Method for treating organic-matter-containing water

Abstract

Disclosed is a treatment apparatus capable of inhibiting growth of microorganisms and carrying out long-term stable treatment in an activated carbon tower and a reverse osmosis membrane separation device during processes including activated carbon treatment and RO membrane separation treatment of a later step in a system for manufacturing ultrapure water used in an electronic device factory. A method for treating organic-matter-containing water includes: the slime-controlling-agent-adding step of adding a slime-controlling agent to organic-matter-containing water; the activated-carbon-treating step of treating with activated carbon the organic-matter-containing water having undergone the slime-controlling-agent-adding step; and the reverse-osmosis-membrane-separation step of passing the organic-matter-containing water having undergone the activated-carbon-treating step through means for reverse osmosis membrane separation, wherein the slime-controlling agent uses a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound.

Claims

1. A method for treating organic-matter-containing water, comprising: a slime-controlling agent preparation step of preparing a slime-controlling agent comprising a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound such that an amount of the sulfamic acid compound per mol of an effective chlorine in the chlorine-based oxidizer is 0.5 to 5.0 mol; a slime-controlling-agent adding step of adding the slime-controlling agent to organic-matter-containing water in a concentration of the combined chlorine agent between 0.1-10 mg-Cl.sub.2/L; an activated-carbon-treating step of treating with activated carbon the organic-matter-containing water having undergone the slime-controlling-agent-adding step, the combined chlorine agent leaking in an activated carbon device to inhibit proliferation of viable cells in the activated carbon device; and a reverse-osmosis-membrane-separation step of passing the organic-matter-containing water having undergone the activated-carbon-treating step through a reverse osmosis membrane separation device comprising an aromatic polyamide membrane, the combined chlorine agent leaking in the activated carbon device further preventing biofouling and a decrease in flux due to an attachment of organic matter onto a membrane surface in a reverse osmosis membrane separation device.

2. The method according to claim 1, wherein the chlorine-based oxidizer is at least one selected from the group consisting of chlorine gas, chlorine dioxide, hypochlorous acid or salts thereof, chlorous acid or salts thereof, chloric acid or salts thereof, perchloric acid or salts thereof, and chlorinated isocyanuric acid or salts thereof.

3. The method according to claim 1, wherein the chlorine-based oxidizer is at least one of sodium hypochlorite and potassium hypochlorite.

4. The method according to claim 1, wherein the sulfamic acid compound is at least one selected from the group consisting of sulfamic acid, N-methyl sulfamic acid, N,N-dimethyl sulfamic acid, N-phenyl sulfamic acid, and salts thereof.

5. The method according to claim 1, wherein the sulfamic acid compound is at least one of sodium sulfamate and potassium sulfamate.

6. The method according to claim 1, further comprising, before or after the slime-controlling-agent adding step, a removing step of removing a suspended matter in the organic matter-containing-water by a filtration, the organic matter-containing-water after the removing step being supplied to the activated carbon device.

7. The method according to claim 6, wherein the removing step includes a step of adjusting pH in the organic matter-containing-water to optimize flocculation, a step of adding a flocculant to the organic matter-containing-water, and a step of removing the suspended matter.

8. The method according to claim 6, wherein the filtration is pressure filtration, gravity filtration, microfiltration, ultrafiltration, pressurized flotation, or precipitation.

9. A method for treating organic-matter-containing water, comprising: a slime-controlling-agent-adding step of adding a slime-controlling agent comprising a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound to organic-matter-containing water in a concentration of the combined chlorine agent between 1 and 50 mg-Cl.sub.2/L; an activated-carbon-treating step of treating with activated carbon the organic-matter-containing water having undergone the slime-controlling-agent-adding step to inhibit proliferation of viable cells in an activated carbon device; a reverse-osmosis-membrane-separation step of passing the organic-matter-containing water having undergone the activated-carbon-treating step through a reverse osmosis membrane separation device, to prevent biofouling and a decrease in flux due to an attachment of organic matter onto a membrane surface in a reverse osmosis membrane separation device; a hardness-component-removing step of decreasing hardness by passing the organic-matter-containing water having undergone the activated-carbon-treating step through a cation-exchange device; a scale inhibitor-adding step of adding five-fold excess by weight or more of a scale inhibitor per calcium ion contained in the organic-matter-containing water having undergone the hardness-component-removing step to the organic-matter-containing water having undergone the hardness-component-removing step; and a pH-adjusting step of adjusting pH of the organic-matter-containing water to be injected into the reverse osmosis membrane separation device of a later step to 9.5 or more by adding an alkali to the organic-matter-containing water before, after, or at the same time as the scale inhibitor-adding step.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a systematic diagram showing a method and apparatus for treating organic-matter-containing water of an embodiment of the present invention.

