JP2012125732A - Water treatment method and method for producing ultrapure water - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a water treatment method which even when the concentration of urea and that of a urea derivative in raw water fluctuate, highly decomposes the urea by quickly following the fluctuation.SOLUTION: A pretreatment system 1 is used for treating the raw water W to be supplied from a raw water storage tank not shown in figure. The raw water W treated in the pretreatment system 1 is stored temporarily in a feed tank 2. The feed tank 2 is continuous with a biological treatment means 3. The raw water W treated in the biological treatment means 3 can be supplied to a primary pure water apparatus as treated water W1. A pH sensor not shown in the figure and a supply means 4 are arranged in the preceding stage of the biological treatment means 3. An ammonia nitrogen source (NH-N) and sulfuric acid being a pH adjusting agent can be added from the supply means 4. In this treatment flow, a reduction treatment means 6 is preferably arranged in the succeeding stage of the biological treatment means 3 and in the preceding stage of the primary pure water apparatus.

Description

  The present invention relates to a water treatment method for raw water such as city water, groundwater, and industrial water, and a method for producing ultrapure water using treated water treated by this water treatment method, and in particular, it can highly remove urea in raw water. The present invention relates to a water treatment method that can be performed and a method for producing ultrapure water using treated water treated by the water treatment method.

  Conventionally, an ultrapure water production apparatus that produces ultrapure water from raw water such as city water, groundwater, and industrial water basically includes a pretreatment apparatus, a primary pure water production apparatus, and a secondary pure water production apparatus. . Among these, the pretreatment device is composed of agglomeration, levitation, and filtration devices. The primary pure water production apparatus includes, for example, two reverse osmosis membrane separation devices and a mixed bed ion exchange device, or an ion exchange pure water device and a reverse osmosis membrane separation device. Further, the secondary pure water production apparatus is composed of, for example, a low-pressure ultraviolet oxidizer, a mixed bed ion exchanger, and an ultrafiltration membrane separator.

  In such an ultrapure water production apparatus, there is an increasing demand for improvement in the purity, and accordingly, removal of the TOC component is required. Of the TOC components in ultrapure water, it is particularly difficult to remove urea, and the lower the TOC component, the greater the influence of urea removal on the TOC component content. Therefore, Patent Documents 1 to 3 describe that TOC in ultrapure water is sufficiently reduced by removing urea from the water supplied to the ultrapure water production apparatus.

Patent Document 1 discloses that a biological treatment device is incorporated in a pretreatment device and urea is decomposed by this biological treatment device. Further, in Patent Document 2, a biological treatment apparatus is incorporated in a pretreatment apparatus, mixed water of treated water (industrial water) and semiconductor cleaning / collecting water is passed through, and organic substances contained in the semiconductor cleaning / collecting water are disclosed. It has been disclosed that it becomes a carbon source for biological treatment reactions and improves the decomposition rate of urea. In addition, there are cases where a large amount of ammonium ions (NH ₄ ⁺ ) are contained in this semiconductor cleaning / recovered water, which becomes a nitrogen source in the same manner as urea and may inhibit the decomposition of urea. Further, in Patent Document 3, in order to solve the above-mentioned problem of Patent Document 2, the water to be treated (industrial water) and the semiconductor cleaning / collecting water are mixed after being biologically treated separately, It is described that water is passed through a secondary pure water production apparatus.

JP-A-6-63592 JP-A-6-233997 JP-A-7-313994

  However, when the carbon source is added to the water to be treated as in the water treatment method described in Patent Document 2, although the urea decomposition and removal efficiency in the biological treatment apparatus is improved, the amount of bacterial cells in the biological treatment apparatus is increased. There is a problem that the amount of bacterial cells flowing out from the biological treatment apparatus increases.

  In addition, the water treatment method described in Patent Document 2 has a problem that ammonium water inhibits the decomposition of urea when semiconductor cleaning / collected water having a high ammonium ion content is used as water containing a carbon source. is there.

  That is, in the water treatment method described in Patent Document 2, when BOD assimilating bacteria (heterotrophic bacteria) decompose and assimilate organic matter, not nitrifying bacteria, urea and urea derivatives are decomposed as nitrogen sources, ammonia It is presumed that this is a treatment mechanism for removing urea and urea derivatives.

  Accordingly, the present inventors have added a water treatment method and an ultrapure water production method capable of removing urea to a lower concentration in a short time by performing biological treatment after adding ammoniacal nitrogen to raw water. Was previously proposed (Japanese Patent Application No. 2010-105151, etc.).

