like structure, so that the pressure loss can be suppressed to an extremely low level, the processing capacity is increased, and clogging due to solids such as dust is prevented. This is because the occurrence can be suppressed relatively low.

(Embodiment 2)
FIG. 4 is a schematic diagram showing the configuration of the wastewater treatment system according to Embodiment 2 of the present invention. In FIG. 4, illustration of the same parts as the waste water treatment system 1A in the first embodiment of the present invention is omitted. Below, with reference to this FIG. 4, the structure of the waste water treatment system 1B in this Embodiment is demonstrated.

  As shown in FIG. 4, the waste water treatment system 1B in the present embodiment is different from the above-described waste water treatment system 1A in the first embodiment of the present invention in the configuration of the waste water treatment apparatus 200. In the wastewater treatment system 1B in the present embodiment, a piping line L17 for introducing gas into the wastewater treatment apparatus 100 is connected to the piping line L6 for introducing heated gas into the wastewater treatment apparatus 200. Valves V209 and V210 for switching the connection / disconnection state of the piping lines L6 and L17 to the waste water treatment apparatus 200 are provided in the piping lines L6 and L17, respectively. In the wastewater treatment system 1B according to the present embodiment, a piping line L18 for discharging removed wastewater from the wastewater treatment device 200 is connected to the piping line L7 for discharging desorption gas from the wastewater treatment device 200. In addition, valves V211 and V212 for switching the connection / disconnection state of the piping lines L7 and L18 to the waste water treatment apparatus 200 are provided in the piping lines L7 and L18, respectively. The other end of the piping line L18 is connected to a piping line L2 for introducing primary treated water into the waste water treatment apparatus 200.

  In the wastewater treatment apparatus 200 of the wastewater treatment system 1B in the present embodiment, a dehydration process (purge process) is performed between the adsorption process and the desorption process. Specifically, as in the case of the wastewater treatment system 1A in the first embodiment of the present invention described above, in the wastewater treatment apparatus 200, the first treatment tank 210 and the first treatment tank 210 are operated by opening and closing valves V201 to 208. The second treatment tank 220 is alternately switched to the adsorption tank and the desorption tank. When the second treatment tank 220 is switched to the desorption tank, first, the desorption tank is connected to the piping line L17 and the piping line L18, via the piping line L17. A dehydration process is performed to blow off excess wastewater adhering to the surface of the adsorbent by introducing gas into the desorption tank and sprayed onto the adsorbent, and the removed wastewater blown off passes through the piping line L18 and the piping line L2. The wastewater treatment device 200 is supplied again. Then, after performing the dehydration process for a predetermined time, the connection between the desorption tank and the piping line L17 and the piping line L18 is released, and the piping line L6 and the piping line L7 are connected to the desorption tank, and the desorption process is performed. The gas introduced into the desorption tank during the dehydration process is preferably a high temperature and low humidity gas. For example, it is preferable to use dry air heated to a predetermined temperature. .

  By adopting the configuration as in the wastewater treatment system 1B in the present embodiment described above, the effect obtained when the configuration as in the wastewater treatment system 1A in the first embodiment of the present invention described above is employed. In addition, since the desorption efficiency of the organic compound from the adsorbents 211 and 221 is greatly increased, an effect of being able to provide a wastewater treatment system capable of cleaning wastewater more efficiently and stably can be obtained. In addition, in this Embodiment mentioned above, although demonstrated, the case where it comprised so that the removal waste_water | drain discharged | emitted from the waste water treatment apparatus 200 might be supplied to the said waste water treatment apparatus 200 again was demonstrated, the said removal waste_water | drain May be configured to be cleaned by separately using a wastewater treatment apparatus or the like equipped with an exchangeable adsorption element.

(Embodiment 3)
FIG. 5 is a schematic diagram showing the configuration of the waste water treatment system according to Embodiment 3 of the present invention. In FIG. 5, illustration of the same parts as the waste water treatment system 1A in the first embodiment of the present invention and the waste water treatment system 1B in the second embodiment is omitted. Below, with reference to this FIG. 5, the structure of the waste water treatment system 1C in this Embodiment is demonstrated.

