JP2000271577A - Treatment of surfactant-containing waste solution - Google Patents

Abstract

PROBLEM TO BE SOLVED: To easily treat a surfactant-containing waste soln. at ambient temp. under atmospheric pressure to obtain water capable of being discharged to environment. SOLUTION: Ozone gas 5 is added to a surfactant-containing waste soln. 1 to reduce the foamability of the waste soln. to enhance the filterability thereof and hydrogen gas 7 is added to this waste soln. to rapidly decompose a corrosive oxidizing substance such as ozone or the like remaining in the waste soln. Further, the removal of a suspended solid component by filtering, the enhancement of light permeability, the generation of steam from the waste soln. by heating and the removal of an org. component by activated carbon or ultraviolet rays can be achieved. By this constitution, water capable of being discharged to environment can be obtained by easy treatment matched with the properties of the surfactant-containing waste soln.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of treating a surfactant-containing waste liquid for treating a waste liquid containing a surfactant in, for example, washing wastewater.

[0002]

2. Description of the Related Art Waste liquids containing a surfactant include, for example, equipment drain water, floor drain water, shower drain water from shower water, and washing waste water generated by washing clothes.
Conventionally, as a method for treating these waste liquids, for example, when treating a waste liquid containing a surfactant generated from a nuclear power plant, a thermal power generation facility, a sewage treatment facility, or the like, an evaporative concentration method, an activated carbon adsorption method, an ultraviolet ray decomposition method, etc. are known. Have been.

[0003]

However, the surfactant-containing waste liquid has a high foaming property, is hardly soluble, has a large amount of organic components, and has a high suspended solid (SS) content. The evaporative concentration method cannot treat waste liquid with high foaming properties, the activated carbon itself becomes secondary waste in the activated carbon adsorption method, and the ultraviolet light decomposition method does not provide sufficient treatment effects when the light transmittance to industrial water or wastewater is low. There are issues such as.

[0004] The present invention has been made to solve these problems, and an object of the present invention is to provide a treatment method capable of easily treating a surfactant-containing waste liquid at normal temperature and pressure to obtain water quality that can be discharged to the environment. Aim.

[0005]

According to a first aspect of the present invention, an ozone gas is first added to a waste liquid containing a surfactant,
Next, after adding hydrogen gas to decompose corrosive oxides,
It is characterized by release to the environment. In the invention of claim 1,
First, when ozone gas is added to the surfactant-containing waste liquid,
Ozone reacts with the surfactant to cause reactions such as 1) oxidizing a hydrophobic group to an organic acid, 2) breaking a bond between a hydrophilic group and a hydrophobic group, and 3) oxidatively decomposing a hydrophilic group, As a result, the foaming property (or surfactant activity) of the surfactant is reduced, and the filtration property is improved.

Next, oxidizing agents such as ozone and hydrogen peroxide remaining in the waste liquid are rapidly decomposed by adding hydrogen gas. Here, as the ozone gas and the hydrogen gas, those generated by an electrolytic device can be used.

[0007] The invention of claim 2 is characterized in that the waste liquid to which the hydrogen gas has been added is subjected to a filtration treatment. According to the second aspect of the present invention, in the first aspect of the present invention, the insoluble components in the waste liquid can be removed by filtering the waste liquid to which hydrogen gas has been added subsequently to the ozone gas. Further, if the neutralization treatment is performed before the filtration treatment, the metal hydroxide in the liquid can be removed at the same time.

A third aspect of the present invention is characterized in that the waste liquid to which the hydrogen gas has been added is heated and evaporated. Claim 3
According to the invention of the first aspect, the waste liquid to which the hydrogen gas has been added subsequently to the ozone gas is heated and evaporated to remove the moisture in the waste liquid. Further, distilled water can be obtained by condensing the evaporated water, and reusable water can be obtained by treating the distilled water with activated carbon or an ion exchange resin.

The invention according to claim 4 is characterized in that the waste liquid to which the hydrogen gas is added is treated with activated carbon. According to the invention of claim 4, the organic component in the waste liquid can be removed.
The invention according to claim 5 is characterized in that the waste liquid to which the hydrogen gas has been added is subjected to a filtration treatment after a neutralization treatment. According to the fifth aspect of the invention, the remaining metal hydroxide and organic components can be completely removed.

