JP2008296166A - Purification method for wastewater discharged from spirit production facility - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a purification method for wastewater which can easily and stably treat wastewater discharged from a spirit production facility, containing pollutants having a very high COD concentration of more than 60,000 mg/l to be converted into almost colorless and transparent wastewater which can be discharged to the outside and has a COD concentration of about 2,000-3,000 mg/l. <P>SOLUTION: The purification method for wastewater comprises the coagulant adding process for mixing a coagulant mainly comprising crosslinked polyglutamic acid with wastewater, a first centrifugal separation process for removing solids in the wastewater from the coagulant adding process, a chemical treatment process for adding an alkali agent and hydrogen peroxide to the wastewater from the centrifugal separation process to decompose organic matter in the wastewater, second and third centrifugal separation processes for removing solids in the wastewater from the chemical treatment process, and the first filtration-absorption process and a second filtration-absorption process for purifying the wastewater from the third centrifugal separation process. <P>COPYRIGHT: (C)2009,JPO&INPIT

Description

  The present invention relates to an improvement of a method for treating wastewater discharged from a manufacturing facility for distilled liquor such as whiskey, tequila, cognac, and shochu, and efficiently removes high-concentration organic substances and the like contained in the wastewater. The present invention relates to a method for purifying wastewater discharged from a distilled liquor manufacturing facility that can be treated into nearly transparent wastewater.

  Wastewater discharged from whiskey, shochu and other distilled liquor production facilities contains a large amount of organic substances, and these organic substances contain a relatively large amount of persistent colorants. It is. For this reason, wastewater containing high-concentration pollutants (for example, COD values of 60000 mg / l or more) from distilled liquor production facilities cannot be obtained by simply subjecting the wastewater to biological treatment, precipitation treatment or filtration treatment. However, there is a problem that it is difficult to sufficiently purify this, and it is impossible to make the waste water nearly transparent.

  For this reason, a complex large-scale treatment device combined with a precipitation device, a biological treatment device, an ozone generation device, a filtration device, an adsorption device, etc., or a microorganism that decomposes a hardly decomposable substance (coloring substance) is used. Treatment equipment has been developed for the treatment of wastewater from distilled liquor manufacturing facilities and the like.

  However, large processing equipment that combines primary processing equipment, secondary processing equipment, tertiary processing equipment, etc., consisting of the former precipitation equipment, ozone generator, filtration equipment, adsorption equipment, etc., increases the equipment cost and equipment costs. There is a problem that operation management takes too much time.

  In addition, the latter treatment apparatus using microorganisms that decompose the hardly decomposable substance has a problem that it is difficult to reduce the size of the equipment due to the long time required for the treatment, the equipment cost increases, and the management of microorganisms is extremely difficult. have.

  In this way, purification of wastewater containing high-concentration pollutants discharged from facilities equipped with an alcohol fermentation process is extremely difficult, and these wastewaters can be easily and smoothly made stable. Therefore, development of a treatment method that can be purified is awaited.

JP 2002-223746 A JP 2003-274929 A

  The present invention requires the above-mentioned problem in the purification treatment of wastewater containing extremely high concentration of pollutant discharged from the distilled liquor production facility, that is, (i) a complicated large-scale treatment device having a structure is required. Equipment costs soar or require a lot of manpower to manage the operation of the equipment. (Ii) A processing device that uses microorganisms requires a long time for processing and manpower management. In order to solve this problem, wastewater containing extremely high-concentration pollutants can be purified to simple, highly efficient, stable and nearly transparent wastewater with an inexpensive treatment device with a simple structure. The main object of the present invention is to provide a method for purifying wastewater discharged from a distilled liquor production facility so that it can be treated.

