Purification treatment process of raspberry ketone-containing organic waste liquid

Abstract

The invention belongs to the technical field of wastewater treatment, and particularly relates to a purification treatment process of raspberry ketone-containing organic waste liquid, which comprises the following steps: soaking mesoporous silica in a cerous nitrate aqueous solution, roasting, cooling, carrying out hydroxylation treatment, reacting with an inner layer precursor solution, carrying out surface alkenylation treatment, uniformly mixing with an outer layer precursor solution, emulsifying, heating, and carrying out vacuum drying to obtain the raspberry ketone-containing organic waste liquid. And carrying out thermal removal, extraction and drying to obtain the catalyst. Carrying out aldehyde oxidation treatment on the organic waste liquid, adjusting the pH value, reacting with ozone and a catalyst to complete treatment on the organic waste liquid, and eluting the catalyst to obtain a raspberry ketone recovery solution. According to the invention, the catalyst is cooperated with ozone to treat the organic waste liquid after aldehyde oxidation, so that p-hydroxybenzaldehyde in the organic waste liquid is effectively degraded, and raspberry ketone is recovered at the same time.

Description

Technical Field

[0001] This invention belongs to the field of wastewater treatment technology, and particularly relates to a purification process for organic waste liquid containing raspberry ketone. Background Technology

[0002] Raspberry ketone, a high-value fragrance intermediate, is mainly produced industrially through the condensation of p-hydroxybenzaldehyde with acetone and subsequent hydrogenation. In actual production and some modified processes, especially under conditions of incomplete extraction and separation or accumulation of mother liquor, an organic waste liquid is generated. After stripping and recovering volatile acetone, the liquid phase still contains significantly enriched incompletely converted p-hydroxybenzaldehyde and a large amount of the target product raspberry ketone that could not be effectively separated. Since the aldehyde group contained in p-hydroxybenzaldehyde has a significant inhibitory effect on microorganisms, when using a conventional anaerobic + aerobic system for treatment, there is not only a risk of microbial poisoning, but also the accumulation of biological metabolites makes it difficult for the effluent COD to meet the discharge requirements (COD < 50 mg / L).

[0003] Chinese patent document CN115090287B discloses an iron-cobalt-doped ozone activation catalyst Fe-CoOx and its preparation method, which first involves Fe... 2+ Co 2+ The precursor that reacts with K3[Fe(CN)3] to produce a Prussian blue analogue, after being deposited and aged for an appropriate time, yields a highly efficient heterogeneous ozone-activated catalyst after calcination. When the above catalyst and ozone are used to synergistically treat organic waste liquid containing p-hydroxybenzaldehyde and raspberry ketone, the iron-cobalt oxide in the catalyst can catalyze the generation of hydroxyl radicals from ozone. The hydroxyl radicals degrade p-hydroxybenzaldehyde and raspberry ketone. Although this can reduce the COD value of the organic waste liquid, it cannot selectively degrade p-hydroxybenzaldehyde and adsorb and retain raspberry ketone, making it difficult to recycle raspberry ketone and causing resource waste. Summary of the Invention

[0004] This invention provides a purification process for organic waste liquid containing raspberry ketone. First, the organic waste liquid containing raspberry ketone is subjected to aldehyde oxidation treatment. Then, a catalyst is used in conjunction with ozone to treat the aldehyde-oxidized organic waste liquid, effectively degrading p-hydroxybenzaldehyde in the organic waste liquid, while recovering raspberry ketone.

[0005] To solve the above problems, the present invention adopts the following technical solution: A purification process for organic waste liquid containing raspberry ketone includes the following steps: S1. Mesoporous silica is dispersed in an aqueous solution of cerium nitrate, impregnated, washed, dried, calcined, cooled, and then subjected to surface hydroxylation treatment to obtain active microspheres; S2. The active microspheres are dispersed in the inner layer precursor solution and reacted, washed, and then dispersed in the outer layer precursor solution after surface alkenylation treatment. The microspheres are added to the dispersion solution, emulsified, heated, reacted, washed, and then thermally removed, extracted, and dried to obtain the catalyst. The inner layer precursor solution is prepared by reacting TEOS and APTES under acidic conditions and then mixing them with PEG. The outer layer precursor solution is prepared by mixing styrene, divinylbenzene, toluene, poloxamer, an initiator, and a VBTAC aqueous solution. S3. The organic waste liquid is subjected to aldehyde oxidation treatment. After adjusting the pH value, it is mixed with ozone and catalyst through a reaction column to complete the treatment of the organic waste liquid. The catalyst is then eluted to obtain a raspberry ketone recovery solution.

