JP5894420B2 - Polymer wax stripping waste liquid processing apparatus and processing method - Google Patents

Description

  The present invention relates to a processing apparatus and a processing method for a polymer wax peeling waste liquid.

In many cases, a polymer wax is applied to a floor surface of a building as a flooring agent for the purpose of protection or aesthetics.
The applied polymer wax as a flooring agent is worn by dust adhesion, mechanical abrasion, abrasion, and the like, and its function and aesthetics are deteriorated. Therefore, it is usually repainted regularly. In this repainting, it is necessary to first peel off the already applied polymer wax, and a large amount of polymer wax peeling waste liquid is generated by the above-described periodic repainting.

  As a treatment method of this polymer wax stripping waste liquid, the polymer and the stripping solution component contained in the waste liquid are also effectively used as fuel, aiming at the total abolition of industrial waste, and at the same time harmful substances that adversely affect the environment in the processing There has been proposed a method for treating a polymer wax peeling waste liquid in which the generation of the above is suppressed (see, for example, Patent Document 1 and Patent Document 2).

JP 2008-207128 A JP 2010-194493 A

In the above-described method for treating the polymer wax peeling waste liquid, the flaking agent is added to the peeling waste liquid to separate the peeling waste liquid into a polymer lump and primary treated water. The polymer mass becomes a material used for solid fuel and the like as it is. The primary treated water contains a water-soluble agent such as a surfactant or a solvent contained in the release agent that has not been separated. For this reason, solid content is further extracted from primary treated water.
The extraction of the solid content from the primary treated water is performed by separating water from the primary treated water by distillation. That is, the chemical | medical agent etc. are taken out from primary treated water by heat-drying primary treated water.

  However, by drying the primary treated water by heating, other substances are exhausted simultaneously with the separated water. For this reason, substances other than water are discharged into the waste steam generated when the primary treated water is heated. When this waste steam is discharged to the outside from the discharge port of the processing facility, the odor due to the substance such as the drug contained becomes a problem. Odor is regulated by the Odor Control Law, and regulation standards are set for the odor index of the exhaust, the height of the gas outlet, and the like.

  In order to solve the above-mentioned problems, in the present invention, there is provided a processing apparatus and a processing method for a polymer wax peeling waste liquid, which can reduce the odor index of exhaust gas so as to be compatible with the odor index regulations of the Odor Control Law. It is to provide.

  The apparatus for treating a polymer wax stripping waste liquid according to the present invention includes a coagulation stirring tank for mixing the polymer wax stripping waste liquid and a flocculant, and a filtration tank for separating the waste liquid in the coagulation stirring tank into a polymer mass and primary treated water. And an evaporating tank for heating the primary treated water, and a blower provided at the gas outlet of the evaporating tank.

  In addition, the method for treating the polymer wax peeling waste liquid according to the present invention includes a coagulation treatment step in which a flocculant is added to the polymer wax peeling waste liquid to precipitate a polymer mass, and the polymer mass is extracted. It has a separation step for separating into treated water and an evaporation step for heating the primary treated water. The waste steam generated in the evaporation step is diluted and exhausted.

  ADVANTAGE OF THE INVENTION According to this invention, the processing apparatus and the processing method of the polymer wax peeling waste liquid which can reduce the odor index | exponent of exhaust_gas | exhaustion can be provided by diluting the waste steam of primary treated water.

It is a flowchart of the processing method of the peeling waste liquid of the polymer wax of this invention. It is a block diagram of the processing apparatus of the polymer wax peeling waste liquid of this invention. It is a graph which shows the relationship between the air volume of the odor experiment example 1, and an odor index | exponent. It is a graph which shows the relationship between the air volume of odor experiment example 1, and an odor density | concentration. It is a graph which shows the relationship between the air volume index conversion value of the odor experimental example 1, and the odor index. It is a graph which shows the relationship between the dilution rate of Odor Experimental Example 1, and an odor index. It is a graph which shows the relationship between the air volume of the odor experiment example 2, and an odor index. It is a graph which shows the relationship between the air volume of odor experiment example 2, and an odor density | concentration. It is a graph which shows the relationship between the air volume index conversion value of the odor experiment example 2, and the odor index. It is a graph which shows the relationship between the dilution rate of the odor experiment example 2, and an odor index | exponent. It is a graph which shows the relationship between the air volume of the odor experiment example 3, and an odor index. It is a graph which shows the relationship between the air volume of the odor experiment example 3, and an odor density | concentration. It is a graph which shows the relationship between the air volume index conversion value of the odor experiment example 3, and the odor index. It is a graph which shows the relationship between the dilution factor of the odor experiment example 3, and an odor index | exponent.

Hereinafter, specific embodiments of the treatment method and treatment apparatus for the stripping waste liquid of the present invention will be described.
First, a method for treating a polymer wax peeling waste liquid according to the present invention will be described. The method for treating the stripping waste liquid of the present invention comprises an aggregating treatment step, a separation step, a neutralization step, an evaporation step, a dilution step, and a drying step. Hereinafter, the steps of the waste liquid treatment method will be described. FIG. 1 shows a process flow of a method for treating a polymer wax peeling waste liquid according to the present invention.