The invention according to claim 6 is characterized in that the waste liquid to which the hydrogen gas has been added is subjected to a powdered activated carbon treatment and then a filtration treatment. According to the invention of claim 6, in the invention of claim 1, an organic component in the waste liquid can be removed by subjecting the waste liquid to which hydrogen gas has been added subsequently to the ozone gas to activated carbon treatment.

The invention according to claim 7 is characterized in that the filtered waste liquid is irradiated with ultraviolet rays. According to the seventh aspect of the present invention, in the first aspect of the present invention, the organic component in the waste liquid is removed by irradiating the waste liquid to which the hydrogen gas is added subsequently to the ozone gas with ultraviolet rays. Here, a low-pressure mercury lamp (internal pressure <1 mmHg) can be used as the ultraviolet light source.

The invention according to claim 8 is characterized in that the evaporated water is subjected to a condensation treatment. According to the eighth aspect of the present invention, the water that has been converted into steam by heating and evaporation can be converted into distilled water by the condenser. The amount of distilled water increases with an increase in the amount of electric power to be heated, so that distilled water can be quickly recovered, and water can be reused.

A ninth aspect of the present invention is characterized in that the ozone gas and the hydrogen gas are gases generated by a method of supplying pure water in a water electrolysis cell and performing electrolysis. According to the ninth aspect of the present invention, a high-concentration ozone aqueous solution containing approximately 20% ozone can be obtained using ion-exchanged water as a raw material at a voltage of several volts, so that the surfactant can be efficiently oxidized. . In addition, by-products (N
O _x, etc.) it is not. As for the hydrogen gas, the surplus generated at the same time as the generation of ozone by electrolysis can be effectively used.

A tenth aspect of the present invention is characterized in that iron is added simultaneously with the ozone gas. According to the invention of claim 10, foaming generated due to the reaction between the ozone gas and the surfactant can be reduced, and the filterability is improved. When iron is added simultaneously with ozone, the foaming effect is better than when iron is not present. If ozone is not added, there is almost no effect in reducing foaming.

An eleventh aspect of the present invention is characterized in that a hollow fiber membrane is used as the filter. According to the invention of claim 11, by using a hollow fiber membrane as a filter material, a very large number of threads serve as a membrane, so that a processing area is increased,
The device scale can be reduced. In addition, even fine particles can be removed (up to 0.1 μm), which facilitates backwashing after collecting insoluble components.

A twelfth aspect of the present invention is characterized in that a low-pressure mercury lamp (internal pressure <1 mmHg) is used as the ultraviolet light source. According to the invention of claim 12, it is possible to decompose an organic substance (TOC) such as a surfactant. There are high and low pressure mercury lamps, and low pressure mercury lamps are superior.

The invention of claim 13 is characterized in that ozone gas is added simultaneously with the irradiation of the ultraviolet rays. According to the invention of claim 13, when ozone gas is added simultaneously with ultraviolet light, a more excellent decomposition effect can be obtained than when no ozone gas is added (see FIG. 18).

The invention of claim 14 is characterized in that the condensed distilled water is treated with activated carbon. According to the invention of claim 14, the organic component (TOC) can be removed at the same time as the insoluble component by subjecting the condensed distilled water to the activated carbon treatment.

The invention of claim 15 is characterized in that the condensed distilled water is treated with an ion exchange resin. Claim
According to the fifteenth aspect, the conductivity and the organic component (TOC) are obtained by subjecting the condensed distilled water to an ion exchange resin treatment.
The concentration can be at the pure water level.

[0020]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS A first embodiment of a processing method according to the present invention will be described with reference to FIGS.

In the first embodiment, as shown in the process diagram of FIG.
And the ozone gas 5 is blown therein to oxidize the surfactant, thereby reducing the foaming property (or surface activity) of the surfactant and, at the same time, obtaining an oxidized waste liquid 2 having improved filterability. Next, the oxidized waste liquid 2 is placed in a hydrogen reduction tank 6, and hydrogen gas 7 is blown therein to decompose an oxidizing agent such as ozone or hydrogen peroxide to form a reduced waste liquid 3.

