KR102097384B1 - Method for purification of waste organic solvent - Google Patents

Abstract

The method for purifying the waste organic solvent of the present invention is a first purification step in which sodium hypochlorite (NaOCl) is mixed in a waste organic solvent, and a second purification in which potassium carbonate (K ₂ CO ₃ ) is mixed in the first purified waste organic solvent. Including the step, the transparency is high, and the removal efficiency of impurities such as metal components and organic substances is excellent.

Description

METHOD FOR PURIFICATION OF WASTE ORGANIC SOLVENT

The present invention relates to a method for purifying waste organic solvents. Specifically, the present invention includes a first purification step of mixing sodium hypochlorite (NaOCl) in a waste organic solvent and a second purification step of mixing potassium carbonate (K ₂ CO ₃ ) in the first purified waste organic solvent. Accordingly, the present invention relates to a method for purifying a waste organic solvent, which increases the transparency of the waste organic solvent and is excellent in removing impurities such as metal components and organic substances.

The organic solvent refers to a carbon compound (hydrocarbon, alcohol, ether, amine, acetone, etc.) that dissolves and extracts the target substance but does not react with the target substance, such as textile manufacturing, paper product manufacturing, rubber product and plastic product manufacturing, And in a variety of fields, such as high pressure liquid chromatography, a large amount of organic solvents are used, and the quantity and price are gradually increasing.

Therefore, for product price competitiveness, recovery through purification of the waste organic solvent generated during product manufacturing is important. In general, various methods have been tried as a method of removing impurities in the waste organic solvent, but there is a problem in that the removal efficiency of inorganic metal impurities such as organic impurities and metal chlorides is low or the turbidity is high, making reuse difficult.

Accordingly, there is a need for a method for purifying a waste organic solvent that can increase the transparency of the waste organic solvent and is excellent in removing impurities such as metal components and organic substances.
Prior art in this regard is disclosed in Korean Patent Publication No. 10-1999-0044760.

An object of the present invention is to provide a waste organic solvent purification method that can increase the transparency of the waste organic solvent.

Another object of the present invention is to provide a method for purifying a waste organic solvent, which is excellent in removing impurities such as metal components and organic substances of the waste organic solvent.

The above and other objects of the present invention can be achieved by the present invention described below.

One aspect of the present invention relates to a method for purifying waste organic solvents.

According to one embodiment, the method for purifying the waste organic solvent is a primary purification step of mixing sodium hypochlorite (NaOCl) with the waste organic solvent, and potassium carbonate (K ₂ CO ₃ ) is mixed with the primary purified waste organic solvent. And a second purification step.

In addition, the sodium hypochlorite (NaOCl) may be included in 1 to 5 parts by weight based on 100 parts by weight of the waste organic solvent, and the potassium carbonate (K ₂ CO ₃ ) is 1 to 5 parts per 100 parts by weight of the waste organic solvent It may be included in parts by weight.

In another embodiment, the method for purifying the waste organic solvent is triethyl amine by adding 1 to 5 parts by weight of triethylamine (TEA) to 100 parts by weight of the waste organic solvent after mixing sodium hypochlorite (NaOCl). After generating the amine hydrochloride, the method may further include aggregating the triethylamine hydrochloride by adding 1 to 5 parts by weight of the coagulation composition.

In another embodiment, the method of purifying the waste organic solvent is performed by mixing 1 to 5 parts by weight of triethylamine (TEA) with respect to 100 parts by weight of the waste organic solvent after mixing sodium hypochlorite (NaOCl). Ethylamine hydrochloride is generated, 1 to 5 parts by weight of zinc oxide (ZnO) is added to adsorb the chlorine compound, and then 1 to 5 parts by weight of the coagulation composition is added to aggregate the triethylamine hydrochloride or zinc oxide adsorbed with chlorine compound. It may further include a step.

In addition, the coagulant composition includes an aluminum-based coagulant and an iron salt-based coagulant, the aluminum-based coagulant includes aluminum sulfate or polyaluminum chloride, and the iron-based coagulant is ferrous chloride, ferric chloride, polychloride, Ferrous sulfate, ferric sulfate, and poly iron sulfate.

In addition, the coagulant composition may be mixed in an aluminum-based coagulant and iron salt-based coagulant in a weight ratio of 1: 1 to 5: 1.

In another embodiment, the waste organic solvent may further include a pretreatment step of contacting the ion exchange resin.