First, the polymer wax applied to the floor surface is peeled off with a release agent such as amines. The removal work of the polymer wax applied to the floor surface is, for example, a process in which dust is removed from the surface of the wax applied to the floor surface by a vacuum cleaner or the like and a release agent for removing the wax is applied. is there. As the release agent, for example, a composition containing amines, alcohols, ethers and water is used. Then, after the release agent is applied, a release operation is performed, and for example, a release waste liquid containing the polymer wax released by the release agent using a squeegee and a vacuum is collected.
As described above, when the polymer wax is peeled off, a polymer wax peeling waste liquid containing the polymer wax and the release agent is generated. This stripping waste liquid exhibits strong alkalinity, for example, about pH 11 to pH 12.5.

[Aggregation process]
Next, an agglomeration process is performed on the above-described peeling waste liquid by mixing an aggregating agent. As the flocculant, for example, inorganic acids such as sulfuric acid, hydrochloric acid and nitric acid, organic acids such as acetic acid, malic acid and succinic acid, and other known flocculants used for the flocculation treatment of polymer wax are used. When an acid is used for this aggregation treatment step, the stripping waste liquid becomes acidic. By mixing the flocculant with the peeling waste liquid, a wax component, that is, a semi-solid polymer mass is deposited on the upper layer of the peeling waste liquid.

  For example, at least one acid (Bronsted acid) selected from inorganic acids such as sulfuric acid, hydrochloric acid, and nitric acid and organic acids such as acetic acid, malic acid, and succinic acid is mixed with the stripping waste liquid. By mixing the acid, a gel-like semi-solid polymer mass is instantly deposited on the upper layer of the peeling waste liquid. Thus, the amine contained in the release agent reacts with the acid to generate a polymer mass as a salt.

[Separation process]
The precipitated polymer mass is extracted, and the separation waste liquid is separated into the polymer mass and the primary treated water. Alternatively, the extracted polymer mass may be washed with water, and the water used for washing may be added again to the primary treated water.

Next, the polymer mass is separated and extracted from the stripping waste liquid. And by this polymer lump extraction, the stripping waste liquid is separated into a polymer lump comprising a polymer wax and a release agent and the primary treated water after the polymer lump is removed from the stripping waste liquid.
The separation treatment is performed, for example, by passing the stripping waste liquid in a state where a polymer mass is deposited through a filtration device. Furthermore, the water contained in the polymer mass is separated from the separated polymer mass using a method such as pressing or centrifugation. And the water | moisture content isolate | separated from the polymer lump is mixed with the above-mentioned primary treated water.

[Neutralization process]
When an acid is used as the flocculant, the primary treated water exhibits an acidity with a pH of about 2 to 6.1, for example. For this reason, primary treatment water is neutralized by mixing alkali with primary treatment water. In the step of separating and extracting the polymer mass, it is necessary to add excess acid to the primary treated water, so that the primary treated water becomes acidic. By adding alkali to this acidic primary treated water, the primary treated water is made almost neutral or weakly acidic.
Examples of the alkali used for the neutralization treatment include sodium hydroxide, barium hydroxide, sodium hydrogen carbonate, ammonia, sodium carbonate, calcium carbonate, calcium oxide and the like. Then, the primary treated water is made neutral or weakly acidic, for example, about pH 6 by mixing with alkali. By making the primary treated water exhibiting strong acidity neutral or weak acid in this way, the danger of the primary treated water can be reduced, and handling in the subsequent process becomes easy. In addition, when the primary treated water after a separation process is neutral, this neutralization process does not need to be performed. Moreover, when the primary treated water after a separation process is alkaline, you may neutralize by adding an acid at this neutralization process.

[Evaporation process]
Next, the above-described primary treated water is heated to remove moisture and the like contained in the primary treated water.
The primary treated water contains residues such as chemicals that have not been separated and extracted in the above-described separation and extraction step of the polymer mass. For this reason, water and a residue etc. are isolate | separated by heating primary treated water and vaporizing water.

In this evaporation step, the primary treated water is vaporized to separate into waste steam from which water or the like has been vaporized and residual waste liquid containing chemicals or the like. In this evaporation step, the primary treated water is evaporated and vaporized.
In order to prevent vaporization of water-soluble substances, the primary treated water is not completely evaporated but remains as a liquid. Water and substances such as chemicals that are soluble in water are left in the residual waste liquid to suppress movement into the waste steam. For this reason, the concentration rate of the primary treated water is about 30%.
Thereby, evaporation of the residue of chemical | medical agents, such as 2-aminoethanol contained in primary treated water, can fully be reduced, for example, can be restrained below the working environment allowable density | concentration by the Japan Society for Occupational Health.

[Dilution process]
Waste steam vaporized in the evaporation step is discharged from a gas discharge port such as a chimney.
The waste steam discharged here consists almost of water. However, the primary treated water contains water-soluble substances. For example, a release agent and a solvent contained in the release agent are included. In particular, it is known that 2-aminoethanol contained in the release agent is contained in the primary treated water. In addition, since various other substances are dissolved in the primary treated water, these substances are vaporized together with the water and are contained in the waste steam.