FIG. 2 and FIG. 3 show that in the first embodiment, the surfactant-containing waste liquid 1 is put into an ozone reaction tank 4,
FIG. 4 is a plot diagram showing the results of measuring the change over time in the foaming property and filterability of the surfactant-containing waste liquid 1 when ozone gas 5 is blown.

Here, the concentration of the surfactant was 800 ppm, the work clothes were washed, the amount of waste liquid left after being left for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the initial solution pH was 6 to 6 L.
7. The solution temperature was 15-20 ° C. The foamability is 5
By heating a cylindrical tall beaker of cm, filterability increases the pore size.
The filtration area was set to 0.45 μm, and the filtration area was set to 9.6 cm ² . 2 and 3 that the first embodiment can reduce the foaming property in the surfactant-containing waste liquid 1 and improve the filterability.

FIG. 4 is a plot showing the results of measuring the change over time in the concentration of dissolved ozone when the dissolved ozone is introduced into the hydrogen reduction tank 6 and the hydrogen gas 7 is blown in the first embodiment. Here, the surfactant concentration was 800 ppm, the work clothes were washed, and the amount of waste liquid left for 3 days was 1.5 L, the amount of hydrogen gas blown was 5 L / min, and the initial solution pH was 6 to 5 L / min.
7. The solution temperature was 15-20 ° C. FIG. 4 shows that the oxidizing agent such as ozone in the surfactant-containing waste liquid 1 can be decomposed by the first embodiment.

Table 1 is a table comparing the generation method of the ozone gas 5 between the discharge method and the electrolysis method in the first embodiment. In Table 1, there are two types of discharge systems that use silent discharge tubes and ceramic plates as generators.
As is clear from FIG. 7, generation of ozone gas by the electrolysis-type electrolysis apparatus is superior to that of the discharge-type electrolysis apparatus.

[0026]

[Table 1]

FIG. 5 and FIG. 6 show the surfactant when the ozone gas 5 was blown after the surfactant-containing waste liquid 1 was accommodated in the ozone reaction tank 4 and iron was added thereto in the first embodiment. The results of measuring the changes over time of the foaming property and the filterability of the waste liquid 1 are shown in plots.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid after washing the work clothes and left for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm.
-Fe ³⁺ , initial solution pH 6-7, solution temperature 15-20 ° C
And 5 and 6 that the addition of iron can promote the reduction of the foaming property and the improvement of the filterability of the surfactant-containing waste liquid 1.

Next, a second embodiment according to the present invention will be described with reference to FIGS. FIG. 7 is a process diagram for explaining the second embodiment of the present invention, and the same parts as those in FIG. 1 are denoted by the same reference numerals. In the second embodiment, FIG.
As shown in FIG.
And the ozone gas 5 is blown therein to oxidize the surfactant to obtain an oxidized waste liquid 2 having improved surfactant filterability.

Next, this oxidized waste liquid 2
Into a hydrogen reduction tank 6, and blowing hydrogen gas 7 to decompose an oxidizing agent such as ozone or hydrogen peroxide to obtain a waste liquid 3 for reduction treatment. Next, the reduced liquid waste 3 subjected to the reduction treatment is put into a filter 9 and filtered to obtain a filtered liquid 8 from which insoluble components have been removed.

Table 2 shows that, in the second embodiment, the surfactant-containing waste liquid 1 obtained by putting the surfactant-containing waste liquid 1 into the ozone reaction tank 4, blowing the ozone gas 5, and filtering it with the filter 9. 3 shows the results of measuring the filterability and the insoluble component removing property of the sample.

[0032]

[Table 2]

Here, the concentration of the surfactant was 800 ppm, the work clothes were washed, and the amount of waste liquid left after standing for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm.
-Fe ³⁺ , ozone treatment time 60 min, initial solution pH 6
~ 7, solution temperature was 15-20 ° C. The filterability was determined by suction filtration with a pore size of 0.45 μm and a filtration area of 9.6 cm ² . From Table 2, it is understood that the insoluble components of the surfactant-containing waste liquid 1 can be removed according to the second embodiment.

