CN218931898U - Device for reducing TOC (total organic carbon) of epoxy resin high-salt organic wastewater - Google Patents
Device for reducing TOC (total organic carbon) of epoxy resin high-salt organic wastewater Download PDFInfo
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Abstract
The utility model discloses a device method for reducing TOC (total organic carbon) of epoxy resin high-salt organic wastewater, which consists of a pH value adjusting tank, a benzene ring compound adsorption bed, an oxidation reactor, a carboxyl compound adsorption bed and a deep oxidation reactor. Through the steps of adsorption removal of benzene-containing ring compounds, selective oxidation and adsorption removal of carbon three compounds and deep oxidation, the consumption of an oxidant can be reduced to the greatest extent, the wastewater treatment cost is reduced, and meanwhile, refined brine with TOC less than 10mg/L is obtained, so that the requirements of ionic membrane electrolysis brine can be met.
Description
Technical Field
The utility model belongs to the technical field of wastewater treatment, and particularly relates to a device for reducing TOC (total organic carbon) of epoxy resin high-salt organic wastewater.
Background
In order to separate the sodium chloride from the resin, a water-soluble method is often adopted to separate the sodium chloride from the resin, so that a large amount of high-salt organic wastewater is produced. The wastewater has very complex components and comprises the following main components: (1) The organic material is mainly macromolecular intermediate products, a small amount of raw materials which are not completely reacted, toluene which is an organic solvent, ageing resin and the like in the production process of the epoxy resin; (2) Ions such as Na + 、Cl - 、OH - Etc., derived from the production raw materials and by-products of the reaction. Because the organic pollutant content of the waste water is high (TOC can reach 20000mg/L, and most of the organic matters are substances which are difficult to oxidize such as epoxy resin molecules, benzene series, phenol compounds and the like) and the salt content is high (8-20%), the waste water is difficult to thoroughly remove by adopting a conventional treatment method, and meanwhile, the waste water treatment cost is high, and the treatment of the waste water in the epoxy resin production becomes a prominent problem in the epoxy resin industry.
In order to solve the problem of treating high-salt organic wastewater, patent CN102689975B discloses a high-salt wastewater recycling treatment technology, which uses Fe 2+ (or Fe) 2+ And Cu 2+ ) As the catalyst, hydrogen peroxide is used as an oxidant, organic pollutants in the high-salt wastewater are oxidized and degraded, TOC of the high-salt wastewater can be reduced to 200mg/L, but the catalyst used in the method is discharged in the form of iron-containing sludge after the reaction is finished, so that the treatment cost is very high, and the risk of secondary pollution is high. Patent CN104925997B discloses a catalyst which can be recycled and is high in saltThe method for recycling the wastewater comprises the steps of using Cu under the conditions that the temperature is 50-95 ℃ and the pH value is 4-6 2+ The catalyst and the hydrogen peroxide are used as oxidants, so that the TOC content in the epoxy resin high-salt wastewater can be reduced to 100-200mg/L, the catalyst is recycled by acid dissolution after neutralization, precipitation and separation, and harmless disposal of the waste catalyst is avoided. Patent CN105645634A discloses a method for treating epoxy resin synthetic wastewater, namely, under the conditions of 200-300 ℃ and 2-10MPa, copper, manganese, nickel, ruthenium, rhodium and palladium are used as catalysts, oxygen is used as an oxidant to perform catalytic wet oxidation reaction, then precipitation and filtration are performed, and the filtrate is subjected to adsorption treatment, so that electrolytic brine with the organic matter content lower than 10mg/L can be obtained, but the method has the problems of severe reaction conditions and high equipment investment and operation cost.
As can be seen, the TOC value of the epoxy resin high-salt organic wastewater is difficult to be reduced to below 10mg/L in an economical and efficient method in the prior art.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model provides a classification treatment process for the wastewater in the production of epoxy resin, which can efficiently remove organic matters and reduce the TOC value of the wastewater to below 10 mg/L.