  Thus, by heating and drying the primary treated water, other substances are exhausted simultaneously with the water. For this reason, when this exhaust is discharged to the outside through the discharge port of the processing facility, there is an odor due to the contained chemicals. Odor regulations are set forth, for example, in the Odor Control Law. In the Odor Control Law, regulatory standards are set for the odor index of exhaust gas and the height of gas outlets. In addition, 2-aminoethanol is designated as a Class 1 Designated Substance in the Chemical Substance Emission Control and Management (PRTR) Law, and the working environment allowable concentration and the like are determined by the Japan Society for Occupational Health.

Therefore, in order to reduce the concentration of the odor or the like of the waste steam, the waste steam is diluted with air using a blower or the like before being exhausted from a gas exhaust port such as a chimney. By diluting, the odor in the waste steam can be reduced. Moreover, the density | concentration of the chemical | medical agent which causes the odor in waste steam can be reduced.
Dilution lowers the odor index of the steam exhausted from the gas outlet of the chimney or the like to the odor index that can meet the regulations of the Odor Control Law. Further, even when the odor index of waste steam exceeds the reference value, the exhaust from the gas discharge port can be made below the reference value by diluting with air before discharge. For this reason, the height of a gas exhaust port can be made into below a standard. Moreover, it is not necessary to install a new deodorizing device.

[Mixing process]
Separately from the dilution step, the residual waste liquid is treated.
The residual waste liquid contains a concentrated polymer wax component, release agent, and the like remaining in the primary treated water. Moreover, since the primary treated water is concentrated to 30% in the above evaporation step, the residual waste liquid contains water.
By removing this water, the components in the residual waste liquid can be mixed with the polymer mass to obtain a solid fuel material.

  First, the residual waste liquid and the absorbent material are mixed. By mixing the absorbent, the components in the residual waste liquid are adsorbed on the absorbent. By adsorbing, evaporation of components other than water contained in the residual waste liquid when the residual waste liquid is dried is suppressed. Moreover, when using it as a solid fuel, an absorbent material is used as a combustion aid.

  Absorbents include, for example, sawdust, rice husk, buckwheat husk, coconut husk, fiber such as paper, thread, hair, fruit, wine, sake, shochu, soybeans, okara, beer, oil, sugar beet Squeeze, bonito kelp dashi, konjac flying powder, nut shells, activated carbon and the like can be used. Since these illustrated absorbent materials are normally disposed of in large quantities as waste, the cost of the absorbent materials can be reduced.

[Drying process]
Next, the mixture of the residual waste liquid and the absorbent is naturally dried, blown dry, or heat dried.
The drying method is not particularly limited, but it is preferable to dry at a low temperature so that components other than water contained in the residual waste liquid do not vaporize.
Due to the low drying rate, the diffusion rate of substances that cause odors into the atmosphere is low and the concentration is low, so odor problems do not occur. Furthermore, since it is concentrated to about 30% from the primary treated water, the treatment process is not affected even if the drying speed is slow.

Through the above process, the stripping waste liquid can be processed.
By treating the polymer wax stripping waste liquid in this way, the polymer is separated and extracted by adding an acid from the polymer wax stripping waste liquid, and the amine in the harmful stripping agent in the stripping waste liquid is changed to a salt. Detoxify. The extracted polymer is used as a solid fuel. Since this polymer is the main component of the flooring agent, it is extracted in a very large amount, but since it is used for the production of solid fuel, the generation of a large amount of industrial waste is avoided.

(Peeling waste liquid treatment equipment)
Next, a specific embodiment of the treatment apparatus for the stripping waste liquid for performing the above-described processing will be described. An apparatus for treating a stripping waste liquid described below is an apparatus for stripping waste liquid generated by a polymer wax stripping operation in, for example, repainting a polymer wax applied to a floor surface. The polymer wax applied to the floor surface is peeled off by a release agent such as amines. For this reason, the polymer wax peeling waste liquid contains a peeled polymer wax, a release agent, and the like.

[Configuration of waste liquid treatment equipment]
In FIG. 2, the schematic block diagram of the processing apparatus of the peeling waste liquid of this Embodiment is shown. The stripping waste liquid treatment apparatus shown in FIG. 2 includes a stripping waste liquid tank 10, an agglomeration stirring tank 11, a neutralization stirring tank 12, an evaporation tank 13, and a blower 14.

The peeling waste liquid tank 10 stores the above-described polymer wax peeling waste liquid. And it transfers from this peeling waste liquid tank 10 to the aggregation stirring tank 11 using the pump 21 grade | etc.,.
In the agglomeration stirring tank 11, the flocculant is mixed with the peeling waste liquid transferred from the peeling waste liquid tank 10. The flocculant is supplied from the flocculant tank 15 to the flocculant stirring tank 11. The supply of the flocculant is controlled by an electromagnetic valve 25 provided between the flocculant stirring tank 11 and the flocculant tank 15.