FIG. 8 shows that, in the second embodiment, the surfactant-containing waste liquid 1 is put into the ozone reaction tank 4, and the ozone gas 5 is blown into the ozone reaction tank 4. It is a waveform diagram which shows the result of having measured the differential pressure | voltage rise property of the hollow fiber membrane at the time of.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid after washing the work clothes and left for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm.
-Fe ³⁺ , ozone treatment time 60 min, initial solution pH 6
~ 7, solution temperature was 15-20 ° C. The differential pressure increasing property of the hollow fiber membrane is such that the linear velocity is 0.1 m / hr and the filtration area is 0.1 m ^2.
I investigated. FIG. 8 shows that a hollow fiber membrane can be used as the filter medium.

Table 3 shows that, in the second embodiment, the surfactant-containing waste liquid 1 was placed in the ozone reactor 4 and the ozone gas 5 was discharged.
And the results obtained by measuring the insoluble components of the surfactant-containing waste liquid 1 when the mixture was neutralized by adding an acid and an alkali and filtered by the filter 9.

[0037]

[Table 3]

Here, the concentration of the surfactant was 800 ppm, the work clothes were washed, the amount of waste liquid left after standing for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the ozone treatment time was 60 hours.
min, the initial solution pH was 6-7, and the solution temperature was 15-20 ° C. For neutralization, 0.1 N-H ₂ SO ₄ was used as an acid and 0.1 N-NaOH was used as an alkali. Filtration was performed by suction filtration with a filter medium pore size of 0.45 μm and a filtration area of 9.6 cm ² . From Table 3, it can be seen that the dissolved metal component can be removed as a metal hydroxide as an insoluble component by the neutralization treatment.

Table 4 shows that in the second embodiment, the surfactant-containing waste liquid 1 was charged into the ozone reactor 4 and the ozone gas 5 was discharged.
The results obtained by measuring the filterability of the surfactant-containing waste liquid 1 and the removability of insoluble components and organic components (TOC) when filtration was performed by the filter 9 after blowing activated carbon powder were added.

[0040]

[Table 4]

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid left after leaving the work clothes for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm-F.
e ³⁺ , ozone treatment time 60min, initial solution pH 6 ~
7. The solution temperature was 15-20 ° C. The activated carbon treatment was performed by suction filtration with the powdered activated carbon addition amount set to 1000 ppm and the treatment time set to 60 min. The filtration treatment was performed with a filter material pore diameter of 0.45 μm and a filtration area of 9.6 cm ² . From Table 4, it can be seen that the organic component can be removed simultaneously with the insoluble component by the powdered activated carbon treatment.

Next, a third embodiment of the present invention will be described with reference to FIGS. In the third embodiment, as shown in FIG. 9, a surfactant-containing waste liquid 1 is put into an ozone reaction tank 4, and an ozone gas 5 is blown to reduce the foaming property of the surfactant to obtain an oxidation treatment waste liquid 2. Next, the oxidized waste liquid 2 is placed in a hydrogen reduction tank 6, and hydrogen gas 7 is blown therein to decompose an oxidizing agent such as ozone or hydrogen peroxide to form a reduced waste liquid 3. Next, the reduced waste liquid 3 subjected to the reduction treatment is put into a heater 11 and heated and evaporated to thereby form steam 10
And

FIG. 10 shows a surfactant-containing waste liquid when the surfactant-containing waste liquid 1 is put into an ozone reaction tank 4 and ozone gas 5 is blown and then heated and evaporated by a heater 11 in the third embodiment. FIG. 4 is a characteristic diagram showing the result of measuring the foamability of Sample No. 1.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid in which the work clothes were left for 3 days was 12 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, the amount of iron added was 100 ppm-Fe ³⁺ ,
The ozone treatment time was 140 min, the initial solution pH was 6-7, and the solution temperature was 15-20 ° C. In the heating and evaporating treatment, the evaporating area was 19.6 cm ² , the inner diameter of the foaming portion was 5 cm, the amount of the heating liquid was 6.8 L, and the amount of electricity in the heating portion was ３3 kW. From FIG. 10, it can be seen that according to the third embodiment, the surfactant-containing waste liquid 1 can be heated and evaporated.