The technical scheme of the utility model is as follows:
a device for reducing TOC of epoxy resin high-salt organic wastewater consists of a pH value adjusting tank, a benzene ring compound adsorption bed, a structure conversion oxidation reactor, a carboxyl compound adsorption bed and a deep oxidation reactor, and is characterized in that: the pH value adjusting tank is connected with the epoxy resin production wastewater and the hydrochloric acid feed inlet, the outlet of the pH value adjusting tank is connected with the benzene ring compound adsorption bed, the outlet of the benzene ring compound adsorption bed is connected with the structure conversion oxidation reactor, the outlet of the structure conversion oxidation reactor is connected with the carboxyl compound adsorption bed, and the outlet of the carboxyl compound adsorption bed is connected with the deep oxidation reactor.
The devices are connected through a pipeline or a pipeline and a pump.
The benzene ring compound adsorption bed is 1 or more; in the case of a plurality of adsorbent beds, the adsorbent beds are in a series mode or a parallel mode, and the adsorbent is filled in the adsorbent beds.
The number of the carboxyl compound adsorption beds is 1 or more, and in the case of a plurality of adsorption beds, the adsorption beds are in a series mode or a parallel mode, the adsorption beds are filled with adsorbents, and the adsorbents are polystyrene ion exchange resins.
The device for reducing TOC of the epoxy resin high-salt organic wastewater is also provided with a raw material tank and a refined brine tank.
The raw material tank is connected with the pH value adjusting tank through a raw material pump.
The outlet of the pH value adjusting tank is connected with the inlet of the pump at the bottom of the pH value adjusting tank, and the outlet of the pump at the bottom of the pH value adjusting tank is connected with the benzene ring compound adsorption bed.
The outlet of the benzene ring compound adsorption bed is connected with the inlet of the bottom pump of the structure conversion oxidation reactor, and the outlet of the bottom pump of the structure conversion oxidation reactor is connected with the carboxyl compound adsorption bed.
The outlet of the deep oxidation reactor is connected with the inlet of a refined brine pump, and the outlet of the refined brine pump is connected with a refined brine tank.
A method for reducing TOC of epoxy resin high-salt organic wastewater, comprising the following steps:
s1: adjusting the pH value of the epoxy resin production wastewater to 2-4 by using hydrochloric acid, and then sending the wastewater into an adsorption bed to remove benzene ring compounds in the wastewater;
s2: the wastewater which is absorbed and removed by the step S1 and contains benzene ring compound is sent into an oxidation reactor, and the carbon three compound in the wastewater is selectively converted into a compound containing carboxyl under the conditions of catalyst and oxidation reaction;
s3: filtering the wastewater treated in the step S2 to recover a catalyst, continuously using the catalyst for selective oxidation reaction, regulating the pH value of the filtered solution to 3-4, and then sending the filtered solution into an adsorption bed to remove compounds containing carboxyl;
s4: delivering the wastewater subjected to the adsorption treatment in the step S3 into a deep oxidation reactor, thoroughly decomposing organic matters in the wastewater under the conditions of a catalyst and an oxidation reaction, filtering the catalyst for recycling, and delivering filtrate into a chelating resin tower to remove high-valence metal ions to obtain refined brine;
s5: and (3) soaking the catalyst powder filtered in the step (S3) and the step (S4) in hydrochloric acid solution, wherein the catalyst powder is completely dissolved, and the solution is the catalyst solution.
According to the method of the utility model, the high-salt organic wastewater generated in the production process of the epoxy resin refers to wastewater with the sodium chloride content of 8-25 wt%, the TOC content of 2500-20000mg/L and the pH value of 8-13.