The aggregation stirring tank 11 includes a pH meter 31 and a tank rotation motor 26. Then, the peeling waste liquid and the flocculant are stirred and mixed by the tank rotation motor 26 that rotates the aggregation stirring tank 11. Moreover, as stirring of the agglomeration stirring tank 11, for example, air agitation in which air is supplied to the lower part of the aggregation stirring tank 11 from the compressor 23 provided separately from the aggregation stirring tank 11 to stir the inside of the aggregation stirring tank 11 is performed. Do. In addition, other stirring means can be used as the stirring of the aggregation stirring tank 11, and for example, a stirring tank including a stirring blade may be used. A plurality of these stirring methods may be provided, may be activated simultaneously, or may be activated separately.
In this agglomeration stirring tank 11, the stripping waste liquid is a wax component, that is, a semi-solid polymer mass is deposited in the stripping waste liquid.

In the flocculation agitation tank 11, the precipitated polymer mass is removed by the filtration tank 17. The filtration tank 17 includes a filter for solid-liquid separation for filtration inside. By this filter, the polymer lump precipitated in the aggregation stirring tank 11 and the primary treated water are separated.
Furthermore, in order to isolate | separate the primary treated water contained in the polymer lump taken out from the filtration tank 17, a dehydrator 18 is separately provided as a separation device.
The primary treated water separated by the filtration tank 17 and the dehydrator 18 is accumulated in the neutralization stirring tank 12.

The neutralization agitation tank 12 accumulates the primary treated water that has been processed in the agglomeration agitation tank 11 and from which the polymer mass has been separated. The neutralization stirring tank 12 includes a pH meter 32. In the neutralization stirring tank 12, the pH of the primary treated water that has become acidic by the treatment in the aggregation stirring tank 11 is neutralized.
The neutralizing agent (alkali) is supplied from the neutralizing agent tank 16 to the neutralization stirring tank 12. The supply of the neutralizing agent is controlled by an electromagnetic valve 27 provided between the neutralizing stirring tank 12 and the neutralizing agent tank 16.
In addition, the separation waste liquid treatment apparatus shown in FIG. 2 includes a primary treatment water tank 20 for storing the primary treatment water treated in the neutralization stirring tank 12. The primary treated water is transferred from the neutralization stirring tank 12 to the primary treated water tank 20 by driving the pump 22.

The evaporation tank 13 evaporates the primary treated water that has been neutralized and stored in the primary treated water tank 20. The transfer of the primary treated water from the primary treated water tank 20 to the evaporation tank 13 is controlled by opening and closing the electromagnetic valve 29.
The evaporating tank 13 is a heat exchanger, and has a configuration in which a heating steam pipe from the boiler 30 provided outside passes through the inside. And the heating vapor | steam heated with the boiler 30 is supplied to the evaporation tank 13, and it heats by heat exchange with the primary treated water in the evaporation tank 13, and a water | moisture content evaporates.

  The water evaporated in the evaporating tank 13 is exhausted from the gas outlet 34 to the outside of the apparatus as exhaust. A blower 14 is connected between the evaporation tank 13 and the gas discharge port 34, and the exhaust from the evaporation tank 13 is diluted with air (outside air) supplied from the blower 14.

After the evaporation process in the evaporation tank 13, the residual waste liquid remaining in the evaporation tank 13 is discharged into the residual waste liquid tank 19. The residual waste liquid tank 19 is a heat exchanger like the evaporation tank 13, and has a configuration in which a pipe for heating steam from a boiler 30 provided outside passes through the inside. Further, the residual waste liquid tank 19 is previously filled with a residual waste liquid absorber. The residual waste liquid tank 19 is provided with a motor 37 for stirring, and the residual waste liquid is dried by heating steam from the boiler 30 while mixing the residual waste liquid in the residual waste liquid tank 19 and the absorbent.
The heating steam is supplied from the boiler 30 to the evaporation tank 13 and the residual waste liquid tank 19 by switching between the electromagnetic valve 33 and the electromagnetic valve 36.

The stripping waste liquid treatment apparatus includes a compressor 23. The compressor 23 supplies air for stirring the aggregation stirring tank 11 and the neutralization stirring tank 12. The supply of air to the aggregation stirring tank 11 and the neutralization stirring tank 12 is operated by opening and closing the electromagnetic valve 24 and the electromagnetic valve 28. The compressor 23 supplies air to the pump 21 and the pump 22 and drives the pump 21 and the pump 22.
Furthermore, each tank of the apparatus includes a meter such as a limit switch RS and a pH meter as necessary.

[Operation of waste liquid treatment equipment]
Next, an operation method of the above-described peeling waste liquid processing apparatus will be described.
First, the compressor 23 is started by pressing the operation panel start switch (SW). Then, after the operation of the compressor 23, the stripping waste liquid in the stripping waste liquid tank 10 is transferred to the aggregation stirring tank 11 by the pump 21.