  In this water treatment method, nitrifying bacteria (ammonia-oxidizing bacteria) are grown by adding ammoniacal nitrogen to biological treatment to improve urea resolution. However, as a result of subsequent research, the nitrifying bacteria group can generate energy and grow by oxidation of ammonia without decomposing urea. Depending on the operating conditions, only the added ammoniacal nitrogen can be used and urea can be used. It was found that the system may not be decomposed. Specifically, the concentrations of urea and urea derivatives are known to vary seasonally in city water and industrial water, and the activity of the nitrifying bacteria group varies depending on the concentrations of urea and urea derivatives in the feed water. . That is, when the concentration of urea and urea derivatives in the feed water decreases, the activity also decreases, and even if the urea and urea derivative concentrations in the feed water increase rapidly thereafter, it cannot follow, and urea and urea derivatives may leak into the treated water I found out that

  Therefore, in order to keep the urea concentration of biologically treated water low by following the concentration fluctuations of urea and urea derivatives in the water supply, it is conceivable to always add an ammoniacal nitrogen source to maintain the activity of the nitrifying bacteria group However, even if ammonia nitrogen removal performance can be maintained, urea and urea derivative removal urine performance cannot always be maintained.

  The present invention has been made in view of the above problems, and even if the concentrations of urea and urea derivatives in raw water fluctuate, a water treatment method that can quickly follow this and highly decompose urea is provided. The purpose is to provide. Moreover, an object of this invention is to provide the ultrapure water manufacturing method using this water treatment method.

  In order to solve the above problems, first, in the water treatment method for biologically treating raw water containing organic matter, the pH is adjusted to 5 to 6.5 after adding an ammonia nitrogen source to the raw water. And providing a water treatment method characterized by performing biological treatment (Invention 1).

According to the above invention (Invention 1), the nitrifying bacteria group is involved in the removal of urea. By adding an ammonia nitrogen source to the raw water, the nitrifying bacteria group (ammonia-oxidizing bacteria) becomes ammoniacal nitrogen. By oxidizing the source to nitrite ions (NO ₂ ⁻ ), the activity of the nitrifying bacteria group can be maintained and urea can be decomposed and removed. At this time, by adjusting the pH to 5 to 6.5, the nitrifying bacteria group having the optimum value in the neutral range has both ammonia oxidation activity and urea decomposition activity lower than the optimum pH. The decrease in ureolytic activity is less than the decrease in activity. Furthermore, ammonia in an ionic state increases, and the amount of ammonia taken into the nitrifying bacteria group decreases. As a result, the amount of urea consumed by the nitrifying bacteria group increases, so that the activity of the nitrifying bacteria group can be maintained even when the urea concentration varies greatly, and urea can be effectively decomposed and removed.

In the above invention (invention 1), the nitrogen source of the ammoniacal is preferably not more than 20 in _NH ⁴ + -N / urea against the concentration of urea (invention 2). According to this invention (invention 2), the function of preferentially decomposing and removing urea can be maintained by setting the ammonia concentration to 20 times or less of the urea concentration.

  In the said invention (invention 1 and 2), it is preferable to perform the said biological treatment by the biological treatment means which has a biological support | carrier (invention 3). Moreover, in the said invention (invention 3), it is preferable that the said biological treatment is a biological treatment means which has a fixed bed of a biological support | carrier (invention 4).

  According to such inventions (Inventions 3 and 4), since the biological treatment means is a biofilm method using a biological carrier, it is possible to suppress the outflow of bacterial cells from the biological treatment means more than in the case of a fluidized bed. The effect of the treatment is high, and the effect can be maintained for a long time.

  In the said invention (invention 1-4), it is preferable that the said ammoniacal nitrogen source is an ammonium salt (invention 5).

According to the above invention (Invention 5), ammonium salts such as ammonium chloride are suitable for activation of the nitrifying bacteria group by being oxidized by ammonia oxidizing bacteria to become nitrite ions (NO ₂ ⁻ ). The addition and control thereof are easy, and it is suitable for keeping the urea concentration low.

  In the said invention (invention 1-5), it is preferable to perform a reduction process in the back | latter stage of the said biological treatment (invention 6).

  According to the above invention (Invention 6), the raw water for biological treatment often contains a chlorinated oxidant (such as hypochlorous acid), which reacts with an ammoniacal nitrogen source to form a combined chlorine compound. May form. Although combined chlorine has a lower oxidizing power than free chlorine, it may cause oxidative deterioration of the treated member in subsequent processing, so that the combined chlorine compound is rendered harmless by reduction treatment.