FIG. 11 shows that in the third embodiment, the surfactant-containing waste liquid 1 is put into the ozone reaction layer 4, the ozone gas 5 is blown in, and the mixture is heated and evaporated by the heater 11 to form steam 10, FIG. 6 is a plot diagram showing a result of measuring a relationship between an electric energy of a heater 11 and an amount of distilled water when 10 is distilled water by a condenser.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid in which the work clothes were left for 3 days was 12 L, the amount of ozone generated by water electrolysis production was 0.6 g / h, the amount of iron added was 100 ppm-Fe ³⁺ ,
The ozone treatment time was 140 min, the initial solution pH was 6-7, and the solution temperature was 15-20 ° C. In the heating and evaporating treatment, the evaporating area was 19.6 cm ² , the inner diameter of the foaming portion was 5 cm, the amount of the heating liquid was 6.8 L, and the amount of electricity in the heating portion was ３3 kW. From FIG. 11, it can be seen that water converted into steam by heating and evaporation can be converted into distilled water by the condenser.

FIG. 12 shows that in the third embodiment, the surfactant-containing waste liquid 1 is put into the ozone reaction layer 4, the ozone gas 5 is blown in, the water vapor is heated and evaporated by the heater 11, and the water vapor 10 is distilled by the condenser. FIG. 4 is a plot showing the results of measuring the TOC concentration when activated carbon was added to this distilled water after water conversion.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid in which the work clothes were left for 3 days was 12 L, the amount of ozone generated by water electrolysis production was 0.6 g / h, the amount of iron added was 100 ppm-Fe ³⁺ ,
The ozone treatment time was 140 min, the initial solution pH was 6-7, and the solution temperature was 15-20 ° C.

The heating and evaporating treatment reduces the evaporation area to 19.6 c.
m ² , the inner diameter of the foaming section was 5 cm, the amount of the heating liquid was 6.8 L, and the amount of electricity in the heating section was ３3 kW. Activated carbon treatment uses 200 ml of distilled water,
Granular activated carbon was added with the amount of activated carbon added as 1 g. From FIG. 12, the organic component (T) was obtained by treating distilled water with activated carbon.
It can be seen that the OC) concentration can be set to the level of pure water.

FIG. 13 shows a third embodiment in which a surfactant-containing waste liquid 1 is put into an ozone reaction tank 4, ozone gas 5 is blown in, and heated and evaporated by a heater 11 into steam 10, and distilled by a condenser. FIG. 9 is a plot diagram showing the results of measuring the conductivity and the TOC concentration when an ion-exchange resin is added to distilled water after water conversion.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid in which the work clothes were left for 3 days was 12 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, the amount of iron added was 100 ppm-Fe ³⁺ ,
The ozone treatment time was 140 min, the initial solution pH was 6-7, and the solution temperature was 15-20 ° C. In the heating and evaporating treatment, the evaporating area was 19.6 cm ² , the inner diameter of the foaming portion was 5 cm, the amount of the heating liquid was 6.8 L, and the amount of electricity in the heating portion was ３3 kW.

In the ion exchange resin treatment, the amount of distilled water was 200 ml,
Strongly acidic and strongly alkaline resins were added with the ion exchange resin added at 2 ml for cations and 4 ml for anions. This figure
From FIG. 13, it is understood that the conductivity and the organic component (TOC) concentration can be brought to the level of pure water by treating the distilled water with the ion exchange resin.

Next, a fourth embodiment of the present invention will be described with reference to FIGS. In the fourth embodiment, as shown in FIG. 14, a surfactant-containing waste liquid 1 is placed in an ozone reaction tank 4 and an ozone gas 5 is blown into an oxidation treatment waste liquid 2 having improved surfactant filterability. . Next, the oxidized waste liquid 2 subjected to the oxidation treatment is put into a hydrogen reduction tank 6 and hydrogen gas 7
Is blown to decompose an oxidizing agent such as ozone or hydrogen peroxide to produce a reduction treatment waste liquid 3. Next, the reduced waste liquid 3 subjected to the reduction treatment is put into an activated carbon reaction tank 13, and an activated carbon 14 is added to form an activated carbon treated liquid 12 from which organic components have been removed.