When the upper limit switch RS3 of the agglomeration stirring tank 11 senses the peeling waste liquid, the pump 21 stops, the electromagnetic valve 24 opens, air is sent from the compressor 23 to the aggregation stirring tank 11, and the peeling waste liquid in the aggregation stirring tank 11 Is stirred.
Further, after the upper limit switch RS3 senses, the electromagnetic valve 25 is opened, and the flocculant is charged into the flocculant stirring tank 11 from the flocculant tank 15.

After the pH meter 31 installed in the flocculation agitation tank 11 senses a predetermined pH of the peeling waste liquid, for example, about pH 1 to 3, the electromagnetic valve 25 and the electromagnetic valve 24 are closed, and the flocculant is charged into the flocculation agitation tank 11. Then, the supply of air for stirring is stopped.
At this time, the peeling waste liquid in the aggregation stirring tank 11 is mixed and stirred with the flocculant, so that the polymer wax, the release agent, and the like contained in the peeling waste liquid are aggregated as a polymer lump.

After the pH meter 31 senses, the tank rotation motor 26 attached to the coagulation stirring tank 11 is driven, and the peeling waste liquid in the coagulation stirring tank 11 is discharged to the filtration tank 17. In the filtration tank 17, a filter for solid-liquid separation is provided, and the separation waste liquid in the aggregation stirring tank 11 is separated into a polymer lump and primary treated water.
The primary treated water separated in the filtration tank 17 is accumulated in the neutralization stirring tank 12.
The polymer mass is transferred from the filtration tank 17 to the dehydrator 18 to separate water contained in the polymer mass. The separated water is accumulated in the neutralization stirring tank 12 in the same manner as the primary treated water.

When the upper limit switch RS5 of the neutralization stirring tank 12 is operated by the accumulated primary treated water, the electromagnetic valve 27 is opened, and the neutralizing agent (alkali) is charged from the neutralizing agent tank 16 to the neutralization stirring tank 12. The At the same time, the electromagnetic valve 28 is opened, air is sent from the compressor 23 to the neutralization stirring tank 12, and the primary treated water in the neutralization stirring tank 12 is stirred.
The pH meter 32 installed in the neutralization agitation tank 12 senses a predetermined pH (about 7) of the primary treated water, and after the neutralization treatment of the primary treated water is completed, the solenoid valve 27 and the solenoid valve 28. Close.

After the neutralization treatment, the pump 22 is driven, and the primary treatment water in the neutralization stirring tank 12 is pumped up to the primary treatment water tank 20.
When the upper limit switch RS7 of the primary treatment water tank 20 senses, the pump 22 is stopped. Then, the electromagnetic valve 29 is opened, the primary treated water is transferred from the primary treated water tank 20 to the evaporating tank 13, and the evaporating tank 13 is filled with the primary treated water. At the same time, the boiler 30 is ignited, the electromagnetic valve 33 is opened, and the blower 14 is activated.
Heated steam from the boiler 30 is supplied into the evaporation tank 13, and the primary treated water is vaporized by heat exchange between the primary treated water and the heated steam in the evaporation tank 13.
The waste steam vaporized from the primary treated water is exhausted from the gas outlet 34 in a state diluted with the air from the blower 14.

When the lower limit switch RS8 of the primary treatment water tank 20 is operated, the electromagnetic valve 33 is closed and the boiler 30 is stopped.
The electromagnetic valve 35 is opened, and the residual waste liquid in the evaporation tank 13 is discharged into the residual waste liquid tank 19. The electromagnetic valve 36 is opened, and heated steam due to the residual heat of the boiler 30 is introduced into the residual waste liquid tank 19.
The residual waste liquid is dried by the heating steam from the boiler 30 while mixing the residual waste liquid in the residual waste liquid tank 19 and the absorbent by the motor 37 provided in the residual waste liquid tank 19.
When the upper limit switch RS10 of the residual waste liquid tank 19 senses, the electromagnetic valve 35 is closed and the discharge of the residual waste liquid is stopped.
After drying the residual waste liquid, reset all switches and return to the initial operation.

Hereinafter, the above-described peeling waste liquid treatment of the present invention will be described using examples.
[Exhaust concentration test of 2-aminoethanol]
In the evaporation process of the primary treated water, the concentration of 2-aminoethanol contained in the waste steam was measured. Since 2-aminoethanol is used as a stripping agent or the like, it is contained in the stripping waste liquid.

First, with respect to the polymer wax peeling waste liquid, primary treated water was obtained by the method of the above-described embodiment. And the heat treatment concentration was performed about this primary treated water. Furthermore, this heat-treated primary treated water was used as a sample and distilled to measure 2-aminoethanol in the distillate. The concentration of 2-aminoethanol in the primary treated water before heating and concentration was 4600 (mg / L).
Table 1 shows the concentration rate of the primary treated water by heat concentration.

Next, with respect to the primary treated water after concentration, 500 ml of the final concentrated solution was collected, and 5 ml of 0.1 mol sulfuric acid was mixed as an absorbing solution. And distillation operation was performed with respect to this liquid mixture. In the distillation operation, 95 ml of a distillate collected from the start of distillation and 95 ml collected at the end of the distillation were used as measurement samples. The first collected distillate was used as the starting distillate, and the last collected distillate was used as the post distillate, and the concentration of 2-aminoethanol contained therein was measured.
Table 2 shows the mass of the primary treated water before fractionation (before the distillation experiment), the fractionation amount, and the mass of the fractionated sample before and after distillation. Table 3 shows the concentration rate of the primary treated water and the concentration rate of the sample for the first and subsequent distillations.