According to the method of the present utility model, the number of the adsorption beds in the step S1 may be 1 or more, and in the case of a plurality of adsorption beds, the adsorption beds may be in a series mode or a parallel mode. The adsorbent bed is filled with an adsorbent 1 and an adsorbent 2, the adsorbent 1 is made of carbon material such as polypropylene type carbon fiber, polyacrylonitrile type carbon fiber or viscose type carbon fiber, wherein the specific surface area is more than 1500m 2 /g, pore size less than 1nm; the adsorbent 2 is macroporous adsorption resin with specific surface area greater than 1100 m 2 And/g, the pore diameter is 10-20nm. Through the process of the step S1, the compounds containing benzene rings, such as micromolecular epoxy resin, toluene, bisphenol A and the like, are basically removed, and the removal rate can reach 98% -99%. The compounds containing benzene rings such as micromolecular epoxy resin, toluene, bisphenol A and the like which are desorbed by the adsorption bed through regeneration can be reused in the epoxy resin production process and can also be treated by an incinerator.
According to the method of the present utility model, the catalyst of step S2 is one or more metal oxides selected from nickel, cobalt or ruthenium, or a catalyst selected from metal salts of nickel, cobalt or ruthenium, and the oxidation reaction conditions are: the reaction time is 2-4 hours with sodium hypochlorite as oxidant and the catalyst concentration is 50-200mg/L based on the weight of the waste water at the normal pressure and the reaction temperature of 40-50 ℃, and the carbon three compounds such as epichlorohydrin, glycerol, 3-chloro-propanediol and the like in the waste water are converted into compounds containing carboxyl.
According to the method of the present utility model, the number of the adsorption beds in the step S3 may be 1 or more, and in the case of a plurality of adsorption beds, the adsorption beds may be in a series mode or a parallel mode. The adsorbent is filled in the adsorbent bed, and the adsorbent is polystyrene ion exchange resin. Through the step S3, TOC in the wastewater is less than 1000mg/L, and the carbon three compounds are basically removed. The carbon three compounds desorbed by the adsorption bed through regeneration can be used for purifying high-value chemicals and can also be treated by an incinerator.
According to the method of the present utility model, the catalyst of step S4 is a catalyst of one or more metal oxides selected from nickel, copper or cobalt, or a metal salt selected from nickel, copper or cobalt, and the oxidation reaction conditions are: the normal pressure, the reaction temperature of 40-50 ℃, the catalyst content of 0.1-1 wt% based on the weight of the wastewater, sodium hypochlorite as an oxidant, the pH value of the reaction solution maintained at 9-11, and the reaction time of 2-4 hours. Through the step S4, the TOC of the wastewater is less than 10mg/L, and the requirement of the ion membrane electrolysis brine on the organic matter content is met.
According to the process of the present utility model, the main function of the chelate resin packed in the chelate resin column of step S4 is to remove high-valence metal ions, such as Ca, present in the aqueous phase 2+ 、Mg 2+ Or residual catalyst metal ions to meet the technological requirements of caustic soda preparation by an ionic membrane. The chelating resins used in the present utility model are well known to those skilled in the art and are widely marketed products.
According to the method, the mass concentration of the hydrochloric acid solution in the step S5 is 20-30%.
The utility model has the beneficial effects that:
the method of the utility model realizes the classification treatment of different types of organic matters in the wastewater by the TOC process of the high-salt organic wastewater of the epoxy resin, and adopts a carbon material and macroporous adsorption resin combined adsorbent to adsorb and remove the organic matters containing benzene rings in the wastewater, wherein the removal rate reaches 98% -99%. The consumption of the oxidant can be reduced to the greatest extent, the wastewater treatment cost is reduced, and meanwhile, the TOC value of the wastewater can be reduced to below 10mg/L, so that the refined brine meeting the ionic membrane electrolysis is obtained, and the inorganic salt resource in the wastewater is effectively utilized.