FIG. 15 shows that, in the fourth embodiment, the surfactant-containing waste liquid 1 is put into the ozone reactor 4 and the ozone gas 5
FIG. 6 is a plot diagram showing the results of measuring the TOC concentration when activated carbon 14 was added into activated carbon reaction tank 12 after blowing.

Here, the concentration of the surfactant was 800 ppm, the amount of the waste liquid left after leaving the work clothes for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm-F.
e ³⁺ , ozone treatment time 60min, initial solution pH 6 ~
7. The solution temperature was 15-20 ° C. In the activated carbon treatment, granular activated carbon was added at an activated carbon addition amount of 10 g / L. From FIG. 15, it can be seen that according to the fourth embodiment, the organic component (TOC) of the surfactant-containing waste liquid 1 can be removed.

Next, a fifth embodiment of the present invention will be described with reference to FIGS. In the fifth embodiment, as shown in FIG. 16, a surfactant-containing waste liquid 1 is put into an ozone reaction tank 4 and an ozone gas 5 is blown into an oxidation treatment waste liquid 2 having improved surfactant filterability. . Next, the oxidized waste liquid 2 subjected to the oxidation treatment is put into a hydrogen reduction tank 6 and hydrogen gas 7
Is blown to decompose an oxidizing agent such as ozone or hydrogen peroxide to produce a reduction treatment waste liquid 3.

Next, the reduced waste liquid 3 subjected to the reduction treatment is placed in a filter 9 and filtered to obtain a filtered liquid 8 from which insoluble components have been removed. Further, the filtered liquid 8 is placed in an ultraviolet ray tank 16 and irradiated with ultraviolet rays from an ultraviolet ray lamp 17 to decompose organic components to obtain an ultraviolet ray treated liquid 15.

FIG. 17 shows that, in the fifth embodiment, the surfactant-containing waste liquid 1 is put into the ozone reaction tank 4 and the ozone gas 5
FIG. 5 is a plot showing the results of measuring the TOC concentration when the filtered liquid 8 was put into an ultraviolet ray tank 16 and irradiated with ultraviolet rays by an ultraviolet ray lamp 17 after blowing through the filter 9 and filtering.

Here, the surfactant concentration was 800 ppm, the amount of waste liquid left after leaving work clothes for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm-F.
e ³⁺ , ozone treatment time 60min, initial solution pH 5 ~
6. The solution temperature was 20-25 ° C.

The filtration treatment was carried out by suction filtration with a pore size of 0.45 μm and a filtration area of 9.6 cm ² , and the ultraviolet irradiation was performed using a 32 W low-pressure mercury lamp (internal pressure <1 mmHg) as an ultraviolet light source. From FIG. 17, it can be seen that according to the fifth embodiment, the organic component (TOC) of the surfactant-containing waste liquid 1 can be removed.

FIG. 18 shows that in the fifth embodiment, the surfactant-containing waste liquid 1 is put into the ozone reaction tank 4 and the ozone gas 5
FIG. 6 is a plot showing the result of measuring the TOC concentration when ozone gas was added at the same time that the filtered liquid 8 was put into an ultraviolet ray tank 16 and irradiated with ultraviolet rays by an ultraviolet ray lamp 17 after filtering with a filter 9.

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid left after leaving the work clothes for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm-F.
e3 ⁺ , the initial solution pH was 5-6, and the solution temperature was 20-25C.

The filtration was carried out by suction filtration with a pore size of 0.45 μm and a filtration area of 9.6 cm ² , and the ultraviolet irradiation was carried out with a low-pressure mercury lamp of 32 W low pressure (internal pressure <1 mmHg) and an ozone gas addition amount of 0.6 g / L. . As is clear from FIG. 18, by adding the ozone gas simultaneously with the ultraviolet irradiation,
It is recognized that the organic component (TOC) can be removed more efficiently.