[0006] This invention first treats organic waste liquid containing raspberry ketone with aldehyde oxidation to oxidize p-hydroxybenzaldehyde into p-hydroxybenzoic acid. Then, ozone and a catalyst with gradient functions are used to synergistically treat the organic waste liquid after aldehyde oxidation. The catalyst consists of an outer shell, an inner shell, and active microspheres from the outside to the inside. The outer shell can simultaneously enrich p-hydroxybenzoic acid and raspberry ketone. The inner shell selectively enriches p-hydroxybenzoic acid and diffuses it to the active sites of the active microspheres for degradation. Raspberry ketone is retained in the outer shell, reducing the COD value of the organic waste liquid. The raspberry ketone enriched in the outer shell is eluted and recovered, avoiding waste of raspberry ketone.

[0007] The active microspheres use mesoporous silica as a carrier, on which cerium oxide, converted from cerium nitrate by calcination, is loaded as active sites. TEOS (tetraethyl orthosilicate) and APTES (3-aminopropyltriethoxysilane) are hydrolyzed and undergo a condensation reaction with the silanol groups on the surface of the active microspheres, forming an inner shell layer with PEG-1200 (polyethylene glycol-1200) as a porogen. After surface alkenylation treatment, carbon-carbon double bonds are introduced on the surface of the inner shell layer. These carbon-carbon double bonds react with the carbon-carbon double bonds of styrene, divinylbenzene, and VBTAC (p-vinylbenzyltrimethylammonium chloride) under the action of an initiator, forming an outer shell layer with toluene as a porogen. After removing toluene and PEG-1200, the catalyst is obtained. In the catalyst, the inner pore walls of the outer shell contain hydrophobic aromatic structures and permanent positive charges, enabling the effective enrichment of raspberry ketone through hydrophobic interactions and the enrichment of p-hydroxybenzoic acid through electrostatic interactions. The inner pore walls of the inner shell are rich in primary amino groups, allowing p-hydroxybenzoic acid to further enter the pores of the inner shell through electrostatic interactions for enrichment. Under the influence of the concentration gradient, it diffuses towards the active sites. The hydroxyl radicals generated by the catalytic decomposition of ozone at the active sites can degrade p-hydroxybenzoic acid, reducing the content of p-hydroxybenzoic acid in the effluent. Raspberry ketone does not contain ionizable groups and is difficult to electrostatically interact with primary amino groups. There is also a hydrophobic effect between the two. Because raspberry ketone is difficult to enter the pores of the inner shell, it can be effectively retained in the outer shell, thereby effectively reducing the COD of the effluent. The raspberry ketone enriched in the outer shell can be eluted and recovered, avoiding waste of raspberry ketone.

[0008] Furthermore, in step S1, mesoporous silica is dispersed in a 0.6-0.9wt% cerium nitrate aqueous solution and impregnated for 10-12 hours. After washing with deionized water, it is dried in an environment of 85-95℃ for 10-12 hours, calcined at 550-560℃ for 3-4 hours, cooled, and treated with water vapor plasma at 50-60W radio frequency power for 5-6 minutes to obtain active microspheres.

[0009] After calcination at 550-560℃, cerium nitrate supported on mesoporous silica is oxidized to generate cerium oxide active sites, while the number of silanol groups on the mesoporous silica is significantly reduced. After steam plasma treatment, silanol groups are reintroduced onto the surface of the mesoporous silica, providing a molecular basis for subsequent hydrolysis reactions with the silanol groups of TEOS and APTES hydrolysis products. This facilitates the covalent bonding of the inner shell to the active microspheres, improving the structural stability of the catalyst.

[0010] Furthermore, the active microspheres comprise the following raw materials in parts by weight: 40-45 parts of mesoporous silica and 300-310 parts of a 0.6-0.9 wt% cerium nitrate aqueous solution.

[0011] Furthermore, the inner layer precursor solution is prepared by mixing 97-98 wt% ethanol solution, TEOS and APTES, adjusting the pH to 5.5-5.7 by adding acetic acid solution dropwise, reacting for 1.5-2 hours, adding PEG and mixing to obtain the inner layer precursor solution; the outer layer precursor solution is prepared by mixing styrene, divinylbenzene, toluene, poloxamer and initiator AIBN, dispersing in 40-45 wt% VBTAC aqueous solution to obtain the outer layer precursor solution; the average molecular weight of the PEG is 1200-1300 g / mol.