Drawings
FIG. 1-schematic diagram of an apparatus for reducing TOC of high-salt organic wastewater of epoxy resin according to the present utility model
Wherein: 1-pH value adjusting tank 2-benzene ring compound adsorption bed 3-structure conversion oxidation reactor 4-carboxyl compound adsorption bed 5-deep oxidation reactor 6-raw material tank 7-refined brine tank 8-raw material pump 9-pH adjusting tank bottom pump 10-structure conversion oxidation reactor bottom pump 11-refined brine pump
Detailed Description
The present utility model will be described in further detail with reference to the following examples, in order to make the objects, technical solutions and effects of the present utility model more apparent. It should be noted that the detailed description herein is for purposes of illustration only and is not intended to limit the utility model.
The device for reducing TOC of the epoxy resin high-salt organic wastewater consists of a pH value adjusting tank, a benzene ring compound adsorption bed, a structural conversion oxidation reactor, a carboxyl compound adsorption bed and a deep oxidation reactor, wherein the pH value adjusting tank is connected with epoxy resin production wastewater and a hydrochloric acid feed inlet, an outlet of the pH value adjusting tank is connected with the benzene ring compound adsorption bed, an outlet of the benzene ring compound adsorption bed is connected with the structural conversion oxidation reactor, an outlet of the structural conversion oxidation reactor is connected with the carboxyl compound adsorption bed, and an outlet of the carboxyl compound adsorption bed is connected with the deep oxidation reactor.
The devices are connected through a pipeline or a pipeline and a pump.
The benzene ring compound adsorption bed is 1 or more; in the case of a plurality of adsorbent beds, the adsorbent beds are in a series mode or a parallel mode, and the adsorbent is filled in the adsorbent beds.
The number of the carboxyl compound adsorption beds is 1 or more, and in the case of a plurality of adsorption beds, the adsorption beds are in a series mode or a parallel mode, the adsorption beds are filled with adsorbents, and the adsorbents are polystyrene ion exchange resins.
The device for reducing TOC of the epoxy resin high-salt organic wastewater is also provided with a raw material tank and a refined brine tank.
The raw material tank is connected with the pH value adjusting tank through a raw material pump.
The outlet of the pH value adjusting tank is connected with the inlet of the pump at the bottom of the pH value adjusting tank, and the outlet of the pump at the bottom of the pH value adjusting tank is connected with the benzene ring compound adsorption bed.
The outlet of the structure conversion oxidation reactor is connected with the inlet of the bottom pump of the structure conversion oxidation reactor, and the outlet of the bottom pump of the structure conversion oxidation reactor is connected with the carboxyl compound adsorption bed.
The outlet of the deep oxidation reactor is connected with the inlet of a refined brine pump, and the outlet of the refined brine pump is connected with a refined brine tank.
Example 1
The TOC of the epoxy resin production wastewater is 17830mg/L, the content of the benzene ring compound is 4900mg/L, naCl, and the content of 196g/L, pH value is 12.5.
S1: adding hydrochloric acid to adjust pH of the wastewater from 12.5 to 4.0, changing the wastewater from clear transparent solution into white colloid solution, and feeding into two adsorption beds (polyacrylonitrile type carbon fiber with specific surface area 1850 m) containing two adsorption materials in series 2 /g, pore size of 0.46nm; macroporous adsorption resin with specific surface area 1350 m 2 Per g, pore diameter of 10 nm), the volume space velocity of the wastewater is controlled to be 12h based on the volume of the packed macroporous adsorption resin -1 The effluent is colorless transparent solution after passing through the adsorption bed; and the benzene ring compound is 40mg/L.
S2: and (2) delivering the wastewater treated in the step (S1) into an oxidation reactor, adding a cobalt oxide catalyst with the concentration of 150mg/L under the stirring condition, and reacting for 4 hours at the oxidation reaction temperature of 50 ℃ under the condition that sodium hypochlorite is used as an oxidant until the pH value of the wastewater is basically unchanged.
S3: filtering the wastewater treated in the step S2, continuously using the catalyst in the oxidation reaction of the step S2, and feeding the filtrate into two parallel adsorption beds filled with polystyrene ion exchange resin, wherein the volume space velocity of the wastewater is controlled to be 10h based on the filled resin volume -1 The wastewater is colorless transparent solution, and TOC is reduced to 879mg/L.