  As shown in FIG. 5, the wastewater treatment system 1C in the present embodiment is different in the configuration of the wastewater treatment system 1A in the first embodiment of the present invention described above, the wastewater treatment system 1B in the second embodiment, and the combustion apparatus 400. is doing. In the wastewater treatment system 1C according to the present embodiment, one more heat exchange 411 is connected to the combustion apparatus 400, and heat exchange is performed between the cracked gas discharged from the heat exchanger 410 and the gas in the combustion apparatus 400. This is for preheating the heating gas necessary for the desorption process of the waste water treatment apparatus 200. The piping line L19 is a piping line for supplying gas to the heat exchanger 411, and the piping line L6 is a piping line for introducing the heated gas preheated by the heat exchanger 411 into the waste water treatment apparatus 200. . The piping lines L19 and L11 are piping lines for discharging the cracked gas discharged from the heat exchanger 410 to the outside via the heat exchanger 411.

  In the combustion apparatus 400 of the wastewater treatment system 1C in the present embodiment, preheating of the heated gas of the wastewater treatment apparatus 200 is performed in the heat exchanger 411 using the cracked gas discharged from the combustion apparatus 400.

  By adopting the configuration like the wastewater treatment system 1C in the present embodiment described above, the configuration like the wastewater treatment system 1A and the wastewater treatment system 1B in the first embodiment of the present invention described above is adopted. In addition to the effects obtained, the amount of heat necessary for raising the temperature of the heating gas required for the waste water treatment apparatus 200 can be reduced, so that the effect of achieving a waste water treatment system capable of purifying waste water more efficiently can be obtained. In the present embodiment described above, heating means such as a steam heater or an electric heater may be added to the waste water treatment apparatus 200 as necessary.

  The characteristic configurations of the wastewater treatment systems 1A, 1B, and 1C according to the first to third embodiments of the present invention described above can be combined with each other. For example, the waste water treatment apparatus including the adsorbents 250 and 270 having the configuration shown in FIGS. 2 and 3 is applied to the waste water treatment apparatus 200 of the waste water treatment systems 1B and 1C according to the second and third embodiments of the present invention. Also good. In this case, a zone for performing dehydration processing is provided in a zone for performing desorption processing of the adsorption elements 250 and 270, and portions of the adsorption elements 250 and 270 located in the zone for performing the dehydration processing are provided. The above-described piping lines L17 and L18 are connected in proximity to each other, and the waste water treatment apparatus 200 is configured so that the dehydration process is performed between the adsorption process and the desorption process.

  Moreover, in Embodiment 1 to 3 of this invention demonstrated above, it demonstrates by exemplifying the continuous activated sludge processing apparatus with which a process is performed continuously as an activated sludge processing apparatus with which a waste water treatment system is equipped. Although performed, it is naturally possible to use a batch activated sludge treatment apparatus in which the treatment is performed batchwise. In Embodiments 1 to 3 of the present invention described above, the activated sludge treatment device provided in the wastewater treatment system has been described as an example of performing solid-liquid separation using a sedimentation tank. In addition, various configurations such as a membrane separation using a membrane provided in an aeration tank can be used. As described above, the activated sludge treatment apparatus provided in the wastewater treatment system to which the present invention is applicable may be of any type.

  In the first to third embodiments of the present invention described above, the description has been made without particularly showing the components such as the fluid conveying means such as the pump and the fan and the fluid storing means such as the storage tank. What is necessary is just to arrange | position a component in an appropriate position as needed.

  Thus, the above-described embodiments disclosed herein are illustrative in all respects and are not restrictive. The technical scope of the present invention is defined by the terms of the claims, and is intended to include any modifications within the scope and meaning equivalent to the terms of the claims.

Hereinafter, the present invention will be described in more detail with reference to Examples of Embodiment 3, but the present invention is not limited to these Examples.
The evaluation was performed by the following method.
(BET specific surface area)
The BET specific surface area was measured by measuring the amount of nitrogen adsorbed on the sample when the relative pressure was raised in the range of 0.0 to 0.15 in the atmosphere of the boiling point of liquid nitrogen (-195.8 ° C), and a BET plot. Was used to determine the surface area (m ² / g) per unit mass of the sample.
(Pore volume)
The pore volume was measured by a nitrogen gas adsorption method at a relative pressure of 0.95.
(Average pore diameter)
The average pore diameter was determined by the following formula.
dp = 40000 Vp / S (where dp: average pore diameter (径))
Vp: pore volume (cc / g)
S: BET specific surface area (m ² / g)
(Organic compound removal effect)
Waste water mainly containing 1,4-dioxane 1000 mg / L, acetaldehyde 14000 mg / L, and ethylene glycol 16000 mg / L was used as raw water. The amount of waste water is 2.1 m ³ / hr, and the amount of organic compounds in the raw water is 2.1 kg / hr of 1,4-dioxane, 29.4 kg / hr of acetaldehyde, and 33.6 kg / hr of ethylene glycol. Introduce water at a temperature of 50 ° C, measure the concentration of 1,4-dioxane, ethylene glycol and acetaldehyde in the water and gas at the inlet and outlet of the wastewater treatment equipment, activated sludge treatment equipment, combustion equipment, and calculate the amount of organic compounds The removal effect was confirmed.
(Organic compound concentration evaluation)
The concentrations in water and gas at the inlet and outlet were analyzed and measured by gas chromatography.