[0012] TEOS and APTES undergo hydrolysis and controlled condensation at pH 5.5-5.7 to generate oligomeric siloxanes. By controlling the reaction time, the size of the oligomeric siloxanes can be controlled, preventing them from entering and clogging the mesopores of the active microspheres, thus improving the mass transfer efficiency of the catalyst. Poloxamer can synergistically form a hierarchical porous structure on the outer shell layer with toluene, improving the catalyst's enrichment capacity and mass transfer efficiency. Poloxamer contains both hydrophobic and hydrophilic segments, which enhances the dispersibility of VBTAC aqueous solution in a mixture of styrene, divinylbenzene, toluene, and initiator, maintains the stability of the outer precursor solution, and facilitates the introduction of a uniformly distributed permanent positive charge on the outer shell layer.

[0013] Further, in step S2, the active microspheres are dispersed in the inner precursor solution and reacted for 4-5 hours. After washing with toluene, they are dispersed in toluene, VTMS and 97-98 wt% ethanol solution are added and mixed. Acetic acid solution is added dropwise to adjust the pH to 5.5-5.7, and the reaction is carried out for 1.5-2 hours. After washing with toluene, they are dispersed in the outer precursor solution and added to the dispersion. The mixture is emulsified at 8000-9000 rpm for 15-25 minutes, heated to 65-75℃ and reacted for 3-4 hours. After washing with toluene and anhydrous ethanol, the mixture is placed in an environment of 112-115℃ for thermal desorption for 5-6 hours. The mixture is then dispersed in a 50-55 wt% ethanol solution for extraction for 1-2 hours. After washing with anhydrous ethanol, the mixture is placed in an environment of 55-60℃ and 20-25 kPa for drying for 10-12 hours to obtain the catalyst.

[0014] Active microspheres are dispersed in an inner-layer precursor solution. The oligomeric siloxanes generated by the hydrolysis and condensation of TEOS and APTES undergo a condensation reaction with the silanol groups on the surface of the active microspheres, forming an inner shell layer with PEG-1200 as a porogen. Subsequently, the microspheres are dispersed in toluene. Due to the poor compatibility between toluene and PEG-1200, VTMS is mainly distributed outside the inner shell layer. Water from the subsequently added ethanol and acetic acid solutions preferentially accumulates on the hydrophilic surface of the inner shell layer. Therefore, the hydrolysis products of VTMS mainly condense with silanol groups on the inner shell layer surface, introducing carbon-carbon double bonds. This provides the molecular basis for subsequent free radical polymerization reactions with monomers such as styrene to form an outer shell layer, facilitating the connection of the outer shell layer to the inner shell layer through covalent bonds and improving the structural stability of the catalyst. The outer-layer precursor solution, due to its poor compatibility with PEG-1200, has difficulty penetrating into the inner shell layer, thus confining the free radical polymerization reaction outside the inner shell layer, ensuring unobstructed pores in the inner shell layer and improving mass transfer efficiency.

[0015] Furthermore, in step S2, after the active microspheres reacting with the inner layer precursor solution are dispersed in toluene, VTMS, APTES and 97-98wt% ethanol solution are added and mixed.

[0016] After hydrolysis, APTES undergoes a condensation reaction with the silanol groups on the inner shell surface, moderately increasing the density of primary amines at the interface between the inner and outer shells. This facilitates the diffusion and transfer of p-hydroxybenzoic acid into the inner shell, improving the decomposition efficiency of p-hydroxybenzoic acid. At the same time, a hydrophilic barrier is introduced at the interface between the inner and outer shells, inhibiting the diffusion of raspberry ketone into the inner shell and improving the enrichment effect of raspberry ketone.

[0017] Further, the catalyst comprises the following raw materials in parts by weight: 32-38 parts of active microspheres, 276-284 parts of inner layer precursor solution, 5-7 parts of VTMS, 0-3 parts of APTES, 6-8 parts of 97-98 wt% ethanol solution, and 180-190 parts of outer layer precursor solution; the inner layer precursor solution comprises the following raw materials in parts by weight: 295-304 parts of 97-98 wt% ethanol solution, 20-25 parts of TEOS, 5-7 parts of APTES, and 5-6 parts of PEG; the outer layer precursor solution comprises the following raw materials in parts by weight: 72-76 parts of styrene, 19-23 parts of divinylbenzene, 100-110 parts of toluene, 11-14 parts of 40-45 wt% VBTAC aqueous solution, and 4-5 parts of poloxamer; the dispersion comprises 200-220 parts by weight of deionized water and 2-3 parts by weight of sodium dodecyl sulfate.