S4: and (3) sending the wastewater subjected to the adsorption treatment in the step (S3) into a deep oxidation reactor, adding 0.6% of nickel oxide catalyst by weight of the wastewater under the condition of stirring, reacting for 4 hours at the oxidation reaction temperature of 40 ℃ under the condition that 10% sodium hypochlorite solution is used as an oxidant, filtering the catalyst, recycling the catalyst, and sending the filtrate into a chelate resin tower filled with D401 chelate resin to remove high-valence metal ions, thereby obtaining refined brine with the TOC of 3.7mg/L.
S5: soaking the catalyst powder filtered in the step S3 and the step S4 in hydrochloric acid solution with the concentration of 20% respectively, and obtaining a catalyst CoCl after the catalyst powder is completely dissolved 2 A solution.
Example 2
The TOC of the epoxy resin production wastewater is 5627mg/L, the content of the benzene ring compound is 1762mg/L, naCl, the content of 116g/L, pH value is 10.8.
S1: adding hydrochloric acid to adjust pH of the wastewater from 10.8 to 3.5, changing the wastewater from clear transparent solution to white colloid solution, and feeding into two parallel adsorption beds (polypropylene type carbon fiber with specific surface area of 1609 m) containing two adsorption materials 2 /g, pore size of 0.53nm; macroporous adsorption resin with specific surface area 1160 m 2 Per g, pore size of 16 nm), the total volume space velocity of the wastewater is controlled to be 10h based on the volume of the loaded macroporous adsorption resin -1 The effluent is colorless transparent solution after passing through the adsorption bed; 16mg/L of benzene ring compound.
S2: and (2) delivering the wastewater treated in the step (S1) into an oxidation reactor, adding a ruthenium oxide catalyst with the concentration of 50mg/L under the stirring condition, and reacting for 6 hours at the oxidation reaction temperature of 45 ℃ under the condition that sodium hypochlorite is used as an oxidant until the pH value of the wastewater is basically unchanged.
S3: filtering the wastewater treated in the step S2, continuously using the catalyst in the oxidation reaction of the step S2, and feeding the filtrate into two adsorption beds which are connected in series and are provided with polystyrene ion exchange resin, wherein the space velocity of the total volume of the wastewater is controlled to be 13h based on the filled resin volume -1 The wastewater is colorless transparent solution, and TOC is reduced to 692mg/L.
S4: and (3) sending the wastewater subjected to the adsorption treatment in the step (S3) into a deep oxidation reactor, adding 0.2% of cobalt oxide catalyst by weight of the wastewater under the condition of stirring, reacting for 2 hours at the oxidation reaction temperature of 50 ℃ under the condition that 10% sodium hypochlorite solution is taken as an oxidant, filtering the catalyst, recycling the catalyst, and sending filtrate into a chelate resin tower filled with D463 chelate resin to remove high-valence metal ions, thereby obtaining refined brine with the TOC of 2.6mg/L.
S5: soaking the catalyst powder filtered in the step S3 and the step S4 in 25% hydrochloric acid solution to obtain catalyst CoCl 2 A solution.
Example 3
The TOC of the epoxy resin production wastewater is 18200mg/L, the content of the benzene ring compound is 5230mg/L, naCl, and the content of 120g/L, pH value is 9.6.
S1: adding hydrochloric acid to adjust pH of the wastewater from 9.6 to 2, changing the wastewater from clear transparent to white colloid solution, and feeding into two parallel adsorption beds (viscose carbon fiber with specific surface area of 1590 m) 2 /g, pore size of 0.15nm; macroporous adsorption resin with specific surface area of 1265m 2 Per g, pore diameter 19 nm), the total volume space velocity of the wastewater is controlled to be 11h based on the volume of the loaded macroporous adsorption resin -1 The effluent is colorless transparent solution after passing through the adsorption bed; 48.6mg/L of benzene ring compound.