[Example 1]
An aeration tank 100 having an effective aeration capacity of 4.2 m ³ is subjected to an aeration temperature of 60 ° C., an aeration intensity of 2.5 min ⁻¹ , an air volume of 11 Nm ³ / min, a residence time of 2 hrs, 1,4- with a treated water amount of 2.1 m ³ / hr. Raw water containing dioxane 1000 mg / L (2.1 kg / hr), acetaldehyde 14000 mg / L (29.4 kg / hr), ethylene glycol 16000 mg / L (33.6 kg / hr) was introduced to obtain primary treated water. The amount of the organic compound in the primary treated water at that time was 1,4-dioxane 1.1 kg / hr or less, acetaldehyde 0.01 kg / hr or less, and ethylene glycol 33.6 kg / hr or less. Moreover, the organic compound density | concentration of the aeration gas discharged | emitted from the aeration tank 100 was 1, 4- dioxane 420ppm, acetaldehyde 24000ppm, and ethylene glycol 1ppm or less. The amount of steam used was 60 kg / hr or less.

Next, an adsorbing element having a weight of 50 kg using activated carbon fibers having an average pore diameter of 17.1 mm, a BET specific surface area of 1500 m ² / g, and a total pore volume of 0.47 m ³ / g is used as an adsorbent for the wastewater treatment apparatus 200. One was prepared, and the primary treated water after the above-described aeration treatment was introduced so that the amount of treated water was 2.1 m ³ / hr to obtain secondary treated water.

Next, air was used as a gas during the dehydration process of the waste water treatment apparatus 200, and the air volume of dehydration was set to 60 Nm ³ / min. Air at 120 ° C. was used as a heating gas in the desorption process, and the wind speed of desorption was 60 Nm ³ / min. The adsorption cycle in the adsorption step was 60 min, the dehydration time in the dehydration step was 5 min, the desorption time in the desorption step was 55 min, and a switching cycle was set. The amount of the organic compound in the secondary treated water at that time was 1,4-dioxane 1 g / hr or less, acetaldehyde 0.5 g / hr or less, and ethylene glycol 32.6 kg / hr. The organic compound concentration in the desorption gas was 1,4-dioxane 200 ppm or less, acetaldehyde 10 ppm or less, and ethylene glycol 100 ppm or less.

Then, the raw water regulating tank capacity 3m ^3, dilution tank capacity capacity 7m ^3, 2 one carrier flow aeration tank of any capacity 125m ^3, 2 one active sludge tank and capacity 25 m ³ of volume 125m ³ The secondary treated water discharged from the waste water treatment apparatus 200 was introduced using an activated sludge treatment apparatus 300 composed of a settling tank to obtain tertiary treated water. 12.5 m ³ of polyvinyl alcohol cross-linked gel carrier (diameter: about 4 mm) was charged into the carrier flow aeration tank. In addition, since the concentration of organic compounds in the tertiary treated water is high and the load on microorganisms is high, it is diluted with industrial water supplied from a dilution tank, and is 21 m ³ / hr in the carrier flow aeration tank and the activated sludge tank. Introduced. The amount of organic compounds in the tertiary treatment water at that time is 1,4-dioxane 1 g / hr or less, the acetaldehyde concentration is 0.1 g / hr or less, and the ethylene glycol concentration is 0.2 kg / L or less. Met. Moreover, the generated surplus sludge amount was as small as 0.6 t / day.