[0018] Furthermore, the organic waste liquid is subjected to aldehyde oxidation treatment in the following manner: sodium hydroxide solution is added to the organic waste liquid to adjust the pH value to 8-8.5, 15-17wt% potassium permanganate solution is added and reacted for 1-2 hours, sodium sulfite is added and stirred for 15-25 minutes, filtered, and sulfuric acid solution is added to the filtrate to adjust the pH value to 6.5-7, thus completing the pretreatment of the organic waste liquid.

[0019] Under pH conditions of 8-8.5, the aldehyde group of p-hydroxybenzaldehyde is oxidized to a carboxyl group by potassium permanganate to obtain p-hydroxybenzoic acid, which provides a molecular basis for subsequent separation from raspberry ketone. Under pH conditions of 6.5-7, the primary amino group is protonated and becomes positively charged, while the carboxyl group is deprotonated and becomes negatively charged, which is conducive to the enrichment of p-hydroxybenzoic acid by the catalyst through electrostatic interaction.

[0020] Furthermore, the mass ratio of p-hydroxybenzaldehyde, 15-17wt% potassium permanganate solution, and sodium sulfite in the organic waste liquid is 1:(7-7.2):(2.5-2.7).

[0021] Furthermore, in step S3, the catalyst is packed into a fixed-bed column to obtain a reaction column. The organic waste liquid after aldehyde oxidation treatment and ozone are simultaneously introduced into the reaction column to complete the treatment of the organic waste liquid and obtain purified effluent. A 60-70wt% ethanol solution is introduced into the reaction column for elution to obtain a raspberry ketone recovery solution. The flow rate of the organic waste liquid after aldehyde oxidation treatment is 1-2 BV / h; the concentration of ozone is 20-25 mg / L, and the flow rate is 0.2-0.3 L / min; the flow rate of the 60-70wt% ethanol solution is 1.3-1.6 BV / h.

[0022] The present invention has the following beneficial effects: This invention first oxidizes p-hydroxybenzaldehyde in raspberry ketone-containing organic wastewater to p-hydroxybenzoic acid, and then uses ozone and a catalyst for synergistic treatment. The catalyst consists of an outer shell, an inner shell, and active microspheres from the outside to the inside. The inner wall of the outer shell contains hydrophobic aromatic structures and permanent positive charges, which can enrich raspberry ketone through hydrophobic interaction and p-hydroxybenzoic acid through electrostatic interaction. The inner wall of the inner shell is rich in primary amino groups, which can selectively enrich p-hydroxybenzoic acid through electrostatic interaction and transfer it to the active microspheres. The active microspheres are loaded with cerium oxide, which can synergistically degrade p-hydroxybenzoic acid with ozone. Raspberry ketone is retained in the pores of the outer shell because it does not contain ionizable groups and has hydrophobic interactions with primary amino groups, effectively reducing the COD of the effluent. The raspberry ketone enriched in the outer shell can be eluted and recovered, avoiding waste of raspberry ketone. Attached Figure Description

[0023] Figure 1 This is a chromatogram of the raspberry ketone recovery solution obtained in Example 5. Detailed Implementation

[0024] Preparation Example 1 40g of mesoporous silica with a particle size of 1μm was added to 300g of 0.7wt% cerium nitrate aqueous solution, ultrasonically dispersed at 500W for 20min, stirred and impregnated at 200rpm for 12h, filtered, washed 4 times with deionized water, placed in an oven and dried at 85℃ for 10h, transferred to a tube furnace, heated to 550℃ and calcined for 4h, naturally cooled to room temperature, placed in a plasma generator, and nitrogen gas at a flow rate of 250mL / min was bubbled into the deionized water. The bubbled gas was then passed into the plasma generator and plasma treated for 5min at a radio frequency power of 50W to obtain active microspheres.