  Moreover, 2nd this invention processes the treated water obtained with the water treatment method which concerns on the said invention (invention 1-6) with a primary pure water apparatus and a secondary pure water apparatus, and manufactures an ultrapure water. A method for producing ultrapure water is provided (Invention 7).

  According to the above invention (Invention 7), since the urea is sufficiently decomposed and removed in the biological treatment (water treatment) preceding the primary pure water device and the secondary pure water device, high purity ultrapure water is efficiently used. Can be manufactured well.

According to the water treatment method of the present invention, an ammoniacal nitrogen source is added to raw water, and the ammoniacal nitrogen source is oxidized by nitrifying bacteria (ammonia oxidizing bacteria) to become nitrite ions (NO ₂ ⁻ ). Thus, the activity of the nitrifying bacteria group can be maintained and urea can be decomposed and removed. At this time, by adjusting the pH to 5 to 6.5, urea consumed by the nitrifying bacteria group increases, so that the activity of the nitrifying bacteria group can be maintained even if the urea concentration varies greatly. Can be effectively decomposed and removed.

It is a systematic diagram which shows the water treatment method which concerns on 1st embodiment of this invention. It is the schematic which shows the effect of said 1st embodiment. It is a systematic diagram which shows the water treatment method which concerns on 2nd embodiment of this invention. It is a systematic diagram which shows the ultrapure water manufacturing method using the water treatment method which concerns on one Embodiment of this invention. It is a graph which shows the urea removal effect of Example 1 and Comparative Example 1.

  Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings. FIG. 1 is a schematic view showing a water treatment method according to the first embodiment of the present invention.

In FIG. 1, reference numeral 1 denotes a pretreatment system for raw water W supplied from a raw water storage tank (not shown). The raw water W processed by the pretreatment system 1 is temporarily stored in a water supply tank 2. And this water supply tank 2 is following the biological treatment means 3, The raw | natural water W processed by this biological treatment means 3 can be supplied to a primary pure water apparatus as the treated water W1. A pH sensor and a supply unit 4 (not shown) are provided in the previous stage of the biological treatment unit 3, and an ammonia nitrogen source (NH ₄ ⁺ -N) and sulfuric acid as a pH adjuster can be added from the supply unit 4. It has become. In addition, 5 is a supply pipeline.

  In the biological treatment apparatus configured as described above, as raw water W to be treated, ground water, river water, city water, other industrial water, recovered water from a semiconductor manufacturing process, and the like can be used. The urea concentration in the raw water (treatment target water) W is preferably about 5 to 200 μg / L, particularly about 5 to 100 μg / L.

  Moreover, as the pretreatment system 1, a general pretreatment system or a treatment system similar to this in the production process of ultrapure water is suitable. Specifically, a treatment system comprising agglomeration, pressurized levitation, filtration, or the like can be used.

  The biological treatment means 3 is a means for performing a treatment for decomposing and stabilizing pollutants in wastewater such as sewage by biological action, and is classified into an aerobic treatment and an anaerobic treatment. In general, organic matter is decomposed by biological treatment through oxygen respiration, nitric acid respiration, fermentation processes, etc., and is gasified or taken into the body of microorganisms and removed as sludge. Moreover, the removal process of nitrogen (nitrification denitrification method) and phosphorus (biological phosphorus removal method) can also be performed. A means for performing such biological treatment is generally called a biological reaction tank. Such a biological treatment means 3 is not particularly limited, but preferably has a fixed bed of a biological carrier. In particular, a fixed bed of a downward flow type with less bacterial cell outflow is preferred.

  When the biological treatment means 3 is a fixed bed, it is preferable to wash the fixed bed as necessary. As a result, it is possible to prevent the occurrence of blockage of the fixed bed, mudballing, a decrease in the decomposition and removal efficiency of urea, and the like due to the growth of organisms (bacteria). There is no particular limitation on this cleaning method. For example, backwashing, that is, flowing the cleaning water in the direction opposite to the direction of passing raw water to fluidize the carrier, discharging sediment out of the system, It is preferable to perform pulverization, exfoliation of a part of the organism, and the like.