Next, 0.2 ml fractions were taken from the collected 95 ml of the distillate for each of the first distillate and the postdistillate. This was mixed with 0.3 ml of 1 mol / L borate buffer and 0.5 ml of 15 mmol / L FMOC (acetonitrile), stirred for 1 minute, and then allowed to stand for 5 minutes. Next, 10 μl of 10% N-methylmorpholine and 50 μl of acetic acid were mixed with this sample.
This sample was measured for the concentration of 2-aminoethanol using high performance liquid chromatographic analysis. The conditions used for the high performance liquid chromatographic analysis are shown below. Table 4 shows the 2-aminoethanol concentration (mg / L) of the sample for the first distillation and the post-distillation.

Derivatizing reagent: FMOC (9-fluorenylmethyl chloroformate)
Apparatus: Waters 2695-2996
Column: Waters XBridge C18 (5 μm, 150 × 4.6 mm)
Mobile phase: water, acetonitrile (60:40)
Detector: Photodiode array detector (PDA)
Quantitative wavelength: 265nm
Injection volume: 5 μl

Next, Table 5 shows the result of converting the concentration of 2-aminoethanol shown in Table 4 into the concentration (mg / m ³ ) in the gas. Conversion to the concentration in the gas was performed by converting all water into a gasified state, 1000 g per 1 L of water, 18 molecular weight of water, and 22.4 L per 1 mol of gas.

As shown in Table 5, the concentration of 2-aminoethanol generated in the evaporation of the primary treated water in the gas is 0.66 (mg / m ³ ) and 1.08 (mg / m ³ ) on average. Met. Furthermore, 32.8% began distillate concentration ratio, when the 34.4%, 2-amino ethanol concentration 0.24 mg ^/ m 3, was 0.74 mg / ^{m 3.} Then, post-distillation fraction concentration ratio of 25.8 percent, when 27.0% of 2-aminoethanol concentration 1.08 mg ^/ m 3, was 1.42 mg / ^{m 3.}
2-Aminoethanol is designated as a Class 1 Designated Substance in the PRTR Law, but there are no standards for emission into the air or water, nor for human intake. Regarding inhalation exposure, in addition to the non-toxic amount in the test with rats set to 0.12 mg / m ³ , the recommended working environment concentration of 7.5 mg / m ³ (3 ppm) by the Japan Society for Occupational Health is recommended. ing.
On the other hand, in the result of the above-mentioned concentration measurement of 2-aminoethanol, even if the primary treated water is concentrated to about 30%, the concentration of 2-aminoethanol in the waste steam is lower than the allowable working environment concentration. . Moreover, since the concentration when the concentration rate of the post-distilled fraction is 25.8 to 27.0% is 1.08 to 1.42 mg / m ³ , the waste steam is increased to about 10 times even in the non-toxic amount. It turns out that it becomes a density | concentration without a problem by diluting.
Therefore, in the stripping waste liquid treatment of this embodiment described above, in the primary treatment water evaporation step, the concentration rate of the primary treatment water is set to about 25 to 30%, and the concentrated primary treatment water is treated as a residual waste liquid. It is preferable to do.

[Odor measurement]
Next, the exhaust odor generated in the evaporation process of the primary treated water was measured.
First, with respect to the polymer wax peeling waste liquid, primary treated water was obtained by the method of the above-described embodiment. And the evaporation process was performed with respect to this primary treated water. Odor was measured for the waste steam generated by this evaporation treatment.
The odor of waste steam was measured according to 1995 Environment Agency Notification No. 63 (method of outlet sample). Moreover, the odor measurement of waste steam was performed 3 times using the primary treated water each processed from another peeling waste liquid (Odor Experimental Examples 1-3).