FIG. 19 shows that, in the fifth embodiment, the surfactant-containing waste liquid 1 is put into the ozone reaction tank 4, the ozone gas 5 is blown therein, and the ozone gas 5 is filtered by the filter 9. FIG. 4 is a plot diagram comparing the results of measuring the TOC concentration when irradiating a high-pressure mercury lamp and a low-pressure mercury lamp (internal pressure <1 mmHg).

Here, the concentration of the surfactant was 800 ppm, the amount of waste liquid left after leaving the work clothes for 3 days was 1.5 L, the amount of ozone generated in water electrolysis production was 0.6 g / h, and the amount of iron added was 100 ppm-F.
e3 ⁺ , the initial solution pH was 5-6, and the solution temperature was 20-25C.

The filtration was carried out by suction filtration with a pore size of 0.45 μm and a filtration area of 9.6 cm ² , and the ultraviolet irradiation was performed by using an ultraviolet light source of 100 W high-pressure mercury lamp (internal pressure of 1 to several atm) / 32 W low-pressure mercury lamp (internal pressure < 1mmHg), the amount of added ozone gas is 0.6
g / L. From FIG. 19, it can be seen that the low-pressure mercury lamp (internal pressure <
1 mmHg).

[0067]

According to the present invention, first, ozone gas is added to a surfactant-containing waste liquid to oxidatively decompose a hydrophobic group with respect to the surfactant and to cleave the hydrophilic group and the hydrophobic group. It oxidatively decomposes hydrophilic groups to reduce foaming properties and improve filterability. Second, by adding hydrogen gas, corrosive oxides such as ozone remaining in the waste liquid are quickly decomposed. Third, treatment methods such as filtration, heat evaporation, activated carbon adsorption, and UV decomposition can be arbitrarily applied.

Therefore, suspended solids (SS) by filtration
Removal of components, improvement of light transmittance, vaporization of waste liquid by heating, and removal of organic components by activated carbon and ultraviolet rays. Therefore, it is possible to obtain water quality that can be released to the environment by easy treatment according to the properties of the surfactant-containing waste liquid.

[Brief description of the drawings]

FIG. 1 is a schematic process diagram for explaining a first embodiment according to the present invention.

FIG. 2 is a plot diagram showing a change with time in effervescence in water in the first embodiment.

FIG. 3 is a plot diagram showing a change over time in filterability in water in the first embodiment.

FIG. 4 is a plot diagram showing a change over time of a dissolved ozone concentration in water in the first embodiment.

FIG. 5 is a plot diagram showing a change over time in foamability in water when iron is added in the first embodiment.

FIG. 6 is a plot diagram showing a change with time in filterability in water when iron is added in the first embodiment.

FIG. 7 is a schematic process diagram for explaining a second embodiment according to the present invention.

FIG. 8 is a waveform diagram showing a differential pressure increasing property when performing hollow fiber membrane filtration in the second embodiment.

FIG. 9 is a schematic process diagram for explaining a third embodiment according to the present invention.

FIG. 10 is a characteristic diagram showing foamability when heated and evaporated in the third embodiment.

FIG. 11 is a plot diagram showing a relationship between a power amount of a heater and a distilled water amount in a third embodiment.

FIG. 12 is a plot diagram showing a change over time in the TOC concentration when activated carbon is added to distilled water in the third embodiment.

FIG. 13 is a plot diagram showing changes over time in the electrical conductivity and the TOC concentration when an ion exchange resin is added to distilled water in the third embodiment.

FIG. 14 is a schematic process diagram for explaining a fourth embodiment according to the present invention.

FIG. 15 is a plot diagram showing the change over time in the TOC concentration in water in the fourth embodiment.

FIG. 16 is a schematic process diagram for explaining a fifth embodiment according to the present invention.

FIG. 17 is a plot diagram showing the change over time in the TOC concentration in water in the fifth embodiment.

FIG. 18 is a plot diagram showing a change over time in the TOC concentration in water when ozone gas is added in the fifth embodiment.

FIG. 19 is a plot diagram showing the change over time of the TOC concentration in water by a high-pressure and low-pressure mercury lamp (internal pressure <1 mmHg) in the fifth embodiment.