(2) FIG. 2 is a systematic diagram showing a method and apparatus for treating organic-matter-containing water of another embodiment of the present invention.

(3) FIG. 3 is a graph showing a change over time in the concentration of chlorine leaked from an activated carbon tower when compared between Example 1 and Comparative Example 1.

DESCRIPTION OF EMBODIMENTS

(4) Hereinafter, the present invention is further illustrated in detail.

(5) First, a slime-controlling agent for activated carbon of the present invention is described in detail.

(6) A slime-controlling agent for activated carbon of the present invention includes a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound.

(7) Examples of the chlorine-based oxidizer used in the present invention can include, but are not limited to, chlorine gas, chlorine dioxide, hypochlorous acid or salts thereof, chlorous acid or salts thereof, chloric acid or salts thereof, perchloric acid or salts thereof, chlorinated isocyanuric acid or salts thereof, and the like. Among them, specific examples of the salts can include alkali metal hypochlorite such as sodium hypochlorite and potassium hypochlorite, alkali metal chlorite such as sodium chlorite and potassium chlorite, alkali metal chlorate such as ammonium chlorate, sodium chlorate, and potassium chlorate, alkaline earth metal chlorate such as calcium chlorate and barium chlorate, and the like. For these chlorine-based oxidizers, one kind can be used solely, or two kinds or more can be combined to be used. Among them, hypochlorous acid can be preferably used because they are easily handled.

(8) As the sulfamic acid compound, examples can include a compound or a salt thereof, the compound represented by the following general formula [1]:

(9) ##STR00001##

(10) In the general formula [1], R.sup.1 and R.sup.2 each independently represent hydrogen or hydrocarbon having a carbon number of 1 to 8. As these sulfamic acid compounds, examples can include, in addition to sulfamic acid where both R.sup.1 and R.sup.2 are hydrogen, N-methyl sulfamic acid, N,N-dimethyl sulfamic acid, N-phenyl sulfamic acid, and the like. Examples of the salt of the sulfamic acid compound can include, alkali metal salts such as sodium salts and potassium salts, ammonium salts, guanidine salts, and the like. Specific examples can include sodium sulfamate, potassium sulfamate, and the like. For the sulfamic acid and sulfamate thereof, one kind can be used solely, or two kinds or more can be combined to be used.

(11) When a chlorine-based oxidizer such as hypochlorite and a sulfamic acid compound such as sulfamate are blended, these compounds are combined to form chloro sulfamate and are stabilized. Without causing a difference in dissociation due to pH as for conventional chloramine or causing the resulting change in the concentration of free chlorine, these compounds enable the concentration of free chlorine to be kept stable in water.

(12) In the present invention, the ratio of the chlorine-based oxidizer to the sulfamic acid compound is not particularly limited. However, the amount of the sulfamic acid compound per mol of effective chlorine in the chlorine-based oxidizer is preferably set to 0.5 to 5.0 mol, and more preferably 0.5 to 2.0 mol.

(13) A slime-controlling agent for activated carbon of the present invention may contain, within a degree to which its effect is not impaired, an additional component other than a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound. Examples of the additional component can include alkaline agents, azoles, anionic polymers, phosphonates, and the like.

(14) The alkaline agent is used for stabilizing the combined chlorine agent contained in the slime-controlling agent for activated carbon. Usually, sodium hydroxide or potassium hydroxide, etc., is used.

(15) In the case of inclusion of the additional component, a dosage form of the slime-controlling agent for activated carbon of the present invention is not particularly limited. The dosage form can be a one-liquid type agent containing a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound, and one or more kinds selected from azoles, anionic polymers, and phosphonates. The dosage form can also be a two-liquid type agent in which the respective components are divided into two kinds of liquid. As the two-liquid type agent, examples can include, a two-liquid type agent containing solution A including a combined chlorine agent produced from a chlorine-based oxidizer and a sulfamic acid compound and solution B including additional components.

(16) In the case of the one-liquid type agent, in order to maintain the stability of the combined chlorine agent, an alkali such as sodium hydroxide and potassium hydroxide is preferably added to adjust pH to 12 or more, and more preferably to adjust pH to 13 or more. In the case of the two-liquid type agent, the pH of the agent containing the combined chlorine agent is preferably similarly adjusted to 12 or more, and more preferably adjusted to 13 or more.