  Table 1 shows the amounts of organic compounds, utility consumption, and sludge in the treated water after 500 hours using the water treatment system of this example. Even after 500 hours, the treatment was stable. The aeration tank 100 volatilizes and removes acetaldehyde and 1,4-dioxane, thereby reducing the load on the wastewater treatment apparatus 200 and the activated sludge treatment apparatus 300, while the activated sludge treatment apparatus 300 treats the wastewater treatment apparatus 200. Efficient wastewater treatment is enabled by adsorbing and removing difficult 1,4-dioxane with high efficiency and biodegrading ethylene glycol with the activated sludge treatment apparatus 300. Further, since the wastewater treatment apparatus 200 is processed by continuously performing adsorption and desorption, the wastewater treatment apparatus 200 can be treated stably and with high efficiency without deterioration in performance.

  Next, when the aeration gas duct discharged from the aeration tank 100 and the desorption gas duct discharged from the waste water treatment apparatus 200 were connected and the concentration of the mixed exhaust gas was measured, 1,4-dioxane 300 ppm, acetaldehyde It became 3400 ppm and ethylene glycol 100 ppm.

Next, a platinum catalyst is installed in the combustion device 400 as a catalyst of the combustion device 400, and the mixed exhaust gas of the aeration gas discharged from the aeration tank 100 and the desorption gas discharged from the waste water treatment device 200 is air volume 71 Nm ³ / min. Then, the temperature was raised to 300 ° C. with a heat exchanger and a preheating heater, and then contacted with the catalyst, and the organic compound in the mixed exhaust gas was oxidized and decomposed with the catalyst to obtain a cracked gas. The 1,4-dioxane, acetaldehyde, and ethylene glycol concentrations in the cracked gas were each 1 ppm or less and could be treated satisfactorily.

  Further, when the outlet temperature of the combustion device 400 was measured over time, the average outlet temperature was 450 ° C., and when calculated with a heat exchange rate of 60%, the mixed exhaust gas was obtained only by heat exchange with the cracked gas from the combustion device 400. Therefore, the power consumption when an electric heater is used as the preheating heater can be reduced to 0.1 kWh or less.

  Moreover, when the temperature of the decomposition gas after the heat exchange discharged | emitted from the heat exchanger 410 shown in FIG. 1 was measured, it is 300 degreeC in average temperature, and it is trial calculation with the heat exchange rate 50% of the heat exchanger 411 shown in FIG. Then, since the heating gas required for the wastewater treatment apparatus 200 can be raised only by heat exchange, the amount of steam used when heated using a steam heater can be reduced to 0.1 kg / hr or less. It was.

  Table 1 shows each organic compound concentration, utility consumption, and sludge amount in the processing gas after 500 hours of implementation using the water treatment system of this example. Even after 500 hours, processing was possible with stable and small utility consumption. In addition to the desorption gas discharged from the waste water treatment apparatus 200, the process is performed by mixing aeration gas with a low air volume and a high organic compound concentration and a small concentration fluctuation discharged from the aeration tank 100. The amount of combustion heat generated is generated, and energy consumption can be reduced by heat recovery.

[Comparative Example 1]
Raw water regulating tank capacity is 9m ^3, volume dilution tank capacity 21m ^3, two carrier flow aeration tank also 300 meters ³ any capacity, sedimentation tank capacity two activated sludge tank and capacity of 300 meters ³ 75 m ³ The raw water used in Example 1 was introduced using an activated sludge treatment apparatus 300 consisting of the following to obtain treated water. 30 m ³ of polyvinyl alcohol cross-linked gel carrier (diameter: about 4 mm) was charged into the carrier flow aeration tank. Moreover, since the organic compound density | concentration of raw | natural water is high and the load with respect to microorganisms is high, it diluted with the industrial water supplied from a dilution tank, and introduce | transduced into the support | carrier flow aeration tank and the activated sludge tank at 55 m < ³ > / hr. As shown in Table 1, the amount of organic compounds in the treated water at that time is 1,4-dioxane 2.1 kg / hr or less, the acetaldehyde concentration is 0.5 kg / hr or less, and the ethylene glycol concentration is 0.2 kg / hr or less. Yes, good treatment was possible for acetaldehyde and ethylene glycol, but no treatment was possible for 1,4-dioxane. Moreover, as shown in Table 1, the generated surplus sludge amount was 2 t / day, which was about four times that of Example 1.

[Comparative Example 2]
Two adsorbing elements with a weight of 100 kg using activated carbon fibers having an average pore diameter of 17.1 mm, a BET specific surface area of 1500 m ² / g, and a total pore volume of 0.47 m ³ / g as an adsorbent for the wastewater treatment apparatus 200 were prepared. The raw water used in Example 1 was introduced so that the amount of treated water was 2.1 m ³ / hr to obtain primary treated water.