About the odor measurement result of waste steam, Table 6 shows the odor experimental example 1, Table 7 shows the odor experimental example 2, and Table 8 shows the odor experimental example 3. Tables 6 to 8 are based on the waste steam generated from the evaporation tank, and the wind speed at this time is 0 (m / s). And the change of the odor of exhaust_gas | exhaustion when the wind speed of the external air from a blower when starting a blower and diluting waste steam is changed from 1 (m / s) to 5 (m / s) is shown.
Moreover, a wind speed shows the setting value of an air blower, and the measured value (m / s) by the anemometer provided in the discharge port. The air volume (m ³ / h) is converted from the measured value of the wind speed.
The actual multiple odor concentration is a numerical value obtained by dividing the odor concentration by the dilution factor. The actual multiple odor concentration is a theoretical value when the odor concentration of exhaust, which is predicted to be reduced by dilution with a blower, is simply calculated based on the dilution rate from the odor concentration at a wind speed of 0.
The amount of gas (L) is calculated based on the difference between the weight before heating (kg) of the primary treated water and the weight after completion of the experiment (kg) and the experimental time (h) when the wind speed is 0. Considering the evaporation of water, it was converted to a molecular weight of 18 and 22.4 L per 1 mol of gas. Further, the gas amount when the wind speed is other than 0 is a numerical value obtained by adding the gas amount when the wind speed is 0 to the air volume. Specifically, in the odor experimental example 1, since the weight before heating is 6.2 kg, the weight after the experiment is 4.9 kg, and the experiment time is 45 minutes, the reduction amount is 1.73 kg / h, and the gas amount is 2153L. It becomes. Moreover, in the odor experimental example 2, since the weight before heating is 6.65 kg, the weight after completion of the experiment is 5.60 kg, and the experiment time is 42 minutes, the reduction amount is 1.5 kg / h and the gas amount is 1867L. . In the odor experiment example 3, since the weight before heating is 6.69 kg, the weight after the experiment is 5.65 kg, and the experiment time is 35 minutes, the decrease amount is 1.61 kg / h, and the gas amount is 2004L.
The ratio is a numerical value obtained by dividing the gas amount when the wind speed is 0 by the air amount, and the dilution factor is the reciprocal of the ratio.
The air volume (m ³ / h) index is a common logarithm of air volume.

  From the results of Odor Experimental Example 1 shown in Table 6, the relationship between the air volume and the odor index is shown in FIG. As shown in FIG. 3, the odor index decreases exponentially with increasing air volume. FIG. 4 shows the relationship between air volume and odor concentration. As shown in FIG. 4, the odor concentration decreases exponentially with increasing air volume.

Next, FIG. 5 shows the relationship between the air volume index converted value and the odor index. As shown in FIG. 5, there is shown a relationship in which the odor index decreases so as to be approximately proportional to the increase in the airflow index conversion value.
FIG. 6 shows the relationship between the dilution factor and the odor index. As shown in FIG. 6, as the dilution factor increases, the odor index decreases so as to be approximately proportional.

Similarly, from the results of Odor Experimental Example 2 shown in Table 7, the relationship between the air volume and the odor index, the relationship between the air volume and the odor concentration, the relationship between the air volume index converted value and the odor index, and the dilution rate and the odor index. The relationship is shown in FIGS.
Moreover, from the result of the odor experiment example 3 shown in Table 8, the relationship between the air volume and the odor index, the relationship between the air volume and the odor concentration, the relationship between the air volume index converted value and the odor index, and the dilution factor and the odor index. The relationship is shown in FIGS.

  As shown in FIGS. 7, 8, 11, and 12, the odor index and the odor concentration decrease exponentially as the air volume increases. Moreover, as shown in FIGS. 9, 10, 13 and 14, the odor index decreases so as to be approximately proportional to the increase in the air volume index converted value and the dilution factor.

From the above results, it can be seen that the reduction in odor decreases in proportion to the dilution air volume, the exponential function of the air volume, and the dilution factor. As indicated by the relationship between the odor concentration and the actual multiple odor concentration, even if the waste steam of the primary treatment water is diluted to a predetermined multiple, the odor concentration does not decrease according to the dilution amount. Represents that.
For example, the odor index of the waste steam of the primary treated water is 41 to 49, and the odor concentration is 13,000 to 79000. And when waste steam is diluted about 90 times (wind speed 3m / s), an odor density | concentration will be 250-400. The odor index at this time is 24-26.
That is, in order to sufficiently reduce the odor concentration or odor index to a value that can be adapted to the malodor control method, it is necessary to determine the dilution air volume in consideration of an exponential decrease in the odor concentration or odor index. Although the regulation conditions of the odor index in the malodor prevention method will be described later, the odor indices 24-26 at the dilution factor 90 are sufficiently low odor indices that can practically meet the regulation of the outlet.
Furthermore, in the odor experiment example described above, the odor index can be reduced to 17-22 by setting the wind speed to 5 m / s. The odor index 17 to 22 is a sufficiently low odor index that can practically conform to the regulation of the outlet, similarly to the wind speed of 3 m / s.

  In the Odor Prevention Law, the odor control standard (No. 2 standard) for gas outlets such as chimneys based on the odor index regulates exhaust at the outlet. The odor gas discharged from the gas discharge port is gradually diffused and diluted and landed on the ground surface. In the No. 2 standard, the odor emission standard at the outlet is set so that this odor is below the regulation standard (No. 1 standard) on the site boundary at the landing point outside the site boundary.

In the odor experiment example described above, when the odor index at the wind speed of 5 m / s is assumed to be 22 which is the largest value, the diameter and height of the discharge port to meet the No. 1 regulation are observed. The height of the outlet is less than 15m.
According to the odor index regulation of the Odor Control Law, the diameter of an outlet having a height of less than 15 m is defined as “small” if it is less than 60 cm, “medium” if it is 60 cm or more but less than 90 cm, and “large” if it is 90 cm or more.
The standard value of No. 1 regulation is determined according to the outline of the local government and the regulated area. Hereinafter, the conditions of the exhaust port for the exhaust gas having the odor index 22 of the above-described odor experimental example to conform to the No. 1 regulation will be shown. Table 9 summarizes the conditions of the discharge port.