In addition, the pre-treatment step may further include a step of contacting the zeolite 4A after the waste organic solvent contacts the ion exchange resin.

The present invention has an effect of providing a method for purifying a waste organic solvent that can increase the transparency of the waste organic solvent and has excellent removal efficiency of impurities such as metal components and organic substances.

Hereinafter, the present invention will be described in more detail.

In describing the present invention, when it is determined that detailed descriptions of related known technologies may unnecessarily obscure the subject matter of the present invention, detailed descriptions thereof will be omitted.

When 'include', 'have', 'consist of', etc. mentioned in this specification are used, other parts may be added unless '~ man' is used. When a component is expressed as a singular number, the plural number is included unless otherwise specified.

In addition, in analyzing the components, it is interpreted as including an error range even if there is no explicit description.

In addition, in this specification, 'X to Y' representing a range means 'X or more and Y or less'.

Waste organic solvent purification method

Hereinafter, the method for purifying the waste organic solvent of the present invention will be described in detail.

According to one embodiment, the method for purifying the waste organic solvent is a primary purification step of mixing sodium hypochlorite (NaOCl) with the waste organic solvent, and potassium carbonate (K ₂ CO ₃ ) is mixed with the primary purified waste organic solvent. And a second purification step.

The present invention has the advantage of excellent removal efficiency of impurities such as metal components and organic substances by including a primary purification step of mixing sodium hypochlorite (NaOCl) in a waste organic solvent. Since sodium hypochlorite (NaOCl) has strong oxidizing power, it can perform the function of purifying the waste organic solvent through oxidation, bleaching, and decomposition.

In an embodiment, the sodium hypochlorite (NaOCl) can be used with an appropriate amount of water (H ₂ O) and / or ceramic catalyst. The ceramic catalyst may be a mecasera catalyst containing a ferrite magnetic material, and the mechacera catalyst may be used in a mixing ratio of white catalyst: black catalyst: brown catalyst in the range of 30 to 45: 10 to 25: 30 to 45 by weight. . Specifically, the white catalyst may include a ferrite magnetic material, zirconia (ZrO2), titanium (Ti), barium oxide (BaO), and diatomaceous earth, and the black catalyst may include a ferrite magnetic material, iron (Fe). , Manganese (Mn), cobalt (Co), titanium (Ti), magnesium (Mg), aluminum (Al), and potassium (K), and the Brown catalyst is ferrite (ferrite) magnetic material, iron (Fe), Manganese (Mn), cobalt (Co), titanium (Ti), magnesium (Mg), aluminum (Al), potassium (K), and zirconium (Zr).

The water (H ₂ O) and the ceramic catalyst may be included in 0.1 to 3 parts by weight based on 100 parts by weight of the waste organic solvent. In the above content range, the efficiency of refining the waste organic solvent may be maximized.

The sodium hypochlorite (NaOCl) may be included in 1 to 5 parts by weight, specifically 2 to 4 parts by weight based on 100 parts by weight of the waste organic solvent. In the above-mentioned content range, chlorine-based impurities can be minimized while the purification efficiency of the waste organic solvent is excellent.

In addition, the present invention includes a second purification step of mixing potassium carbonate (K ₂ CO ₃ ) with the primary purified waste organic solvent, while further improving the purification efficiency of the waste organic solvent and improving the transparency of the waste organic solvent. Can be improved. The potassium carbonate (K ₂ CO ₃ ) is capable of removing impurities due to a surface active effect, and is particularly excellent in improving the transparency of the waste organic solvent.

The potassium carbonate (K ₂ CO ₃ ) may be included in 1 to 5 parts by weight, specifically 2 to 4 parts by weight based on 100 parts by weight of the waste organic solvent. In the above content range, the purification efficiency of the waste organic solvent is excellent, but the effect of improving the transparency of the waste organic solvent is excellent.

In an embodiment, the sodium hypochlorite (NaOCl) and potassium carbonate (K ₂ CO ₃ ) may be included in the waste organic solvent in a weight ratio of 0.5: 1 to 2: 1. In the weight ratio range, the balance of improving purification efficiency and transparency is excellent.

In the present invention, the waste organic solvent means an organic solvent that has been used, and may mean, for example, hydrocarbon, alcohol, ether, amine or acetone. Specifically, the method for purifying the waste organic solvent of the present invention may be particularly effective in purifying acetone.

In another embodiment, the method of purifying the waste organic solvent is a step of mixing sodium hypochlorite (NaOCl), and then adding triethylamine (TEA) to produce triethylamine hydrochloride, and then adding the coagulation composition to the tree. The method may further include agglutinating the ethylamine hydrochloride salt.