Next, air was used as the gas during the dehydration process of the waste water treatment apparatus 200, and the air volume of dehydration was 120 Nm ³ / min. 120 ° C. air was used as a heating gas in the desorption process, and the wind speed of desorption was 120 Nm ³ / min. The adsorption cycle in the adsorption step was 60 min, the dehydration time in the dehydration step was 5 min, the desorption time in the desorption step was 55 min, and a switching cycle was set. The amount of the organic compound in the primary treated water at that time was 1,4-dioxane 1 g / hr, acetaldehyde 28.4 kg / hr or less, and ethylene glycol 31.6 kg / L or less. Moreover, the organic compound density | concentration in desorption gas was 1, 4- dioxane 120ppm, acetaldehyde 280ppm, and ethylene glycol 20ppm.

Then, the raw water regulating tank capacity 9m ^3, volume dilution tank capacity 21m ^3, two carrier flow aeration tank also 300 meters ³ any capacity, capacity two activated sludge tank and capacity of 300 meters ³ 75 m ³ The primary treated water discharged from the waste water treatment apparatus 200 was introduced using an activated sludge treatment apparatus 300 composed of a settling tank to obtain secondary treated water. 30 m ³ of polyvinyl alcohol cross-linked gel carrier (diameter: about 4 mm) was charged into the carrier flow aeration tank. Moreover, since the organic compound concentration in the primary treated water is high and the load on microorganisms is high, it is diluted with industrial water supplied from a dilution tank, and is 55 m ³ / hr in the carrier flow aeration tank and the activated sludge tank. Introduced. As shown in Table 1, the amount of the organic compound in the secondary treated water at that time is 1,4-dioxane 1 g / hr or less, the acetaldehyde concentration is 0.5 kg / hr or less, and the ethylene glycol concentration is 0.2 kg / hr or less. And good processing was possible. However, the amount of excess sludge generated was 2 t / day, which was about four times that of Example 1.

Next, a platinum catalyst is installed in the combustion apparatus 400 as a catalyst of the combustion apparatus 400, and the desorption gas discharged from the waste water treatment apparatus 200 is supplied at an air volume of 120 Nm ³ / min, and is heated to 300 ° C. by a heat exchanger and a preheating heater. After the temperature was raised to 1, the organic compound in the desorption gas was oxidatively decomposed with the catalyst to obtain a decomposition gas. As shown in Table 1, the concentration of the organic compound in the cracked gas was 1 ppm or less for each of 1,4-dioxane, acetaldehyde, and ethylene glycol, and could be treated satisfactorily.

  When the outlet temperature of the combustion device 400 was measured over time, the average outlet temperature was 330 ° C., and when calculated at a heat exchange rate of 60%, the desorption gas was 220 ° C. only by heat exchange with the cracked gas from the combustion device 400. As shown in Table 1, the power consumption when using an electric heater for preheating up to 300 ° C. was 200 kWh.

  When the temperature of the cracked gas after heat exchange discharged from the heat exchanger 410 was measured, the average temperature was 300 ° C., and the heat exchange rate of the heat exchanger 411 was calculated to be 50%. As shown in Table 1, the amount of steam used when the steam heater was used for heating could be 0.1 kg / hr or less.

[Comparative Example 3]
The raw water used in Example 1 was introduced into an aeration tank 100 having an effective aeration capacity of 21 m ^{3 under} the conditions of an aeration temperature of 80 ° C., an aeration intensity of 2.5 min ⁻¹ , an air volume of 55 Nm ³ / min, and a residence time of 10 hr, and primary treated water. Got. The amount of the organic compound in the primary treated water at that time was 1,4-dioxane 1 g / hr or less, acetaldehyde 0.01 kg / hr or less, and ethylene glycol 33.6 kg / hr or less. Moreover, the organic compound density | concentration of the aeration gas discharged | emitted from the aeration tank 100 became 1, 4- dioxane 120ppm, acetaldehyde 4500ppm, and ethylene glycol 1ppm or less. However, as shown in Table 1, the amount of input steam required for heating was 1000 kg / hr or more, and the amount of steam used was extremely high.