  In the present invention, firstly, a flocculant, for example, a biodegradable flocculant mainly composed of a cross-linked polyglutamic acid (manufactured by Japan Polyglu Co., Ltd., hereinafter referred to as PGα21Ca) is added to waste water from a distilled liquor production facility, The wastewater to which the flocculant is added is centrifuged to remove the aggregates (solid matter) in the wastewater, and then the residual organic matter in the wastewater after the removal of the aggregates (solid matter) is treated with an alkali agent. It is chemically decomposed with hydrogen oxide, and solids are removed from the wastewater after chemical treatment by centrifugation, and the wastewater after removing the solids is filtered and adsorbed. By removing residual organic matter, wastewater containing high-concentration pollutants from distilled liquor production facilities can be treated efficiently, inexpensively, and stably to nearly transparent wastewater. It is.

  That is, the present invention relates to a flocculant addition step of mixing a flocculant with wastewater containing high-concentration pollutant discharged from a distilled liquor manufacturing facility, and a first step of removing solids in the wastewater from the flocculant addition step. Centrifugation step, chemical treatment step of decomposing organic matter in waste water by adding alkaline agent and hydrogen peroxide to waste water from the centrifugation step, and second centrifugation to remove solid matter in waste water from chemical treatment step A distilled liquor manufacturing facility characterized in that it comprises a first filtration / adsorption process and a second filtration / adsorption process for purifying the waste water from the third centrifugation process and the third centrifugation process. This is a method for purifying wastewater.

  As the flocculant to be added in the flocculant addition step, a flocculant mainly composed of a polyglutamic acid cross-linked product is desirable, and the amount of the flocculant mainly composed of the polyglutamic acid cross-linked product is determined by the concentration of the flocculant in the waste water. The amount is preferably 150 ppm.

  Moreover, the 1st centrifugation process which processes the wastewater from a coagulant | flocculant addition process is set as the centrifugation process which processes wastewater by wastewater temperature 40-60 degreeC, the centrifugal force 2500-50500G, and the centrifugation time 6-8 minutes. Is desirable.

  Furthermore, between the first centrifugation step and the chemical treatment step, heavy metal removal is performed by adding diethylenetriaminepentaacetic acid in an amount of 1 wt% in the wastewater as a heavy metal removal agent (chelating agent) into the wastewater. It is desirable to provide an agent addition step.

  In the chemical treatment process, hydrogen peroxide, sodium silicate, caustic soda, and an alkali solution formed by mixing water are stirred and mixed into the waste water to automatically adjust the PH value of the waste water to about 10.8. At the same time, it is desirable to use a chemical treatment step for decomposing organic substances in the wastewater while maintaining the temperature at 40 to 60 ° C.

  It is desirable to provide a calcium oxide addition step of adding calcium oxide in an amount such that the concentration in the waste water is 0.5 wt% to the waste water from the second centrifugation step.

  It is desirable that the second centrifugation step and the third centrifugation step are centrifugal steps in which waste water is treated with a centrifugal force of 2500 to 3500 G and a centrifugal time of 6 to 8 minutes.

  It is desirable to provide a sulfuric acid addition step for adjusting the PH value of the waste water to approximately 7.0 by adding sulfuric acid to the waste water from the third centrifugation step on the upstream side of the first filtration / adsorption step.

  The first filtration / adsorption process is preferably a filtration / adsorption process using a column packed with calcium carbonate and diatomaceous earth as an adsorbent.

  The second filtration / adsorption step is preferably a filtration / adsorption step using a column filled with activated carbon as a filtration / adsorbent.

Basically, in the present invention, waste water is obtained by organically combining a centrifugal separation process for removing solids, which has been widely used in the past, a chemical decomposition process for organic substances, and a filtration and adsorption process for solid substances. While constituting the purification treatment method, this purification treatment method is used to treat high-concentration wastewater from the distilled liquor manufacturing facility.
As a result, the purification treatment method of the present invention can be carried out based on the conventional technique, and a highly efficient and stable wastewater purification treatment can be performed.

  In the present invention, the biodegradable flocculant PGα21Ca is first mixed into the wastewater, and the mixing concentration and mixing temperature are maintained at optimum values. Therefore, the organic matter in the waste water can be efficiently and quickly aggregated, and the aggregate (solid matter) can be easily removed by the centrifugal separation process.