(17) A method for passing water through an activated carbon device according to the present invention is to prevent slime-mediated damage by including such a slime-controlling agent for activated carbon of the present invention in water supplied to the activated carbon device or flushing water.

(18) In this case, the concentration of the combined chlorine agent in water may be a degree to which an initial effect of preventing slime can be achieved. The concentration of the combined chlorine agent to be added is preferably, but is not particularly limited to, between 0.1 and 10 mg/L, and particularly between 1 and 5 mg/L. An activated carbon tower is suitable for the activated carbon device.

(19) A slime-controlling agent of the present invention may be added to water flowing into the activated carbon device. Sodium hypochlorite may be added to the water flowing into the activated carbon device, and the slime-controlling agent of the present invention may be added to flushing water at the time of back washing. The latter can decrease the usage of the slime-controlling agent and can reduce the cost of the agent.

(20) When an RO membrane device is provided in the step following the activated carbon device, a slime-controlling agent is preferably added to the water flowing into the activated carbon device as described in an embodiment of the following method and apparatus for treating organic-matter-containing water.

(21) Hereinafter, by referring to the drawings, embodiments of a method and apparatus for treating organic-matter-containing water according to the present invention are described in detail.

(22) FIGS. 1 and 2 are systematic diagrams showing embodiments of a method and apparatus for treating organic-matter-containing water according to the present invention. In figures, the symbol P denotes a pump.

(23) In FIG. 1, in a flocculation tank 2, a slime-controlling agent for activated carbon of the present invention and a flocculant, and, if needed, a pH modifier are added to raw water (e.g., organic-matter-containing water such as industrial water) which is injected by way of a raw water tank 1. Then, the water passes through, in turn, a pressure filtration tower 3, an activated carbon tower 4, and filter-treatment water tank 5. After that, the water passes through a safety filter 6 and is injected into an RO membrane separation device 7 to be subjected to RO membrane separation treatment.

(24) Examples of water exemplified include, but are not limited to, a variety of industrial water such as ground water and river water, and factory drainage such as drainage from processes for manufacturing a semiconductor device.

(25) For the slime-controlling agent added, the concentration of the combined chlorine to be added is preferably 1 mg-Cl.sub.2/L or more, and more preferably between 1 and 50 mg-Cl.sub.2/L. In general, due to a poor ability of degradation and removal of the combined chlorine agent in the activated carbon, the agent immediately leaks from the activated carbon tower 4 of a later step to be able to achieve a sterilization effect. However, when the additive concentration is less than 1 mg-Cl.sub.2/L or the flow SV in the activated carbon tower 4 is less than 20 hr.sup.1, the concentration at which the agent leaks from the activated carbon tower becomes markedly low. Then, slime sometimes grows in the activated carbon tower 4 or a device (e.g., a softening tower 8 of FIG. 2) installed at a later step. In addition, an excessively large amount of application of the combined chlorine agent markedly increases the cost of the agent, so that the concentration of the combined chlorine is preferably set to 50 mg-Cl.sub.2/L or less.

(26) In addition, in the case of presence of suspended matter in raw water, as shown in FIG. 1, after or before a slime-controlling agent is added, pH is adjusted to a pH range having optimal flocculation. Then, a flocculant is added and the suspended matter is removed beforehand by flocculation filtration, etc. After that, the water is preferably made to pass through the activated carbon tower. This means for flocculation filtration can be, but is not particularly limited to, any means capable of removing the suspended matter in the raw water by performing treatment such as pressure filtration, gravity filtration, microfiltration, ultrafiltration, pressurized flotation, and precipitation.

(27) Examples of the activated carbon used in the activated carbon tower 4 include, but are not particularly limited to, coal-based one, coconut-shell-based one, and the like. Examples of the shape include, but are not particularly limited to, particulate activated carbon, spherical activated carbon, and the like.

(28) Examples of the type of the activated carbon tower 4 include, but are not particularly limited to, a fluidized bed, an immobilized bed, and the like. In view of inhibition of leak of powdered coal, the immobilized bed is preferable.