The triethylamine (TEA) is highly reactive with chlorine or chlorine ions, and thus can produce triethylamine hydrochloride. Thus, the method for purifying the waste organic solvent of the present invention has an effect of effectively removing chlorine-based impurities such as chlorine, chlorine ions, or chlorine compounds that are contained in the waste organic solvent or may be generated by applying sodium hypochlorite (NaOCl). have.

Specifically, a specific reaction mechanism in which triethylamine hydrochloride is produced can be exemplified by the following chemical reaction formula 1.

[Chemical Reaction Formula 1]

The triethylamine hydrochloride is highly soluble in an aqueous solution, but is present as an insoluble chlorine compound in a waste organic solvent, and thus can be selectively removed by collecting chlorine or chlorine ions.

The triethylamine (TEA) may be added in 1 to 5 parts by weight, specifically 2 to 4 parts by weight, based on 100 parts by weight of the waste organic solvent. In the above content range, the efficiency of removing chlorine impurities in the waste organic solvent may be maximized.

The step of agglomeration by introducing the agglomeration composition is a process of agglomeration and trituration of triethylamine hydrochloride particles.

Specifically, the coagulation composition may include an aluminum-based flocculant and an iron salt-based flocculant. The aluminum-based coagulant includes aluminum sulfate or polyaluminum chloride, and the iron-based coagulant is at least one of ferrous chloride, ferric chloride, poly iron chloride, ferrous sulfate, ferric sulfate, and poly iron sulfate. It may include.

In addition, the cohesive composition may be a mixture of aluminum-based coagulant and iron salt-based coagulant in a weight ratio of 1: 1 to 5: 1, specifically, 1.5: 1 to 2.5: 1. In the weight ratio range, it is possible to exhibit excellent aggregation speed and aggregation effect.

The particles agglomerated by the coagulation composition grow into particles capable of gravity precipitation of 25 to 40 μm, and thus particles can be easily removed. The chlorine compound particles precipitated by the gravity precipitation can be removed by reduced pressure or pressure filtration or natural sedimentation.

The coagulation composition may be added in 1 to 5 parts by weight, specifically 2 to 4 parts by weight with respect to 100 parts by weight of the waste organic solvent. In the above content range, the efficiency of removing chlorine impurities in the waste organic solvent may be maximized.

In another embodiment, the method of purifying the waste organic solvent after the step of mixing sodium hypochlorite (NaOCl), triethylamine (Triethylamine, TEA) is added to generate triethylamine hydrochloride, and zinc oxide (ZnO) is added. After injecting and adsorbing the chlorine compound, the agglomeration composition may be introduced to further include aggregating triethylamine hydrochloride or zinc oxide adsorbed with the chlorine compound.

As described above, triethylamine (TEA) has high reactivity with chlorine or chlorine ions to generate triethylamine hydrochloride, and zinc oxide (ZnO) is used for adsorption and removal of chlorine compounds contained in waste organic solvents. It works.

The production mechanism of the triethylamine hydrochloride is as described above, and the zinc oxide (ZnO) is not particularly limited, but in view of the adsorption performance of the chlorine compound, a specific surface area (bet) of 20 to 100 m ² / g, specifically 3 to 80 m ² / g, more specifically 40 to 70 m ² / g can be used. Here, the specific surface area represents the average specific surface area obtained based on the adsorption isotherm of BET (Brunauer, Emmett, Teller).

The zinc oxide can be obtained by firing zinc hydroxide, zinc carbonate, basic zinc carbonate and the like at 350 to 400 ° C. The zinc hydroxide, zinc carbonate, basic zinc carbonate, etc. may be crystallized in an aqueous solution, for example, zinc carbonate precipitated in an aqueous solution of ammonium zinc carbonate, zinc hydroxide obtained by a uniform precipitation method, or the like may be used.

The reaction mechanism in which the zinc oxide adsorbs the chlorine compound can be exemplified by the following chemical reaction formula 2.

[Chemical Reaction Formula 2]

The zinc oxide may be added in 1 to 5 parts by weight, specifically 2 to 4 parts by weight with respect to 100 parts by weight of the waste organic solvent. In the above content range, the efficiency of removing chlorine impurities in the waste organic solvent may be maximized.