[Explanation of symbols]

DESCRIPTION OF SYMBOLS 1 ... Waste liquid containing surfactant, 2 ... Oxidation waste liquid, 3 ... Reduction treatment waste liquid, 4 ... Ozone reaction tank, 5 ... Ozone gas, 6 ... Hydrogen reduction tank, 7 ... Hydrogen gas, 8 ... Filtration treatment liquid, 9 ... Filtration Vessel, 10… steam, 11… heater, 12… activated carbon treatment liquid, 13…
Activated carbon reaction tank, 14 ... Activated carbon, 15 ... UV treatment liquid, 16 ... UV tank, 17 ... UV lamp.

──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat ゛ (Reference) C02F 1/70 C02F 1/70 Z G21F 9/06 551 G21F 9/06 551Z (72) Inventor Hideji Seki Kanagawa 1 Toshiba Research and Development Center, Komukai Toshiba-cho, Kawasaki-shi, Kawasaki-shi (72) Inventor Koichi Hiruta 8 Shinsugita-cho, Isogo-ku, Yokohama-shi, Kanagawa Prefecture In-house Toshiba Yokohama Office (72) Inventor Takao Takada 8F Shin-Sugita-cho, Isogo-ku, Yokohama-shi, Kanagawa Prefecture F-term in the Toshiba Yokohama office (reference) 4D006 GA07 KB04 KB11 KB12 KB14 KB18 KB30 MA01 MB02 PB08 PB70 4D024 AA04 AB04 BA02 DB05 DB06 DB10 DB19 DB22 DB24 4D034 AA26 CA12 4D037A BA18 BB06 CA01 CA03 CA09 CA12 CA14 CA15 4D050 AA12 AA15 AB02 BA14 BB02 BC07 BD02 BD04 BD06 CA01 CA02 CA06 CA07 CA08 CA 09 CA13 CA15 CA20

Claims (15)

[Claims] 1. A surfactant-containing waste liquid characterized in that an ozone gas is first added to a waste liquid containing a surfactant, and then a hydrogen gas is added to decompose corrosive oxides and then release it to the environment. Waste liquid treatment method. 2. The method for treating a surfactant-containing waste liquid according to claim 1, wherein the waste liquid to which the hydrogen gas is added is subjected to a filtration treatment. 3. The method for treating a surfactant-containing waste liquid according to claim 1, wherein the waste liquid to which the hydrogen gas has been added is heated and evaporated. 4. The method for treating a surfactant-containing waste liquid according to claim 1, wherein the waste liquid to which the hydrogen gas has been added is treated with activated carbon. 5. The method for treating a surfactant-containing waste liquid according to claim 2, wherein the waste liquid to which the hydrogen gas is added is subjected to a neutralization treatment and then a filtration treatment. 6. The method for treating a surfactant-containing waste liquid according to claim 2, wherein the waste liquid to which the hydrogen gas is added is subjected to a powdered activated carbon treatment and then a filtration treatment. 7. The method for treating a surfactant-containing waste liquid according to claim 2, wherein the filtered waste liquid is irradiated with ultraviolet rays. 8. The method for treating a surfactant-containing waste liquid according to claim 3, wherein the evaporated water is subjected to a condensation treatment. 9. The treatment of a surfactant-containing waste liquid according to claim 1, wherein the ozone gas and the hydrogen gas comprise gas generated by a method of supplying pure water in a water electrolysis cell and performing electrolysis. Method. 10. The method for treating a surfactant-containing waste liquid according to claim 1, wherein iron is added simultaneously with the ozone gas. 11. The method for treating a surfactant-containing waste liquid according to claim 2, wherein a hollow fiber membrane is used as the filter medium. 12. The method for treating a surfactant-containing waste liquid according to claim 7, wherein a low-pressure mercury lamp (internal pressure <1 mmHg) is used as the ultraviolet light source. 13. The method for treating a surfactant-containing waste liquid according to claim 7, wherein the ozone gas is added simultaneously with the irradiation of the ultraviolet rays. 14. The method for treating a surfactant-containing waste liquid according to claim 8, wherein the condensed distilled water is treated with activated carbon. 15. The method for treating a surfactant-containing waste liquid according to claim 8, wherein the condensed distilled water is treated with an ion exchange resin.