  In addition, there is no particular limitation on the type of carrier for the fixed bed, and activated carbon, anthracite, sand, zeolite, ion exchange resin, plastic molded product, etc. are used, but in order to carry out biological treatment in the presence of an oxidizing agent. It is preferable to use a carrier that consumes less oxidant. However, when there is a possibility that a high concentration oxidizing agent flows into the biological treatment means, it is preferable to use a carrier such as activated carbon that can decompose the oxidizing agent. Thus, when activated carbon etc. are used, even if it is a case where the density | concentration of the oxidizing agent in to-be-processed water is high, it is prevented that a microbial cell is inactivated and killed.

The water flow rate to the biological treatment means 3 is preferably about SV5 to 50 hr- ¹ . The temperature of the water supplied to the biological treatment means 3 is preferably normal temperature, for example, 10 to 35 ° C. Therefore, it is preferable to provide a heat exchanger before the biological treatment means as necessary.

  The ammoniacal nitrogen source added to the biological treatment means 3 from the supply means 4 is not particularly limited, and ammonium salt (inorganic compound), ammonia water (ammonium hydroxide), and ammonium by biodegradation of proteins and the like. An organic substance or the like that can generate ions or free ammonia can be suitably used. Among these, inorganic ammonium salts such as ammonium chloride are preferable.

  Next, a water treatment method using the apparatus and additives as described above will be described.

  First, by supplying the raw water W to the pretreatment system 1 and removing the turbid components in the raw water W, the efficiency of decomposition and removal of organic substances in the first biological treatment means 3 in the subsequent stage is reduced by the turbid components. And the increase in the pressure loss of the first biological treatment means 3 is suppressed.

  Then, if necessary, the pretreated raw water W is heated by a heat exchanger (not shown) when the raw water W has a low temperature and cooled to a predetermined water temperature when the raw water W has a high temperature. Adjust the temperature accordingly. That is, the higher the water temperature of the raw water W, the higher the reaction rate and the higher the decomposition efficiency. On the other hand, when the water temperature is high, it is necessary to impart heat resistance to the treatment tank of the biological treatment means 3 and the piping of the feed pipe 5, which leads to an increase in equipment cost. Moreover, when the water temperature of the raw | natural water W is low, it leads to the increase in heating cost. Specifically, if the water temperature of the biological reaction is 40 ° C. or lower, basically, the higher the water temperature, the higher the biological activity and removal rate. However, when the water temperature exceeds 40 ° C., the biological activity and removal efficiency may tend to decrease. For the above reasons, the treatment water temperature is preferably about 20 to 40 ° C. Therefore, if the initial temperature of the raw water W is within the above range, nothing needs to be done.

  In this way, the raw water W whose temperature has been adjusted as necessary is supplied to the biological treatment means 3 to decompose and remove organic substances, particularly persistent organic substances such as urea. At this time, an ammoniacal nitrogen source is added from the supply means 4 and sulfuric acid is added to adjust the pH of the raw water W to 5 to 6.5.

The addition amount of the ammoniacal nitrogen source as described above may be 0.1 to 5 mg / L (converted to NH ₄ ⁺ ). Specifically, it is added so that the concentration of ammonium ions in the raw water W is within the above range. If the ammonium ion concentration in the raw water W is less than 0.1 mg / L (converted to NH ₄ ⁺ ), it becomes difficult to maintain the activity of the nitrifying bacteria group, but even if it exceeds 5 mg / L (converted to NH ₄ ⁺ ) Further, not only the activity of the nitrifying bacteria group is not obtained, but also the amount of leak from the biological treatment means 3 becomes too large, which is not preferable.

  By adding an ammoniacal nitrogen source so that the concentration of ammonium ions in the raw water W is within the above range, the urea concentration in the treated water W1 in the biological treatment means 3 after about 10 to 30 days has elapsed is 5 μg / L or less, particularly 2 μg / L or less.

In this way, by adding an ammoniacal nitrogen source to the raw water W, urea and urea derivatives as TOC can be stably decomposed. This is presumably due to the following reasons. That is, it is known that the concentrations of urea and urea derivatives vary depending on the season in city water and industrial water. If the concentrations of urea and urea derivatives in raw water W are low, nitrification that assimilates urea. Even if the activity of the fungal group decreases and then the urea concentration rapidly increases, the activity of the nitrifying bacterial group cannot follow and cannot be completely decomposed, and therefore leaks into the treated water W1. Therefore, by adding an ammoniacal nitrogen source, the nitrifying bacteria group maintains its activity by oxidizing the ammoniacal nitrogen source into nitrite ions (NO ₂ ⁻ ). Thereby, the urea concentration of the treated water W1 in the biological treatment means 3 can be kept low by following the concentration fluctuations of urea and urea derivatives in the raw water W.