The step of agglomeration by incorporating the coagulation composition is a process of agglomeration and enlarging zinc oxide particles adsorbed with triethylamine hydrochloride or chlorine compounds. It may be substantially the same as the step of agglomeration, including the agglomeration composition described in the other embodiments, except that the zinc oxide particles adsorbed chlorine compound are aggregated together. Specifically, the particles aggregated by the agglomeration composition can be easily removed because they grow into particles capable of gravity precipitation of 25 to 40 μm. The chlorine compound particles precipitated by the gravity precipitation can be removed by reduced pressure or pressure filtration or natural sedimentation.

In another embodiment, the waste organic solvent may further include a pretreatment step of contacting the ion exchange resin.

The ion-exchange resin has an effect of removing certain metal components and organic substances contained in the waste organic solvent, has an excellent removal efficiency compared to other adsorbents, and has the advantage of preventing re-elution of the metal components.

Specifically, the ion exchange resin is greatly cationic resin (counter ion (counter ion) a cation and (SO ₃ ^- H ^+), separating the cation) and an anion resin (the counter ion (counter ion) anion and (N ⁺ OH ^- ), Separated anions). Since the metal component to be removed among impurities contained in the waste organic solvent is composed of a metal component of the cation, a cation ion exchange resin is suitable. As a cationic ion exchange resin suitable for this, in the present invention, Trilite SCR-B (manufactured by Iontech Co., Ltd.) can be used, which is a state in which a sulfate group is exchanged with styrene-divinylbenznene as a basic matrix. The ion exchange resin is mainly injected into the column with an average particle size of 0.4 mm (particle size distribution 0.3 to 1.2 mm) to continuously inject waste organic solvent to be purified on the top of the column to recover the continuously purified waste organic solvent to the bottom of the column. Method. Therefore, the flow rate of recovered acetone injected per gram of ion-exchange resin injected into the column is a process variable in the range of 10 to 100 cc / min ㆍ g (unit: flow rate of recovered acetone per g of ion-exchange resin), and the waste organic When the flow rate of the solvent is less than 10 cc / min · g, the flow rate is too small to cause channeling when passing through the column, which may degrade ion exchange capacity, and when the flow rate exceeds 100 cc / min · g The flow rate is so large that the contact time with the ion exchange resin is small, so the efficiency of removing impurities may be reduced.

In addition, the pre-treatment step may further include a step of contacting the zeolite 4A after the waste organic solvent contacts the ion exchange resin.

The zeolite 4A removes metal components such as Al, Zn, Sn, Cu, and Ba, which may be eluted in a process in which the waste organic solvent is in contact with the ion exchange resin, and moisture that may be generated by the ion exchange resin, and removes organic substances. It can be removed completely. This can be distilled in a batch-type packed distillation tower containing zeolite 4A, specifically, the batch-type distillation column can use a distillation column made of 30 to 40 stages of glass. For distillation stage, a distillation column type containing a glass packing material may be used. The operation of the batch-type distillation column is performed by adjusting the distillation temperature and adjusting the reflux ratio based on the boiling point of the waste organic solvent to be distilled at normal pressure (for example, the waste acetone has a boiling point of 56 ° C). That is, the distillation temperature is good for distillation up to the boiling point of the waste organic solvent, but the concentration of impurities increases and the temperature of the waste organic solvent must be manipulated beyond this boiling point to increase the recovery amount of the waste organic solvent. That is, a distillation temperature of about 5 to 25 ° C higher than the boiling point is appropriate, and if it is less than that range, the amount of waste organic solvent recovered is too small, and when it exceeds the range, some impurities with a high boiling point are also distilled and purified. There is a problem in that the purity is low because it is mixed with the waste organic solvent. In addition, the reflux ratio of the distillation column needs to be adjusted in an appropriate ratio for separation of the organic material of the similar component and the waste organic solvent by distillation, and the conditions of 2 to 6 are suitable for this. That is, when the reflux ratio exceeds 6, the purity of the waste organic solvent obtained by distillation may increase, but the amount of reflux into the distillation column is too large than the amount of purified waste organic solvent separated from the top by distillation, so it takes time to distill. If it takes too long to maintain the temperature for a long time, components such as aldehydes among the impurities are decomposed by heat, and there is a problem in that the concentration of impurities can be increased by some reaction with impurities. In addition, when the reflux ratio is too low, the purity of the waste organic solvent decreases. When the reflux ratio is less than 2, there is a problem that the purity of the separated purified waste organic solvent rapidly decreases, and thus impurities are not easily removed.