When the No. 1 regulation is set to 21 in the semi-industrial area, the industrial area, the industrial exclusive area, etc., in order for the exhaust gas of the odor index 22 of the above-mentioned odor experiment example to comply with the No. 1 regulation, It is necessary to determine the outlet as follows.
If the diameter of the discharge port is small, the height of the discharge port needs to be 0.9 m or more.
If the diameter of the discharge port is medium, the height of the discharge port needs to be 1.6 m or more.
If the diameter of the discharge port is large, the height of the discharge port needs to be 2.3 m or more.

When the No. 1 regulation is set to 18 in the city adjustment area, etc., in order for the exhaust gas of the odor index 22 in the above-mentioned odor experiment example to comply with the No. 1 regulation, it is necessary to define the outlet as follows. is there.
If the diameter of the discharge port is small, the height of the discharge port needs to be 1.3 m or more.
If the diameter of the discharge port is medium, the height of the discharge port needs to be 2.3 m or more.
If the diameter of the discharge port is large, the height of the discharge port needs to be 3.2 m or more.

When the No. 1 regulation is set at 15 in commercial areas, etc., in order for the exhaust gas with the odor index 22 of the above-mentioned odor experiment example to comply with the No. 1 regulation, it is necessary to define the outlet as follows: .
If the diameter of the discharge port is small, the height of the discharge port needs to be 1.7 m or more.
If the diameter of the discharge port is medium, the height of the discharge port needs to be 3.2 m or more.
If the diameter of the discharge port is large, the height of the discharge port needs to be 4.5 m or more.

When the No. 1 regulation is set to 12 in each residential area, residential area, etc., in order for the exhaust gas with the odor index 22 of the above odor experiment example to comply with the No. 1 regulation, the outlet is as follows: It is necessary to determine.
If the diameter of the discharge port is small, the height of the discharge port needs to be 2.4 m or more.
If the diameter of the discharge port is medium, the height of the discharge port needs to be 4.5 m or more.
If the diameter of the discharge port is large, the height of the discharge port needs to be 6.3 m or more.

  As described above, the waste water from the primary treated water is diluted, and further, the discharge port is set to the above-described conditions, thereby constituting a treatment apparatus for the polymer wax peeling waste liquid that complies with the regulations of the Odor Control Law. be able to. That is, by diluting the waste steam from the primary treated water using a blower, the installation condition of the discharge port can be relaxed to the above-mentioned regulation condition. For this reason, even in the existing exhaust equipment, if it is within the above range, the method for treating the polymer wax peeling waste liquid of this embodiment can be carried out without introducing new equipment.

  DESCRIPTION OF SYMBOLS 10 Separation waste liquid tank, 11 Aggregation stirring tank, 12 Neutralization stirring tank, 13 Evaporation tank, 14 Blower, 15 Coagulant tank, 16 Neutralizing agent tank, 17 Filtration tank, 18 Dehydrator, 19 Residual liquid tank, 20 Primary Treated water tank, 21, 22, 30, 37 boiler, 23 compressor, 24, 25, 27, 28, 29, 33, 35 Solenoid valve, 26 tank rotation motor, 31, 32 pH meter, 34 Gas outlet, RS1, RS3 RS5, RS7, RS10, RS13 Upper limit switch, RS2, RS4, RS6, RS8, RS9, RS11, RS12, RS14 Lower limit switch

Claims (8)

A coagulation agitation tank for mixing the polymer wax peeling waste liquid and the coagulant;
A filtration tank for separating the stripping waste liquid in the agglomeration stirring tank into a polymer mass and primary treated water;
An evaporating tank for heating the primary treated water to generate heated steam ;
And a blower provided at a gas discharge port of the evaporating tank. 2. The polymer wax peeling waste liquid according to claim 1, further comprising a residual waste tank that mixes the residual waste liquid in the evaporation tank and the absorbent and dries the mixture of the residual waste liquid and the absorbent. Processing equipment.   The apparatus for treating a polymer wax peeling waste liquid according to claim 1 or 2, wherein air agitation is performed in the coagulation agitation tank. An agglomeration treatment step of adding a flocculant to the polymer wax peeling waste liquid to precipitate a polymer mass;
A separation step of extracting the polymer mass and separating the stripping waste liquid into a polymer mass and primary treated water;
Evaporating step of heating the primary treated water to generate heated steam ,
A method for treating a polymer wax peeling waste liquid, wherein the waste steam generated in the evaporation step is diluted and exhausted.   The method for treating a polymer wax peeling waste liquid according to claim 4, wherein the dilution ratio is 90 times or more.   The method for treating a polymer wax peeling waste liquid according to claim 4, wherein an air volume for diluting the waste steam is set to 3 m / s or more. The processing method of the peeling waste liquid in any one of Claim 4 to 6 which has a mixing process which mixes the residual waste liquid in the said evaporation process with an absorber. The processing method of the peeling waste liquid of Claim 7 which has a drying process which dries the mixture of the said residual waste liquid and the said absorber.

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