Next, using the same activated sludge treatment apparatus 300 as in Example 1, the primary treated water discharged from the aeration tank 100 was introduced to obtain secondary treated water. In addition, since the organic compound concentration in the primary treated water is high and the load on microorganisms is high, it is diluted with industrial water supplied from a dilution tank, and is 21 m ³ / hr in the carrier flow aeration tank and the activated sludge tank. Introduced. The amount of the organic compound in the secondary treated water at that time is 1,4-dioxane 1 g / hr or less, the acetaldehyde concentration is 0.5 g / hr or less, and the ethylene glycol concentration is 0.2 kg / hr or less as shown in Table 1. And good processing was possible. Moreover, as shown in Table 1, the amount of generated excess sludge was as small as 0.6 t / day.

Next, a platinum catalyst is installed in the combustion apparatus 400 as a catalyst for the combustion apparatus, and aeration gas discharged from the aeration tank 100 is supplied at an air volume of 55 Nm ³ / min, and the temperature is increased to 300 ° C. by a heat exchanger and a preheating heater. After heating, the catalyst was brought into contact with the catalyst, and the organic compound in the desorption gas was oxidatively decomposed with the catalyst to obtain a decomposition gas. As shown in Table 1, the concentration of the organic compound in the decomposition gas at that time was 1 ppm or less for 1,4-dioxane, acetaldehyde, and ethylene glycol.

  When the outlet temperature of the combustion apparatus 400 was measured over time, the average outlet temperature was 450 ° C., and when calculated with a heat exchange rate of 60%, the aeration gas was reduced to 300 by only heat exchange with the cracked gas from the combustion apparatus 400. Since it is possible to raise the temperature to about 0 ° C., the power consumption when using the electric heater can be reduced to 0.1 kWh or less as shown in Table 1.

1A, 1B, 1C Wastewater treatment system, 100 aeration tank, 111 aeration apparatus, 112 heating apparatus, 200 wastewater treatment apparatus, 210 first treatment tank, 211 adsorbent, 220 second treatment tank, 221 adsorbent, 250 adsorbent , 261 Rotating shaft, 270 Adsorbent, 275 Unit adsorption unit, 281 Introducing pipe, 282 Deriving pipe, 285 Frame, 300 Activated sludge treatment apparatus, 310 Aeration tank, 311 Aeration apparatus, 320 Precipitation tank, 400 Combustion apparatus, 410 Heat Exchanger, 411 heat exchanger, 420 combustion furnace, L1-L19 piping line, V201-V212 valve.

Claims (5)

A wastewater treatment system for purifying wastewater by removing organic compounds from wastewater containing organic compounds,
Aeration tank that discharges aeration gas containing organic compound by discharging the wastewater containing organic compound as primary treated water from which organic compound is volatilized and removed by aeration treatment,
It includes an adsorbing element that adsorbs the organic compound by contacting the primary treated water containing the organic compound and desorbs the adsorbed organic compound by contacting the heated gas, and supplies the primary treated water to the adsorbing element. The organic compound is adsorbed on the adsorption element and discharged as secondary treated water, and the heated gas is supplied to the adsorption element so that the organic compound is desorbed from the adsorption element and discharged as a desorption gas containing the organic compound. The portion where the adsorption element has been desorbed is transferred to the portion where the adsorption process is performed, and the portion where the adsorption process of the adsorption element is completed is shifted to the portion where the desorption process is performed, so that the secondary treated water is continuously obtained. Wastewater treatment equipment capable of treating
Activated sludge treatment that has activated sludge containing microorganisms that decompose organic compounds, and decomposes and removes organic compounds by microorganisms by bringing the secondary treated water into contact with the activated sludge and discharges it as tertiary treated water Equipment,
Combustion connected to the aeration tank and the wastewater treatment apparatus, and combusting a mixed exhaust gas of an aeration gas and a desorption gas containing an organic compound discharged from the aeration tank and the wastewater treatment apparatus to oxidatively decompose and discharge decomposition gas Wastewater treatment system equipped with a device.   The wastewater treatment system according to claim 1, wherein the wastewater treatment device blows off excess wastewater adhering to the adsorption element by blowing gas onto the adsorption element and discharges it as removed wastewater.   The wastewater treatment system according to claim 2, wherein the removed wastewater discharged from the wastewater treatment device is again supplied to the wastewater treatment device as wastewater.   The wastewater treatment system according to any one of claims 1 to 3, wherein the adsorption element includes at least one member selected from the group consisting of activated carbon, activated carbon fiber, and zeolite. The wastewater treatment system according to any one of claims 1 to 4, wherein the waste gas treatment system is configured to heat-exchange cracked gas discharged from the combustion device and preheat the heated gas of the wastewater treatment device.

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