  The ammoniacal nitrogen source does not need to be added constantly. For example, a method of adding only during the start-up period at the time of exchanging the biological carrier, a method of repeating addition or non-addition every certain period, or the like can be used. Thus, by not always adding the ammoniacal nitrogen source, there is also an effect that the addition cost of the ammoniacal nitrogen source can be reduced.

  In addition, the activity of nitrifying bacteria decreases when there is no presence of food (ammonia nitrogen source, urea, urea derivatives, etc.) (air aeration) in the presence of dissolved oxygen. Specific measures for avoiding this decrease in activity include (1) a method of constantly or intermittently adding an ammoniacal nitrogen source (method according to the present invention), and (2) ammoniacal treatment in biologically treated feed water or treated water. (3) A method for controlling the dissolved oxygen concentration in the same manner as (2) above (addition of oxygen absorber, addition of reducing agent, degassing) Treatment, removal of dissolved oxygen by nitrogen gas aeration, etc.). From the viewpoint of simplicity and cost, the method of the present invention (method (1) above) is considered to be a more preferable method.

  Moreover, the reason for adjusting the pH of the raw water W to 5 to 6.5 at this time is as follows. That is, as shown in FIG. 2, the nitrifying bacteria group (ammonia oxidizing bacteria) having urea resolution can assimilate both urea and ammonia, and the substrate to be preferentially used varies depending on environmental conditions. For example, when the pH is high or the ammonia / urea ratio is high, ammonia is preferentially used and the urea resolution is rather lowered. Therefore, by adjusting the pH of the raw water W to 5 to 6.5, the nitrifying bacteria group having an optimum value in the neutral range has both ammonia oxidation activity and urea decomposition activity decreased compared to the optimum pH. The decrease in urea decomposition activity is less than the decrease in ammonia oxidation activity. Furthermore, ammonia in an ionic state increases, and the amount of ammonia taken into the ammonia oxidizing bacteria decreases. As a result, urea decomposed by nitrifying bacteria increases. By these actions, the activity of the nitrifying bacteria group can be maintained even if the urea concentration largely fluctuates, and urea can be effectively decomposed and removed. In addition, about the minimum of pH, when the pH of the raw | natural water W shall be less than 5, the activity of a nitrifying bacteria group will become large.

For the same reason, the ammonia nitrogen source added from the supply means 4 is preferably added so that the concentration of urea in the raw water W is 20 or less in terms of NH ₄ ⁺ -N / urea. If the concentration of the ammoniacal nitrogen source exceeds 20 times the concentration of urea, the nitrifying bacteria group, which is a urea-decomposing bacterium, will give priority to the degradation of the ammoniacal nitrogen source, so that the resolution of urea decreases, and urea The concentration cannot significantly follow the increase, and urea tends to leak into the treated water W1. In addition, since the effect of maintaining the activity of nitrifying bacteria due to the addition is reduced if the amount of the ammoniacal nitrogen source is too small, NH ₄ ⁺ -N / urea is preferably set to 1 or more.

  In addition, in this raw | natural water W, an oxidizing agent and / or a disinfectant can be further added as needed. There is no restriction | limiting in particular in the kind of oxidizing agent and / or disinfectant to add, What can give priority to the bacterial species which decomposes | disassembles urea efficiently is used suitably. Specifically, a chlorine-based oxidizing agent such as sodium hypochlorite and chlorine dioxide, a combined chlorine agent (stabilized chlorine agent) such as monochloramine and dichloroamine, and the like can be suitably used.

  Next, a water treatment method according to the second embodiment of the present invention will be described with reference to FIG. The water treatment method of the second embodiment has the same configuration as that of the first embodiment described above except that the reduction treatment means 6 is provided after the biological treatment means 3 and before the primary pure water device.

  By adopting such a configuration, in the first embodiment described above, when a chlorine-based oxidant (such as hypochlorous acid) is used and surplus chlorine is present, these are ammoniacal nitrogen sources. Reacts with bound chlorine compounds. Although this bonded chlorine compound has a lower oxidizing power than free chlorine, it may cause oxidative deterioration of the components of these components in the subsequent primary pure water device, etc. These bound chlorine compounds can be rendered harmless.

  In addition, when activated carbon is used as a fixed bed of the biological support carrier of the biological treatment means 3, it is known that activated carbon can reduce a chlorine-based oxidizing agent by a catalytic reaction, but it cannot rapidly reduce bound chlorine compounds. Even if activated carbon is used, it is preferable to provide the reduction treatment means 6 because it easily leaks and may remain and affect the subsequent primary pure water device.