S2: and (2) delivering the wastewater treated in the step (S1) into an oxidation reactor, adding a nickel oxide catalyst with the concentration of 100mg/L under the stirring condition, and reacting for 4 hours at the oxidation reaction temperature of 45 ℃ under the condition that sodium hypochlorite is used as an oxidant until the pH value of the wastewater is basically unchanged.
S3: filtering the wastewater treated in the step S2, continuously using the catalyst in the oxidation reaction of the step S2, and feeding the filtrate into two adsorption beds which are connected in series and are provided with polystyrene ion exchange resin, wherein the space velocity of the total volume of the wastewater is controlled to be 13h based on the filled resin volume -1 The wastewater is colorless transparent solution, and TOC is reduced to 820mg/L.
S4: and (3) sending the wastewater subjected to the adsorption treatment in the step (S3) into a deep oxidation reactor, adding 0.8% of cobalt oxide catalyst by weight of the wastewater under the condition of stirring, reacting for 3.5 hours at the temperature of 45 ℃ under the condition that 10% sodium hypochlorite solution is taken as an oxidant, filtering the catalyst, recycling the catalyst, and sending the filtrate into a chelating resin tower filled with D463 chelating resin to remove high-valence metal ions, thereby obtaining refined brine with the TOC of 3.1mg/L.
S5: soaking the catalyst powder filtered in the step S3 and the step S4 in 30% hydrochloric acid solution to obtain catalyst CoCl after the catalyst powder is completely dissolved 2 A solution.
Comparative example 1
The TOC of the epoxy resin production wastewater is 17830mg/L, the content of the benzene ring compound is 4900mg/L, naCl, and the content of 196g/L, pH value is 12.5.
Step (1): directly feeding the wastewater into an oxidation reaction tank without carbon fiber adsorption, adding a cobalt oxide catalyst with the concentration of 150mg/L under the stirring state, and reacting for 4 hours under the conditions that the oxidation reaction temperature is 45 ℃ and sodium hypochlorite is an oxidant until the pH value of the wastewater is basically unchanged.
Step (2): filtering the wastewater treated in the step (1), continuously using the catalyst in the oxidation reaction of the step (2), and feeding the filtrate into two adsorption beds which are connected in series and are filled with polystyrene ion exchange resin, wherein the space velocity of the total volume of the wastewater is controlled to be 10h based on the filled resin -1 The waste water is yellow transparent solution, and TOC is reduced to 12300mg/L.
Step (3): and (3) delivering the wastewater treated in the step (2) into a deep oxidation reactor, adding 1.0% of cobalt oxide catalyst by weight of the wastewater under the condition of stirring, reacting for 3 hours at the temperature of 45 ℃ under the condition that 10% sodium hypochlorite solution is taken as an oxidant, filtering the catalyst, and recycling the catalyst to obtain the TOC content of 8500mg/L and the benzene ring compound content of 2200mg/L in the water.
Comparative example 2
The TOC of the epoxy resin production wastewater is 17830mg/L, the content of the benzene ring compound is 4900mg/L, naCl, and the content of 196g/L, pH value is 12.5.
S1: adding hydrochloric acid to regulate pH value of the wastewater from 12.5 to 4.0, changing the wastewater from clear transparent solution into white colloid solution, then sending the white colloid solution into an adsorption bed filled with active carbon, and controlling volume space velocity of the wastewater to be 12h -1 The TOC content of the effluent after passing through the adsorption bed is 8620mg/L, and the benzene ring compound content is 165mg/L.
S2: and (2) delivering the wastewater treated in the step (S1) into an oxidation reactor, adding a cobalt oxide catalyst with the concentration of 150mg/L under the stirring condition, and reacting for 4 hours at the oxidation reaction temperature of 50 ℃ under the condition that sodium hypochlorite is used as an oxidant until the pH value of the wastewater is basically unchanged.