  Furthermore, in the present invention, a coagulation treatment with a biodegradable coagulant mainly composed of a polyglutamic acid cross-linked product, a chemical decomposition treatment of organic matter, a centrifugation treatment for removing the solid matter after decomposition, and a residual solid matter are removed. The waste water from the distilled liquor manufacturing process (Vinassas Vinasses) containing very high concentration pollutants with COD values of 60000-65000 mg / l is COD 2000-3000 mg. It is possible to purify the wastewater to almost colorless, odorless waste water of / l.

Hereinafter, the method for purifying wastewater of the present invention will be described with reference to the drawings.
FIG. 1 is a process diagram of a method for purifying wastewater discharged from a distilled liquor manufacturing facility according to the present invention. Here, wastewater A having a temperature of about 80 ° C. discharged from the final production process of distilled liquor (tequila) in Mexico is the object of treatment. That is, this waste water A is a brown liquid containing a large amount of plant fiber after fermenting a raw material mainly composed of agape rice cake and subjecting it to distillation, and contains a high concentration of alcohol fermentation residue. It is a waste liquid and is called Vinasses. Further, the contamination level of this Vinasas is about 60000-65000 mg / l in terms of COD (chemical oxygen demand) value, and the PH value is about 3-3.5.

In the purification treatment of the waste water A, first, the flocculant B is mixed and stirred in the waste water A in the flocculant addition step 1, and then in the first centrifugal separation step 2, the flocculant is separated and removed. Done.
The flocculant B used is a powdery flocculant called PGα21Ca, which was previously developed and put to practical use by the applicant of the present invention, and is a novel natural substance mainly composed of biodegradable γ-polyglutamic acid. It is a degradable substance and is represented by the following structural formula.

The aggregating agent B has the following component contents (wt%).
PGα21 = 14%, C = 0.5%, O = 45%, Na = 8%, Al = 0.5%, Si = 12%, Cl = 0.4, Ca = 15%, K = 0.1 %, Fe = 15%.
O, Ca, Fe, Si, etc. in the flocculant B are usually 2CaSO ₄ · H ₂ O, NaCO ₃ · H ₂ O, NaSO ₄ , MgSO ₄ , 6H ₂ O, Al ₂ (SO ₄ ) · 18H _2. A type of substance represented by a chemical structural formula such as O and contained in the flocculant.

  The removal efficiency of organic substances (pollutant substances) contained in the waste water A largely depends on the amount of the flocculant B added, the temperature of the waste water A, and the operating conditions of the centrifuge. Therefore, the effects of the addition amount of the flocculant B, the treatment temperature of the waste water A, the operation time of the separator, etc. on the pollution removal efficiency were investigated.

  FIG. 2 shows the NTU value (Nephelometric Turbidity Unit / turbidimetric unit of turbidimetric analysis) in the waste water A, the separation processing time (min), the centrifugation time when the decanter type centrifuge is used as the separator. FIG. 2 shows the relationship with the separation force (G). As is clear from FIG. 2, the rotational speed of the centrifuge has a great influence on the removal of organic substances. Judging from the NTU value of A, etc., it is desirable to perform centrifugation for 7.5 to 10 minutes with a centrifugal force of 2500 to 3500 G (preferably 7.5 minutes with a centrifugal force of about 3300 G). In this embodiment, a decanter type centrifuge is used as the centrifuge, but any type of centrifuge may be used.

  Next, in order to investigate the optimum mixing amount of the flocculant (PGα21Ca) B, separation processing is performed for 7.5 minutes with the mixing amount of the flocculant B in the waste water (Vinousus) A and the centrifugal force of 3300G. The NTU value was investigated.

  FIG. 2 shows the results, and it can be seen that it is appropriate that the amount of the flocculant B mixed is such that the flocculant concentration is 100 to 150 ppm. This is because if the amount of the flocculant B is excessive, the NTU value of the wastewater A is increased.