  Examples of the reduction treatment means 6 include gases such as hydrogen gas, lower oxides such as sulfur dioxide, lower oxygenates such as thiosulfate, sulfite, bisulfite, and nitrite, iron (II) salts, and the like. Other reducing agents such as low-valent metal salts, organic acids such as formic acid, oxalic acid, and L-ascorbic acid or salts thereof, hydrazine, aldehydes, and saccharides may be added. Among these, nitrite, sulfite, iron (II) salt, sulfur dioxide, bisulfite, oxalic acid or a salt thereof and L-ascorbic acid or a salt thereof can be preferably used. Further, as the reduction treatment means 6, an activated carbon tower may be provided and further reduction may be performed with activated carbon.

When the reducing agent is added, for example, when the reducing agent is sodium sulfite, the amount of sulfite ion (SO ₃ ²⁻ ) and hypochlorite ion (ClO ⁻ ) is equal to or greater than equimolar. What is necessary is just to add and it should just add 1.2-3.0 times amount in consideration of safety | security. Since there is a fluctuation in the oxidizing agent concentration of the treated water, it is more preferable to monitor the oxidizing agent concentration of the treating water and control the reducing agent addition amount according to the oxidizing agent concentration. For simplicity, a method may be used in which the oxidant concentration is measured periodically and the addition amount corresponding to the measured concentration is set appropriately. Examples of means for detecting the oxidant concentration include an oxidation-reduction potential (ORP) and a residual chlorine meter (such as a polarographic method) for residual chlorine.

  Specifically, when ammonium chloride or the like is added as an ammoniacal nitrogen source in the state where free chlorine is present in the biological treatment water (raw water) W, the free chlorine reacts with ammonium ions to form combined chlorine (chloramine). ) Is generated. Bound chlorine is a component that is harder to remove even with activated carbon than free chlorine, and the bound chlorine leaks into biologically treated water. Bound chlorine is said to be a component with low oxidizing power compared to free chlorine, but it is also known that free chlorine is generated again from bound chlorine by an equilibrium reaction. May cause degradation.

  A slime control agent may be added to the raw water W treated by the biological treatment means 3. The slime control agent is a failure in the subsequent treatment caused by the microbial cells contained in the treated water of the biological treatment means 3 (microbial cells detached from the biological carrier) (slime failure such as clogging of piping, increased differential pressure, RO What is necessary is just to add suitably as needed for the purpose of avoiding the biofouling etc. of a film | membrane.

  Furthermore, you may remove the microbial cell contained in the treated water of the biological treatment means 3 with a microbial cell separation apparatus as needed.

  The addition of the reducing agent and / or slime control agent and the treatment with the bacterial cell separation device may be appropriately performed in accordance with the quality of the biologically treated water from the biological treatment means 3, and the water quality is good. If you do not have to.

  According to the water treatment method according to the first and second embodiments described above, the treated water W1 obtained by highly decomposing and removing urea can be obtained. By further treating this with a pure water production apparatus, the urea concentration It is possible to produce ultrapure water with extremely low.

  Next, an embodiment of the ultrapure water production method using the water treatment method of the present invention will be described with reference to FIG. In the ultrapure water production method in the present embodiment, raw water W is treated by the pretreatment system 11, the biological treatment device 12, the fungus body separation means 13, and the reduction treatment means 14, and then the treated water W1 is treated with the primary pure water device 15 and Further processing is performed by a subsystem (secondary pure water device) 19. As the bacterial cell separation means 13, a filter, a cartridge filter, a microfiltration membrane separation device, an ultrafiltration membrane separation device, or the like can be used. In addition, as the biological treatment apparatus 12, what was shown by the 1st and 2nd water treatment method mentioned above is used.

  The primary pure water device 15 includes a first reverse osmosis membrane (RO) separation device 16, a second reverse osmosis membrane (RO) separation device 17, and a mixed bed ion exchange device 18 arranged in this order. . However, the device configuration of the primary pure water device 15 is not limited to such a configuration. For example, a reverse osmosis membrane separation device, an ion exchange treatment device, an electrodeionization exchange treatment device, a UV oxidation treatment device, etc. You may comprise suitably combining.