In order to remove water from the distillation column, zeolite 4A is filled with 1 to 5 parts by weight based on 100 parts by weight of the waste organic solvent, and when the amount of zeolite 4A is less than 1 part by weight, it is difficult to remove the desired amount of moisture, and 5 weight In case of exceeding the amount, it removes moisture as well as adsorbs a part of the waste organic solvent and is inefficient because more heat is required when heating the distillation column. Water can be effectively removed by including the zeolite 4A in a distillation column.

Hereinafter, the configuration and operation of the present invention through a preferred embodiment of the present invention will be described in more detail. However, this is provided as a preferred example of the present invention and cannot be interpreted as limiting the present invention by any means.

The contents not described here will be sufficiently technically inferred by those skilled in the art, and thus the description thereof will be omitted.

Example

The waste organic solvent used in Examples and Comparative Examples used waste acetone, and the specifications of the waste acetone are as follows.

Waste acetone: inorganic metal impurities such as Ca 0.12 ppm, Fe 40.65 ppm, K 0.29 ppm, Mg 0.06 ppm, Mn 11.6 ppm, Co 10.41 ppm, Cd 3.3 ppm, Sn 0.48 ppm, Cu 3.5 ppm and Al 0.52 ppm, Contains 0.39% moisture, UV absorbance when analyzed by UV spectroscopy (UV spectroscopy) was 1.79 at a wavelength of 330 nm, 0.84 at a wavelength of 350 nm to 400 nm, and contained 20 ppm of polychlorinated biphenyls (PCBs). . Inorganic metal impurities were calculated by ICP-MS (Inductively coupled pasma-atomic emission spectrometer) analysis.

Example 1

After 3 parts by weight of sodium hypochlorite (NaOCl) was mixed with 100 parts by weight of waste acetone, 3 parts by weight of potassium carbonate (K ₂ CO ₃ ) was added and stirred sufficiently.

Example 2

After mixing 3 parts by weight of sodium hypochlorite (NaOCl) in 100 parts by weight of waste acetone, 3 parts by weight of triethylamine (TEA) is added to produce triethylamine hydrochloride, 2 parts by weight of aluminum sulfate as a coagulant and 1 part of poly iron chloride After adding the part, the resulting agglomerate was allowed to stand for about 1 hour to settle naturally by gravity. The precipitated waste acetone was filtered using a filtration filter, and 3 parts by weight of potassium carbonate (K ₂ CO ₃ ) was added and stirred sufficiently.

Example 3

After mixing 3 parts by weight of sodium hypochlorite (NaOCl) in 100 parts by weight of waste acetone, 3 parts by weight of triethylamine (TEA) is added to generate triethylamine hydrochloride, and zinc oxide (ZnO) having a specific surface area of 45 m ² / g. ) 3 parts by weight was added. After adding 2 parts by weight of aluminum sulfate and 1 part by weight of polyiron chloride as a coagulant, the resultant aggregate was allowed to stand for about 1 hour to settle naturally by gravity. The precipitated waste acetone was filtered using a filtration filter, and 3 parts by weight of potassium carbonate (K ₂ CO ₃ ) was added and stirred sufficiently.

Example 4

50 cc / min of waste acetone as a pretreatment process into a styrene-divinylbenzene-based cation resin ion exchange resin column (diameter 1/2 inch, height 1 m, 1200 cm ³ capacity, ion exchange resin Trilite SCR-B 1000 g injection) While g was injected into the top of the column, the first pretreated waste acetone was obtained from the bottom of the column. Subsequently, a 30-stage batch filling distillation column containing a glass material was continuously injected, and 3 parts by weight of zeolite 4A with respect to 100 parts by weight of waste acetone was injected into the distillation column to distill at a distillation temperature of 70 ° C and a reflux ratio of 3. Distillation was performed until 90% of the initial injection amount was distilled, and the recovery rate of waste acetone obtained through purification was 85% as a result of calculating the amount obtained after distillation based on the initial injection amount. Was.

The obtained waste acetone is based on 100 parts by weight again, and after mixing 3 parts by weight of sodium hypochlorite (NaOCl), 3 parts by weight of triethylamine (TEA) is added to generate triethylamine hydrochloride, and the specific surface area is 45 m ² / 3 parts by weight of g zinc oxide (ZnO) was added. After adding 2 parts by weight of aluminum sulfate and 1 part by weight of polyiron chloride as a coagulant, the resultant aggregate was allowed to stand for about 1 hour to settle naturally by gravity. The precipitated waste acetone was filtered using a filtration filter, and 3 parts by weight of potassium carbonate (K ₂ CO ₃ ) was added and stirred sufficiently.