  Furthermore, the influence of the temperature on the aggregation performance of the flocculant (PGα21Ca) B with respect to the organic matter in the wastewater (Vinousus) A was investigated. Specifically, the temperature of the waste water A when the concentration of the flocculant in the waste water A is about 100 ppm and the centrifugal force is about 2500 G and the solid is centrifuged for 7.5 minutes. The relationship between values was investigated.

  FIG. 4 shows the results, and it can be seen that the flocculant B exhibits higher flocculation performance when the temperature of the wastewater A is 40 ° C. to 60 ° C.

  From the results shown in FIGS. 2 to 4, the highest separation performance is obtained in the first centrifugation step 2 because the temperature of the wastewater A is 50 to 60 ° C., the addition amount of the flocculant B is 100 to 150 ppm, The separation power was found to be 3300 G and the centrifugation time was 7.5 minutes.

The waste water A from which aggregates (solid matter) have been removed in the second centrifugation step 2 is a brownish liquid, and various colored components made of organic matter are contained therein.
The waste water A ₁ from which the solid matter has been removed in the second centrifugation step 2 is sent to the chemical treatment step 4 through the heavy metal removing agent addition step 3, where decomposition by a so-called redox reaction of organic matter is performed.

The heavy metal removing agent adding step 3 is a step necessary for chelating and removing the heavy metal in the wastewater A ₁ , and the step 3 is provided when the heavy water is contained in the waste water A ₁ . It is.

Specifically, diethylenetriamine pentaacetic acid (Dietilen tetra amine Pentacetic (DTPA) is mixed proper amount into the waste water A ₁ as the heavy metal scavenging agent (chelator) C.

  The chemical treatment step 4 is based on an oxidation-reduction reaction of an organic substance generated by an alkaline system to which hydrogen peroxide is added, and the organic substance is decomposed here.

As shown in FIG. 5, the ratio of the heavy metal removing agent (DTPA) from the heavy metal removing agent tank 12 to the waste water A ₁ from which the solid matter (sludge) S ₁ has been removed by the first centrifuge 11 is about 0.1 wt%. Then, the waste water A ₁ is put into the stirring and mixing tank 13.

  On the other hand, 41 baume sodium silicate D is stored in the sodium silicate tank 15, and 50% sodium hydroxide (sodium hydroxide) E is stored in the caustic soda tank 16. Further, the sodium silicate D and An alkaline agent G obtained by mixing caustic soda E and water W at a volume ratio of 1: 3: 4 is prepared in the alkaline agent tank 17.

The sodium silicate D having 41Be (Baume degree 41) means sodium silicate having a specific gravity of 1.38 g / cm ³ and a weight ratio of SiO ₂ / Na ₂ O of 3.22. In addition, the sodium silicate D needs to be dissolved in the water W before being mixed with the caustic soda E.

The alkaline agent (solution) G is automatically fed into the stirring reaction tank 13 by the pump P ₁ until the PH value of the waste water A ₁ in the stirring reaction tank 13 becomes 10.8. The reason why the PH value is maintained at about 10.8 is that organic substances are most efficiently decomposed when the PH value is around 10.8.

Further, hydrogen peroxide H is sent from the hydrogen peroxide tank 18 to the stirring reaction tank 13 by the pump P ₂ .
The hydrogen peroxide is added in an amount of 1 wt% or less even if the COD value of the wastewater A ₁ is higher than 80000 mg / l. When the hydrogen peroxide H is added to the stirring reaction tank 13 and the chemical reaction starts, The PH value immediately decreases to PH = 8.

Since an extreme decrease in PH value is not desirable, a pH controller 19 is provided to avoid this, and the pH value is automatically maintained in the vicinity of 10.8 by automatically supplying the alkaline agent G. I am doing so. Also, during this chemical reaction, the precipitate resulting from the soluble substances, such as polyphenols in waste water A ₁ is formed.