  The sub-system 19 includes a sub-tank 20, a heat exchanger 21, a low-pressure ultraviolet oxidizer 22, a mixed bed ion exchanger 23, and a UF membrane separator 24 in this order. However, the apparatus configuration of the subsystem 19 is not limited to such a configuration. For example, a degassing apparatus, a UV oxidation apparatus, an ion exchange apparatus (non-regenerative type), an ultrafiltration membrane apparatus (Particle removal) or the like may be combined.

  An ultrapure water production method using such an ultrapure water production system will be described below. First, the pretreatment system 11 includes agglomeration, pressurized flotation (precipitation), filtration (membrane filtration) apparatus, and the like. In the pretreatment system 11, suspended substances and colloidal substances in the raw water are removed. The pretreatment system 11 can also remove high molecular organic substances, hydrophobic organic substances, and the like.

To the effluent from the pretreatment system 11, an ammonia nitrogen source (NH ₄ ⁺ -N) is added and sulfuric acid as a pH adjuster is added to adjust the pH. If necessary, an oxidizing agent and After the disinfectant is added, the biological treatment described above is performed by the biological treatment device 12. The microbial cell separation means 13 installed on the downstream side of the biological treatment apparatus 12 separates and removes microorganisms, carrier particles, and the like flowing out from the biological treatment apparatus 12. This microbial cell separation means 13 may be omitted. Since the effluent water of the biological treatment apparatus 12 may contain bound chlorine compounds as described above, the reduced chlorine treatment means detoxifies the bound chlorine compounds. When there is almost no concentration of the chlorine-based oxidant in the raw water W, since the bound chlorine compound is hardly contained in the effluent water of the biological treatment apparatus 12, even if the addition of the reducing agent in the reduction treatment means 14 is omitted. Good.

  In the primary pure water treatment device 15, the biological treatment device 12 includes a first reverse osmosis (RO) membrane separation device 16, a second reverse osmosis (RO) membrane separation device 17, and a mixed bed ion exchange device 18. The ionic component remaining in the treated water W1 is removed.

  Further, in the sub-system 19, the treated water of the primary pure water device 15 is introduced into the low-pressure ultraviolet oxidizer 22 through the sub-tank 20 and the heat exchanger 21, and the contained TOC component is ionized or decomposed. Among these, the ionized organic matter is removed by the mixed bed ion exchanger 23 at the subsequent stage. The treated water of the mixed bed type ion exchange device 23 is further subjected to membrane separation treatment by the UF membrane separation device 24, and ultrapure water W2 can be obtained.

  According to the ultrapure water production method as described above, urea is sufficiently decomposed and removed in the biological treatment apparatus 12, and other TOC components, metal ions, other By removing the inorganic / organic ion component, it is possible to efficiently produce ultrapure water W2 having high purity from which urea has been removed to a high degree.

  Moreover, according to the said ultrapure water manufacturing method, before introducing raw | natural water W into the biological treatment apparatus 12, it introduce | transduces into the pre-processing system 11 and removes the turbidity in the raw | natural water W. For this reason, the decomposition and removal efficiency of urea in the biological treatment apparatus 12 is prevented from decreasing due to turbidity, and an increase in pressure loss of the biological treatment apparatus 12 due to the turbidity is suppressed. Moreover, according to this ultrapure water production method, since the microbial cell separating means 13, the primary pure water device 15 and the subsystem 19 are provided on the downstream side of the biological treatment device 12, organisms flowing out from the biological treatment device 12 or There is also an effect that the carrier can be satisfactorily removed by the bacterial cell separation means 13, the primary pure water device 15, and the subsystem 19.

  The following examples illustrate the invention in more detail.

[Example 1]
As simulated raw water W, water (Nogi-cho water: average urea concentration 10 μg / L, average TOC concentration 500 μg / L, ammonium ion concentration less than 0.1 mg / L) and reagent urea (manufactured by Kishida Chemical Co., Ltd.) appropriately added Was used.

  In the apparatus having the configuration shown in FIG. 1, as a biological treatment means 3, a cylindrical container is charged with 2 L of granular activated carbon (“Crycol WG160, 10/32 mesh”, manufactured by Kurita Kogyo Co., Ltd.) to form a fixed bed. Was used. In addition, as granular activated carbon of the biological treatment means 3, after washing | cleaning new charcoal, it filled by immersing in 2 L of city waters which added 200 mL of nitrification sludge, and started water flow after that.