(29) The lower flow SV in this activated carbon tower 4 increases the amount of the combined chlorine agent which is removed by the activated carbon tower 4. Accordingly, the effect of inhibiting slime growth in a later step is lowered. Thus, the flow SV in the activated carbon tower 4 is preferably set to 20 hr.sup.1 or more. Provided that the flow SV in the activated carbon tower 4 is excessively high, the effect of removing an oxidizer, organic matter, and chromaticity, etc, which is derived from the raw water in the activated carbon tower 4 decreases. Accordingly, the flow SV in the activated carbon tower 4 is preferably set to, in particular, 50 hr.sup.1 or less, and especially between 20 and 40 hr.sup.1.

(30) In FIG. 2, after a slime-controlling agent of the present invention and, if needed, a pH modifier are added to raw water which is injected by way of a raw water tank 1, the water is made to pass through, in turn, an activated carbon tower 4 and a softening tower 8. Then, five-fold excess or more of a scale dispersant per calcium ion concentration in water drained from the softening tower 8 (hereinafter, sometimes referred to as softened treated water) is added. After that, an alkali is added to adjust pH to 9.5 or more. By way of an intermediate tank 9, the water is then injected into an RO membrane separation device 7 while keeping the high pH state to be subjected to RO membrane separation treatment.

(31) In FIG. 2, the addition of the slime-controlling agent and the treatment in the activated carbon tower 4 are carried out in a manner similar to FIG. 1.

(32) The ion-exchange resin used in the softening tower 8 can be any resin capable of removing hardness components in raw water, including, but being not particularly limited to, an H-type cation exchange resin whose ion exchange group is H, an Na-type cation exchange resin whose ion exchange group is Na, a chelating resin, and the like. In addition, examples of the type of the softening tower 8 include, but are not particularly limited to, a fluidized bed, an immobilized bed, and the like.

(33) Besides, in the present invention, the treatment of removing hardness components is not limited to a softening tower, but a cation-exchange tower can be used. Further, the treatment is not limited to a tower type. However, in a manner similar to the activated carbon tower, the tower type is preferable from an aspect of treatment efficiency.

(34) The flow SV in the softening tower 8 or cation-exchange tower is not particularly limited. From aspects of the treatment efficiency and the effect of removing hardness components, the treatment is usually carried out at the SV of between 10 and 40 hr.sup.1.

(35) As a scale inhibitor which is added to treated water from the softening tower 8, a chelator-based scale inhibitor such as nitrilotriacetic acid (NTA) and ethylenediaminetetraacetic acid (EDTA) which readily forms a complex with a metal ion by dissociation in an alkaline range is preferably used. However, additional examples which can be used include (meth)acrylic acid polymers and salts thereof, low-molecular-weight polymers such as maleic acid polymers and salts thereof, ethylenediamine tetramethylene phosphonic acid and salts thereof, hydroxyethylidene diophosphonic acid and salts thereof, nitrilotris(methylene) phosphonic acid and salts thereof, phosphonic acid and phosphonate such as phosphonobutane tricarbonic acid and salts thereof, hexametaphosphoric acid and salts thereof, polymerized inorganic phosphoric acid and polymerized inorganic phosphate such as tripolyphosphoric acid and salts thereof, and the like. For these scale inhibitors, one kind can be used solely, or two kinds or more can be combined to be used.

(36) The additive amount of the scale inhibitor is set to five-fold excess by weight or more per calcium ion concentration in water effluent from the softening tower 8 (i.e., water to which the scale inhibitor is added). When the additive amount of the scale inhibitor is less than five-fold excess by weight per calcium ion concentration in the softened treated water, a sufficient effect of adding the scale inhibitor cannot be achieved. Addition of an excessively large amount of the scale inhibitor is not preferable from an aspect of the cost of the agent. Accordingly, the amount is preferably set to between 5- and 50-fold excess by weight per calcium ion concentration in the softened treated water.

(37) Next, to the water to which the scale inhibitor has been added is added an alkali. Then, the pH of the water (RO supply water) which is injected into the RO membrane separation device 7 of a later step is adjusted to 9.5 or more, preferably 10 or more, more preferably between 10.5 and 12, and, for example, between pH 10.5 and 11. The alkali used herein can be any inorganic-based alkaline agent capable of adjusting pH of the RO supply water to 9.5 or more, including, but being not particularly limited to, sodium hydroxide, potassium hydroxide, and the like.

(38) The location at which the scale dispersant and the alkali are added can be any location between the softening tower 8 and the RO membrane separation device, and does not have any particular limitation. The order of adding these agents can be any order. However, in order to completely inhibit proliferation of microorganisms in the system and to completely inhibit scale generation in the system, preferably, the scale dispersant is added, and the alkali is then added to adjust pH of the RO supply water to 9.5 or more.