In FIG. 5, reference numeral 19a denotes an electrode for detecting the PH value provided in the stirring reaction tank 13. Both pumps P ₁ and P ₂ are generated via the PH controller 19 so that the PH value is within the set range. The stop is controlled.
Further, since the chemical reaction (decomposition reaction of organic matter) in the stirring reaction tank 13 is greatly influenced by the temperature, the temperature for maintaining the temperature of the waste water A ₁ at 50 to 60 ° C. as described above. An adjusting device (not shown) is provided.

More specifically, by adding hydrogen peroxide H, in the stirred reaction tank 13,
H ₂ O ₂ + OH → OOH ⁻ + H ₂ O (1)
H ₂ O ₂ → H ₂ O + 1 / 2O ₂ (2)
It is assumed that active ionic perhydroxyl (OOH ⁻ ) is generated through this reaction, which decomposes organic matter in the wastewater A ₁ .
That is, the sodium silicate D provides an alkaline agent G as a driving force for generating a porhydroxyl group (OOH ⁻ ) and functions as a buffering agent for alleviating the decomposition of hydrogen peroxide H ₂ O _2. Is.
Further, 50% caustic soda E provides an alkaline agent G as a driving force for generating a perhydroxyl group (OOH ⁻ ).
Furthermore, hydrogen peroxide H ₂ O ₂ provides oxygen to generate ionic perhydroxyl groups (OOH ⁻ ).

The waste water A ₁ in which the organic matter in the waste water A ₁ is decomposed in the chemical treatment step 4 is subsequently subjected to a treatment for removing solids (aggregates) generated by the decomposition of the organic matter in the second centrifugal separation treatment step 5. receive. Then, at this waste water A ₂ calcium oxide addition step 6, 0.5 g / l the ratio of calcium oxide (CaO) I of (0.5 w%) was added, the insoluble material in the waste water A ₂ aggregation Is done. Then, the waste water A ₂ is supplied to the third centrifugation step 7 follows, where the solid (aggregates) are removed.

Further, wherein the third centrifugation step 7 wastewater A ₃ which solids have been removed by, is added an appropriate amount of sulfuric J In sulfuric acid addition step 8, PH wastewater A ₃ is adjusted to about 8 .

Waste water A ₃ having a pH adjusted to about 8 is used in a first filtration / adsorption process 9 using a column packed with calcium carbonate and celite (diatomaceous earth) and a second filtration / adsorption process 10 using a column charged with activated carbon. After being subjected to a removal treatment by filtration and adsorption of solids, etc., it is treated as waste water A ₄ having a clean transparent color and discharged to the outside.

FIG. 6 is a system diagram showing the arrangement of each processing apparatus for performing the chemical processing step 4 to the second filtration / adsorption processing step 10 of FIG.
Referring to FIG. 6, the waste water A ₂ from the stirring reaction tank 13 in the chemical treatment step 4 is centrifuged in the second centrifuge 21 with a centrifugal force of 3500 G for about 7.5 minutes, and the sludge S ₂ is removed.

Waste water A ₂ from the second centrifuge 21 is introduced into the insoluble compound precipitation tank 22 where calcium oxide (CaO) is fed into the waste water A ₂ from the calcium oxide tank 28 at a rate of 0.5 g / l. I is added.
By the addition of the calcium oxide (CaO) I, most of the insoluble components in the wastewater A ₂ are condensed and become solid matter.

Thereafter, the waste water A ₂ is sent to the third centrifuge 23 where the sludge S 3 is removed by centrifuging the waste water A ₂ under the same conditions as the second centrifuge 21.

Waste water A ₂ from the third centrifuge 23 is continuously sent to the pH adjusting tank 24, and by supplying sulfuric acid (H ₂ SO ₄ ) J from the sulfuric acid storage tank 29, its PH is lowered to 7.0. (Neutralized).