Since the water temperature of the city water was 25 to 28 ° C. and the pH was 6.5 to 7.5 during the test period, the water temperature of the simulated raw water W was adjusted to about 25 ° C. using a heat exchanger. In such a biological treatment apparatus, after pre-treating the simulated water 1 with the pre-treatment system 1, sulfuric acid is added from the supply means 4 to adjust the pH of the simulated raw water to about 6.0 to 6.5, Ammonium chloride (manufactured by Kishida Chemical Co., Ltd.) was added as an ammoniacal nitrogen source so that the ammonium ion concentration was about 0.5 mg / L (NH ₄ ⁺ conversion). The raw water W to which these were added was passed through the biological treatment means 3 in a downward flow. The water flow rate SV was 20 / hr (water flow rate per hour ÷ filled activated carbon amount). In the water flow treatment, back washing was performed once a day for 10 minutes. Backwashing was performed with biologically treated water in an upward flow from the lower part of the cylindrical container to LV = 25 m / hr (per hour water flow rate ÷ cylinder container sectional area).

  Under the water flow conditions as described above, continuous flow of the raw water W was performed for 60 days, and the urea concentration of the treated water was analyzed. At this time, first, water is passed for 27 days at a urea concentration of about 100 μg / L in the raw water W, and then, after the 28th day, water is passed through to the 41st day (14 days) at a urea concentration of about 25 μg / L in the raw water W. From the 42nd day, the urea concentration of the raw water W was again adjusted to about 100 μg / L. The result is shown in FIG. 5 together with the fluctuation of the urea concentration in the raw water.

  The procedure for analyzing the urea concentration is as follows. That is, first, the total residual chlorine concentration of the test water is measured by the DPD method and reduced with a considerable amount of sodium bisulfite (then, the total residual chlorine is measured by the DPD method, and less than 0.02 mg / L). Confirm that it is.) Next, this reduced test water was passed through an ion exchange resin (“KR-UM1”, Kurita Kogyo Co., Ltd.) at SV50 / hr, deionized, and concentrated 10 to 100 times with a rotary evaporator. Thereafter, the urea concentration is quantified by the diacetyl monooxime method.

  As is apparent from FIG. 5, in Example 1 in which an ammoniacal nitrogen source was added and the pH was adjusted to about 6.0 to 6.5, the urea concentration of the treated water was 2 μg / L on the 21st day. From the 42nd day, the urea concentration in the raw water W was again maintained at about 100 μg / L, and this was maintained.

[Comparative Example 1]
In Example 1, the raw water W was treated in the same manner except that the pH of the raw water W was adjusted to 7.0 to 7.5. An analysis of the urea concentration when the raw water W was continuously passed over 60 days was performed. The results are shown in FIG.

  As is apparent from FIG. 5, in Comparative Example 1 in which an ammoniacal nitrogen source was added and the pH was adjusted to about 7.0 to 7.5, which was almost neutral, urea was treated on the 21st day. Although the concentration became 2 μg / L, when the urea concentration of the raw water W was again set to about 100 μg / L from the 42nd day, the urea concentration of the treated water rose to 10 μg / L or more, and thereafter 10 μg / L during the period. I kept maintaining the neighborhood. It was confirmed that all the ammoniacal nitrogen sources added during this period were converted to nitric acid.

  By applying such a biological treatment apparatus to the production of ultrapure water, a method for producing ultrapure water that can highly remove urea in raw water can be obtained.

3 ... biological treatment means 4 ... supply means 6 ... reduction treatment means 14 ... reduction treatment means 15 ... primary pure water device 19 ... subsystem (secondary pure water device)
W ... Raw water W1 ... treated water W2 ... ultrapure water

Claims (7)

In a water treatment method for biologically treating raw water containing organic matter,
A water treatment method characterized in that after adding an ammoniacal nitrogen source to raw water, the pH is adjusted to 5 to 6.5 to perform biological treatment. 2. The water treatment method according to claim 1, wherein the ammoniacal nitrogen source is 20 or less in terms of NH ₄ ⁺ -N / urea with respect to the concentration of urea.   The water treatment method according to claim 1 or 2, wherein the biological treatment is a biological treatment means having a biological carrier.   The water treatment method according to claim 3, wherein the biological treatment is a biological treatment means having a fixed bed of a biological carrier.   The water treatment method according to any one of claims 1 to 4, wherein the ammoniacal nitrogen source is an ammonium salt.   The water treatment method according to any one of claims 1 to 5, wherein a reduction treatment is performed after the biological treatment.   Ultrapure water characterized by producing ultrapure water by treating the treated water obtained by the water treatment method according to any one of claims 1 to 6 with a primary pure water device and a secondary pure water device. Water production method.

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