(39) In the present invention, a reductant can be used as needed to degrade and remove the remaining combined chlorine agent by reduction treatment. The reductant used herein can be any reductant capable of removing the combined chlorine agent, including, but being not particularly limited to, sodium bisulfite and the like. For the reductant, one kind can be used solely, or two kinds or more can be combined to be used. The additive amount of the reductant can be an amount capable of completely removing the remaining combined chlorine agent. The reductant is usually added at the inlet side of the softening tower 8. However, the combined chlorine agent has a week effect of deteriorating an RO membrane. Thus, the degradation treatment for the combined chlorine agent by the reductant is usually unnecessary.

(40) Examples of the RO membrane of the RO membrane separation device 7 as shown in FIGS. 1 and 2 include those having alkaline resistance such as, for example, a polyether amide composite membrane, a polyvinyl alcohol composite membrane, and an aromatic polyamide membrane. Preferably, the RO membrane uses a polyvinyl alcohol-based low-fouling RO membrane having a salt elimination capability in which a salt elimination rate at the RO membrane separation treatment of 1,500 mg/L of the sodium chloride solution under conditions of 1.47 MPa, 25 C., and pH 7 (hereinafter, simply referred to as the salt elimination rate) is 95% or more. The preferable reasons for using such the low-fouling RO membrane are as follows.

(41) Specifically, when compared to an aromatic polyamide membrane that is usually used, the above low-fouling RO membrane has no charge on the membrane surface and improves in hydrophilicity. Accordingly, the above is markedly superior in contamination resistance. However, for water containing a large amount of a nonionic detergent, the effect of the contamination resistance is reduced, and the flux decreases over time.

(42) By adjusting pH of the RO supply water to 9.5 or more, the nonionic detergent which may decrease the RO membrane flux detaches from the membrane surface. Because of this, even if a typically employed aromatic polyamide membrane is used, a dramatic decrease in the flux can be inhibited. However, when the concentration of the nonionic detergent in the RO supply water is high, the foregoing effect decreases, which results in a decrease in the flux in a long term.

(43) Here, the polyvinyl alcohol-based low-fouling RO membrane having the above specific salt elimination capability is used, and is preferably combined with conditions in which the RO supply water passes through at pH of 9.5 or more. Due to this, a long-term stable operation can be carried out without causing a decrease in the flux for the RO supply water containing a high concentration of the nonionic detergent.

(44) The RO membrane can be any type such as a spiral type, a hollow-fiber type, and a tube type.

(45) Next, to water which permeates through the RO membrane separation device (hereinafter, sometimes referred to as the RO treated water) is added an acid to adjust pH to between 4 and 8. Further, the activated carbon treatment is carried out depending on the need. Then, the water is reused or released. Examples of the acid used herein include, but are not limited to, mineral acid such as hydrochloric acid and sulfuric acid.

(46) The concentrated water in the RO membrane separation device 7 (hereinafter, sometimes referred to as the RO concentrated water) is drained outside the system to be treated.

(47) In addition, FIGS. 1 and 2 represent examples of an embodiment of the present invention. As long as does not exceed its purport, the present invention is not limited to those illustrated. For example, the treatment by the RO membrane separation device is not limited to one-step treatment, and can be multistep treatment having two steps or more. Furthermore, a mixing tank to adjust pH or to add a scale inhibitor, etc., can be provided.

EXAMPLES

(48) Hereinafter, by referring to Examples and Comparative Examples, the present invention is more specifically described.

Example and Comparative Example of Embodiment Shown in FIG. 1

Example 1

(49) To industrial water containing 1 mg/LasC of TOC was added, as a combined chlorine concentration, 5 mg-Cl.sub.2/L of a slime-controlling agent including a combined chlorine agent produced from sodium hypochlorite and a sulfamic acid compound (specifically, sodium sulfamate) (a molar ratio of 1 mol of the sulfamine compound to effective chlorine is 1.5). Then, flocculation filtration treatment was carried out under conditions in which the additive amount of PAC (polyaluminum chloride) was 10 mg/L and the pH was 6. The flocculation filtration treated water was made to pass through an activated carbon tower under conditions at the SV of 20 hr.sup.1. Then, the water was made to pass through an RO membrane separation device (an ultralow-pressure aromatic polyamide-type RO membrane, ES-20, manufactured by NITTO DENKO CORPORATION) under conditions at the flow volume of 60 L/hr and at the recovery rate of 80%. The pH of RO supply water was 5.5.