The waste water A ₃ from the pH adjusting tank 24 adjusted to PH 7.0 is a filler obtained by mixing calcium carbonate Ca (CO ₂ ) ₃ and celite (diatomaceous earth) at a rate of 0.5 g / l. The solid matter is removed by filtration and adsorption through the first filtration / adsorption column 25 filled with K and the second filtration / adsorption column 26 filled with activated carbon L, and the treated wastewater A ₄ is transferred to the treated water tank 27. To be recovered.

The packing material K in the first filtration / adsorption column 25 is sand formed of 300 g / l of sand on the column floor so that the flow rate of the wastewater A ₃ is not greatly limited by a large pressure drop. Ingenuity has been added to the filling structure, such as placing a floor.

In this embodiment, the Vinasasu wastewater A of COD values 60000~65000mg / l, COD value until a clear wastewater A ₄ of 2000~3000mg / l, was able to process.

FIG. 7 shows the appearance of the waste water A (Vinousus) before treatment, and FIG. 8 is a photograph of the appearance of the treated waste water A ₄ of the waste water A. As can be seen from FIG. 7 and FIG. 8, according to the present invention, waste water A containing high-concentration pollutants from a distilled liquor production facility or the like using alcohol fermentation by a relatively simple waste water treatment method can be quickly and It becomes possible to process at low cost.

  The present invention can be applied not only to distilled liquor production equipment but also to any industrial equipment that uses equipment equipped with an alcohol fermentation process.

It is a treatment process figure of the wastewater which came out of the distilled liquor manufacturing facility by this invention. It is a diagram which shows the relationship between the centrifugal separation force G at the time of isolate | separating the solid substance in the wastewater A with a centrifuge, the processing time t, and the pollution unit NTD. It is a diagram which shows the relationship between the coagulant | flocculant density | concentration in waste water A, and the pollution unit NTU when the separation process is performed for 7.5 minutes with the centrifugal force of 3300G. It is a diagram which shows the relationship between the temperature of the wastewater A with a flocculent density | concentration of 100 ppm, and the pollution unit NTU when the separation process is performed for 7.5 minutes by centrifugation of 2500G. It is an arrangement | positioning systematic diagram of each processing apparatus for implementing from the flocculant addition process 1 of FIG. 1 to the chemical treatment process 4. FIG. It is a systematic diagram which shows arrangement | positioning of each processing apparatus for implementing from the chemical treatment process 4 of FIG. 1 to a 2nd adsorption treatment process. It shows the external appearance of waste water A discharged from a tequila manufacturing facility in Attorico, Mexico. It shows the appearance of the treated waste water A ₄ after processing wastewater A in FIG.

Explanation of symbols

A · · processed wastewater A ₁ to A ₃ · · wastewater A ₄ · · treated wastewater B · · polyglutamic acid crosslinked product coagulant mainly of (PGα21Ca)
C. Heavy metal remover (chelating agent)
S _{1 to} S ₃ .. Sludge (aggregation / solid matter)
D · · · 41Be sodium silicate E · · 50% sodium hydroxide (50% sodium hydroxide)
F. Factory G. Alkaline H. Hydrogen peroxide I. Calcium oxide (CaO)
J ・ ・ Sulfuric acid (H ₂ SO ₄ )
K ... Filler (calcium carbonate + diatomaceous earth)
L ・ ・ Activated carbon W ・ ・ Water P ₁ ~ P ₄・ ・ Pump 1 ・ ・ Flocculant addition process 2 ・ ・ First centrifugal separation process 3 ・ ・ Heavy metal removal agent addition process 4 ・ ・ Chemical treatment process 5 ・ ・Centrifugation step 6 ··· Calcium oxide addition step ··· Third centrifugation step 8 · · Sulfuric acid addition step 9 · · First adsorption step 10 · · Second adsorption step 11 · · First centrifuge (centrifugal dehydrator )
12 .. Heavy metal removal agent tank (chelating agent tank)
13. · Stirring reaction tank 14 ·· Flocculant tank 15 ·· Sodium silicate tank 16 ·· Caustic soda (sodium hydroxide) tank 17 ·· Alkaline agent tank 18 ·· Hydrogen peroxide tank 19 ·· PH controller 19a ·· Electrode 20, Water tank 21, Second centrifuge 22, Precipitation tank 23, Third centrifuge 24, PH adjustment tank 25, First filtration, Adsorption column 26, Second filtration, Adsorption column 27..Processed water tank 28..Calcium oxide tank (CaO tank)
29. ・ Sulfuric acid storage tank (H ₂ SO ₄ tank)