Comparative Example 1

The waste acetone was treated in the same manner as in Example 1, except that sodium hypochlorite (NaOCl) was not mixed.

Comparative Example 2

The waste acetone was treated in the same manner as in Example 1, except that potassium carbonate (K ₂ CO ₃ ) was not added.

Example Comparative example One 2 3 4 One 2 Pretreatment Not performed Not performed Not performed Perform Not performed Not performed Sodium hypochlorite 3 3 3 3 0 3 Potassium carbonate 3 3 3 3 3 0 Triethylamine 0 3 3 3 0 0 Zinc oxide 0 0 3 3 0 0 Aluminum sulfate 0 2 2 2 0 0 Poly iron chloride 0 One One One 0 0

Measurement method

(1) Inorganic metal impurities (ppm): The waste acetone of Examples and Comparative Examples was measured by ICP-MS analysis, and the content of inorganic metal impurities was shown in Table 2 below.

(2) UV absorbance: UV absorbance at 330 nm and 350 nm to 400 nm was measured by ultraviolet spectroscopy of waste acetones of Examples and Comparative Examples, and shown in Table 2 below.

(3) Chlorine concentration (ppm): The waste acetone of Examples and Comparative Examples was measured by a diethyl-p-phenylenediamine (DPD) color development method, and is shown in Table 2 below.

Before processing Example Comparative example One 2 3 4 One 2 ICP-MS analysis (ppb) Ca 120 8 7 8 6 82 17 Fe 40650 13 14 11 7 3252 45 K 290 5 4 5 0.87 235 18 Mg 60 12 15 10 6 50 30 Mn 11600 3 3 3.5 One 975 19 Co 10410 2 3 2 One 897 13 CD 3300 10 11 9 0.5 2904 32 Sn 480 8 9 5 1.2 442 45 Cu 3500 3.4 6 3 0.8 3288 13 Al 520 17 11 14 9 348 55 UV absorbance 330nm 1.79 0.7679 0.7538 0.7398 0.8384 1.1892 1.3038 350nm ~ 400nm 0.84 0.0065 0.0063 0.0060 0.0068 0.2247 0.4542 Chlorine concentration (ppm) 37 4.732 0.2865 0.2157 0.234 8.952 7.550

As shown in Table 2, in the case of purification by the method for purifying the waste organic solvent of the present invention, not only is the removal efficiency of metal components and organics excellent, but also the transparency is improved, while sodium hypochlorite is not treated as in Comparative Example 1 In particular, it can be seen that the removal efficiency and transparency of metal components and organic substances are lowered, or the transparency is particularly low when potassium carbonate is not treated as in Comparative Example 2.

Although the embodiments of the present invention have been described above, the present invention is not limited to the above embodiments, and may be manufactured in various different forms, and those skilled in the art to which the present invention pertains have technical spirit of the present invention. However, it will be understood that other specific forms may be practiced without changing essential features. Therefore, it should be understood that the embodiments described above are illustrative in all respects and not restrictive.

Claims (6)

A pretreatment step of contacting the waste organic solvent with an ion exchange resin;
A primary purification step of mixing 3 to 5 parts by weight of sodium hypochlorite (NaOCl) with respect to 100 parts by weight of the waste organic solvent; And
A second purification step of mixing 3 to 5 parts by weight of potassium carbonate (K ₂ CO ₃ ) in the primary purified waste organic solvent;
Waste organic solvent purification method comprising a,
In the method for purifying the waste organic solvent, after mixing sodium hypochlorite (NaOCl), 2 to 4 parts by weight of triethylamine (TEA) is added to 100 parts by weight of the waste organic solvent to produce triethylamine hydrochloride, , Zinc oxide (ZnO) 1 to 5 parts by weight to adsorb the chlorine compound, and then 2 to 4 parts by weight of the aggregation composition to agglomerate zinc oxide adsorbed with triethylamine hydrochloride or chlorine compound; ,
The flocculation composition is a method for purifying waste organic solvent, in which aluminum-based flocculant and iron salt-based flocculant are mixed in a weight ratio of 1.5: 1 to 2.5: 1.
delete delete delete delete According to claim 1,
The pretreatment step further comprises a step of contacting the zeolite 4A after the waste organic solvent contacts the ion exchange resin.