Comparative Example 1

(50) Treatment was carried out under the conditions identical to those of Example 1, except that to industrial water containing 1 mg/LasC of TOC was added, as a combined chlorine concentration, between 8 and 10 mg-Cl.sub.2/L of chloramine having a reaction product of sodium hypochlorite with ammonia.

(51) In Example 1 and Comparative Example 1, the concentrations of the combined chlorine in water effluent from the activated carbon tower were determined. FIG. 3 showed the results.

(52) As described in FIG. 3, Example 1 clearly demonstrated that chlorine leaked from the activated carbon tower in an early time point.

Example and Comparative Example of Embodiment Shown in FIG. 2

Example 2

(53) To drainage containing a nonionic detergent and having the TOC concentration of 20 mg/L and the calcium concentration of 5 mg/L was added, as a combined chlorine concentration, 1 mg-Cl.sub.2/L of the same slime-controlling agent as Example 1. Then, flocculation filtration treatment was carried out under conditions in which the additive amount of PAC (polyaluminum chloride) was 20 mg/L and the pH was 6.5. The flocculation filtration treated water was made to pass through an activated carbon tower of an immobilized bed type under conditions at the SV of 20 hr.sup.1, and the water was made to pass through a softening tower under conditions at the SV of 15 hr.sup.1. After that, 10 mg/L (i.e., five-fold excess by weight per calcium ion concentration of treated water from a softening tower) of a chelator-based scale inhibitor (Welclean A801, manufactured by Kurita Water Industries, Ltd.) was added, and NaOH was added to set pH to 10.5. After that, the RO membrane separation treatment was carried out by using an RO membrane separation device (an ultralow-pressure aromatic polyamide-type RO membrane, ES-20, manufactured by NITTO DENKO CORPORATION) under conditions at the flow volume of 60 L/h and at the recovery rate of 80%. In addition, the pH of RO supply water was 9.5.

Comparative Example 2

(54) Treatment was carried out in the conditions identical to those of Example 2, except that to drainage containing a nonionic detergent and having the TOC concentration of 20 mg/L and the calcium concentration of 5 mg/L was added, as a free chlorine concentration, 1 mg-Cl.sub.2/L of NaClO instead of the above slime-controlling agent.

(55) <Evaluation of Effect of Inhibiting Proliferation of Viable Cells>

(56) For Example 2 and Comparative Example 2, the number of viable cells was investigated at the respective points. Table 1 showed the results.

(57) TABLE-US-00001 TABLE 1 Example 2 Comparative Example 2 Agent used Combined chlorine agent .sup.1) NaCIO Activated carbon ND ND supply water Activated carbon ND 2.1 10.sup.5 cells/mL treated water Softened treated ND l 10.sup.6 cells/mL water RO supply water ND ND RO concentrated ND ND water Note .sup.1) Combined chlorine agent: Combined chlorine agent produced from sodium hypochlorite and sodium sulfamate

(58) As clearly demonstrated in Table 1, in Example 2 in which a slime-controlling agent of a combined chlorine agent of the present invention had been used, no viable cells were observed at the all measurement points. In contrast, in Comparative Example 2, 210,000 cells/mL of viable cells were observed in the activated carbon treated water, and 1,000,000 cells/ml of viable cells were observed in the softening tower treated water.

(59) <Estimation of Effect of Inhibiting Increase in Pressure Difference of RO Membrane>

(60) In Example 2 and Comparative Example 2, a daily variation in a pressure difference between modules of the RO membrane separation device was investigated. Table 2 showed the results.

(61) TABLE-US-00002 TABLE 2 Pressure Difference between Modules (MPa) Comparative Flow Days Example 2 Example 2 1 0.02 0.02 7 0.02 0.025 30 0.02 0.03 60 0.02 0.14

(62) As clearly demonstrated in Table 2, in Example 2, no increase in the pressure difference between the modules of the RO membrane separation device was observed. In contrast, in Comparative Example 2, the pressure difference between the modules increased to 0.14 MPa after 60 days. Slime was detected in the occluded RO membrane.

(63) The present invention has been described in detail by using specific embodiments. However, it is obvious to those skilled in the art that various modifications can be achieved without departing the spirit and scope of the present invention.

(64) In addition, the present application claims the benefit of Japanese Patent Application 2009-046619 filed on Feb. 27, 2009, which is herein incorporated by reference in its entirety.