S3: filtering the wastewater treated in the step S2, continuously using the catalyst in the oxidation reaction of the step S2, and feeding the filtrate into two parallel adsorption beds filled with polystyrene ion exchange resin, wherein the volume space velocity of the wastewater is controlled to be 10h based on the filled resin volume -1 The wastewater is colorless transparent solution, and TOC is reduced to 820mg/L.
S4: and (3) sending the wastewater subjected to the adsorption treatment in the step (S3) into a deep oxidation reactor, adding 0.6% of nickel oxide catalyst by weight of the wastewater under the condition of stirring, reacting for 4 hours at the oxidation reaction temperature of 40 ℃ under the condition that 10% sodium hypochlorite solution is used as an oxidant, filtering the catalyst, recycling the catalyst, and sending the filtrate into a chelate resin tower filled with D401 chelate resin to remove high-valence metal ions, thereby obtaining refined brine with the TOC of 3.5mg/L.
S5: soaking the catalyst powder filtered in the step S3 and the step S4 in hydrochloric acid solution with the concentration of 20% respectively, and obtaining a catalyst CoCl after the catalyst powder is completely dissolved 2 A solution.
Claims (8)
1. A device for reducing TOC of epoxy resin high-salt organic wastewater consists of a pH value adjusting tank, a benzene ring compound adsorption bed, a structure conversion oxidation reactor, a carboxyl compound adsorption bed and a deep oxidation reactor, and is characterized in that: the pH value adjusting tank is connected with epoxy resin production wastewater and a hydrochloric acid feed inlet, an outlet of the pH value adjusting tank is connected with a benzene ring compound adsorption bed, an outlet of the benzene ring compound adsorption bed is connected with a structure conversion oxidation reactor, an outlet of the structure conversion oxidation reactor is connected with a carboxyl compound adsorption bed, and an outlet of the carboxyl compound adsorption bed is connected with a deep oxidation reactor; the connection between the devices is through a pipe, or a pipe and a pump.
2. The device for reducing TOC in high-salt organic wastewater of epoxy resin according to claim 1, wherein the benzene ring compound adsorption bed is 1 or more; in the case of a plurality of adsorbent beds, the adsorbent beds are in a series mode or a parallel mode, and the adsorbent is filled in the adsorbent beds.
3. The device for reducing TOC of high-salt organic wastewater of epoxy resin according to claim 1, wherein the number of the carboxyl compound adsorption beds is 1 or more, and in the case of a plurality of adsorption beds, the adsorption beds are in a series mode or a parallel mode, the adsorption beds are filled with an adsorbent, and the adsorbent is polystyrene ion exchange resin.
4. The device for reducing TOC of the epoxy resin high-salt organic wastewater according to claim 1, wherein the device for reducing TOC of the epoxy resin high-salt organic wastewater is further provided with a raw material tank and a refined brine tank.
5. The device for reducing TOC of high-salt organic wastewater of epoxy resin according to claim 1, wherein the outlet of the pH value adjusting tank is connected with the inlet of a pump at the bottom of the pH value adjusting tank, and the outlet of the pump at the bottom of the pH value adjusting tank is connected with a benzene ring compound adsorption bed.
6. The device for reducing TOC of high-salt organic wastewater of epoxy resin according to claim 1, wherein the structure conversion oxidation reactor is connected with a bottom pump inlet of the structure conversion oxidation reactor, and an outlet of the bottom pump of the structure conversion oxidation reactor is connected with a carboxyl compound adsorption bed.
7. The device for reducing TOC of high-salt organic wastewater of epoxy resin according to claim 3, wherein the outlet of the deep oxidation reactor is connected with the inlet of a refined brine pump, and the outlet of the refined brine pump is connected with a refined brine tank.
8. The device for reducing TOC in organic wastewater containing high salt of epoxy resin according to claim 4, wherein the outlet of the raw material tank is connected with the inlet of the raw material pump, and the outlet of the raw material pump is connected with the pH value adjusting tank.
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