Claims (11)

  Adding a coagulant to the waste water, adding a coagulant to the waste water, a first centrifugation step for removing solids in the waste water from the coagulant addition step, and adding an alkali agent and hydrogen peroxide to the waste water from the centrifugation step; A chemical treatment step for decomposing organic matter in the wastewater, a second centrifugal separation step and a third centrifugal separation step for removing solid matter in the wastewater from the chemical treatment step, and a purification treatment of the wastewater from the third centrifugal separation step A method for purifying wastewater from a distilled liquor manufacturing facility, comprising a first filtration / adsorption step and a second filtration / adsorption step for purifying wastewater from the first filtration / adsorption step.   The method for purifying wastewater from a distilled liquor manufacturing facility according to claim 1, wherein the flocculant adding step is performed by mixing the flocculant mainly composed of a polyglutamic acid crosslinked product with the wastewater.   The method for purifying wastewater discharged from a distilled liquor manufacturing facility according to claim 2, wherein the amount of the flocculant added in the flocculant addition step is such that the concentration of the flocculant in the wastewater is 120 ppm to 150 ppm.   The first centrifugal separation step of the waste water from the flocculant addition step is a centrifugal separation step for treating the waste water at a waste water temperature of 40 to 60 ° C., a centrifugal separation force of 2500 to 3500 g, and a centrifugal separation time of 6 to 8 minutes. A method for purifying wastewater discharged from a distilled liquor manufacturing facility according to Item 1. A heavy metal removal agent addition step is added between the centrifugal separation step and the chemical treatment step to add diethylenetriaminepentaacetate (DIETHYLENETRIAMEPENTAACEATE / DTPA) in an amount of 1 wt% in the wastewater as a heavy metal removal agent in the wastewater. A method for purifying wastewater discharged from the distilled liquor manufacturing facility according to claim 1.   In the chemical treatment process, hydrogen peroxide, sodium silicate, caustic soda and water are mixed with an alkali agent solution in the waste water, and the pH value of the waste water is automatically adjusted to about 9 to 11 by stirring and mixing. The method for purifying wastewater discharged from a distilled liquor manufacturing facility according to claim 1, wherein a chemical treatment step is performed for decomposing organic substances in the wastewater while maintaining the temperature at 40 to 60 ° C.   The wastewater discharged from the distilled liquor manufacturing facility according to claim 1, wherein a calcium oxide addition step is added to the wastewater from the second centrifugal separation step to add calcium oxide in an amount such that the concentration in the wastewater is 0.5 wt%. Purification treatment method.   The distilled liquor manufacturing facility according to claim 1, wherein the second centrifugal separation step and the third centrifugal separation step are centrifugal separation steps for treating wastewater with a centrifugal force of 2500 to 3500G and a centrifugal separation time of 6 to 8 minutes. Purification method of waste water from   The wastewater discharged from the spirits production facility according to claim 1, wherein a sulfuric acid addition step is provided in which wastewater from the third centrifugal separation step is added with sulfuric acid to adjust the PH value of the wastewater to approximately 7.0. Purification treatment method.   The first filtration / adsorption step is a purification treatment method of wastewater discharged from a distilled liquor manufacturing facility according to claim 1, wherein the first filtration / adsorption step is a filtration / adsorption step using a column packed with calcium carbonate and diatomaceous earth as an adsorbent.   The method for purifying wastewater discharged from a distilled liquor production facility according to claim 1, wherein the second filtration / adsorption step is a filtration / adsorption step using a column filled with activated carbon as a filtration / adsorbent.