[0025] Preparation Example 2 42g of mesoporous silica with a particle size of 1μm was added to 305g of 0.6wt% cerium nitrate aqueous solution, ultrasonically dispersed at 500W for 20min, stirred and impregnated at 200rpm for 10h, filtered, washed 4 times with deionized water, placed in an oven and dried at 95℃ for 11h, transferred to a tube furnace, heated to 560℃ and calcined for 3h, naturally cooled to room temperature, placed in a plasma generator, and nitrogen gas at a flow rate of 250mL / min was bubbled into the deionized water. The bubbled gas was then passed into the plasma generator and plasma treated for 5.5min at a radio frequency power of 55W to obtain active microspheres.

[0026] Preparation Example 3 45g of mesoporous silica with a particle size of 1μm was added to 310g of 0.9wt% cerium nitrate aqueous solution, ultrasonically dispersed at 500W for 20min, stirred and impregnated at 200rpm for 11h, filtered, washed 4 times with deionized water, placed in an oven and dried at 90℃ for 12h, transferred to a tube furnace, heated to 556℃ and calcined for 3.5h, naturally cooled to room temperature, placed in a plasma generator, and nitrogen gas at a flow rate of 250mL / min was bubbled into the deionized water. The bubbled gas was then passed into the plasma generator and plasma treated for 6min at a radio frequency power of 60W to obtain active microspheres.

[0027] Example 1 Add 20g TEOS (tetraethyl orthosilicate) and 5g APTES (3-aminopropyltriethoxysilane) to 300g of 97wt% ethanol solution, stir at 500rpm for 10min, adjust the pH to 5.5 by adding 10wt% acetic acid solution dropwise, stir at 400rpm for 1.5h, add 5g of PEG with an average molecular weight of 1200g / mol, stir at 600rpm for 10min to obtain the inner layer precursor solution; mix 75g styrene, 20g divinylbenzene, 100g toluene, 4g poloxamer (preferably poloxamer P123) and 1g AIBN (azobisisobutyronitrile), stir at 300rpm for 10min, add 11g 45wt% ethanol solution... VBTAC (p-vinylbenzyltrimethylammonium chloride) aqueous solution was stirred at 1000 rpm for 5 min to obtain the outer layer precursor solution; 2 g sodium dodecyl sulfate was added to 200 g deionized water and stirred at 300 rpm for 5 min to obtain the dispersion; 35 g of active microspheres were added to 280 g of the inner layer precursor solution, ultrasonically dispersed at 500 W for 30 min, stirred at 600 rpm for 4 h, filtered, washed 3 times with toluene, added to 200 g of toluene, stirred at 2000 rpm for 15 min, and then 5 g VTMS (vinyltrimethoxysilane), 2 g APTES, and 6 g of [unclear text - possibly a continuation of the previous sentence] were added. A 98 wt% ethanol solution was stirred at 500 rpm for 10 min, and a 10 wt% acetic acid solution was added dropwise to adjust the pH to 5.5. The mixture was stirred at 400 rpm for 1.5 h, filtered, washed three times with toluene, and added to 185 g of the outer precursor solution. The mixture was stirred at 2000 rpm for 15 min to obtain an oil phase mixture, which was then added to the dispersion. The mixture was emulsified by stirring at 8000 rpm for 20 min, heated to 65 °C, and stirred at 2000 rpm for 3 h. The mixture was filtered, washed three times with toluene, and washed three times with anhydrous ethanol. The mixture was placed in an oven and thermally desorbed at 115 °C for 5 h. The mixture was then added to 500 g of a 50 wt% ethanol solution, stirred at 1000 rpm for 20 min, and stirred at 300 rpm for 1 h. The mixture was filtered, washed three times with anhydrous ethanol, and dried at 60 °C and 25 kPa for 10 h to obtain the catalyst. The catalyst was then packed into a fixed-bed column to obtain the reaction column.

[0028] The concentration of p-hydroxybenzaldehyde in the organic waste liquid was determined by chromatography, and the mass of p-hydroxybenzaldehyde was calculated based on the volume of the organic waste liquid to be treated. The pH of the organic waste liquid was adjusted to 8 by adding 15 wt% sodium hydroxide solution, followed by adding 15 wt% potassium permanganate solution and stirring at 200 rpm for 1 hour. Sodium sulfite was then added and stirred at 200 rpm for 15 minutes. The mass ratio of p-hydroxybenzaldehyde, 17 wt% potassium permanganate solution, and sodium sulfite in the organic waste liquid was 1:7:2.5. The solution was filtered, and 30 wt% sulfuric acid solution was added to the filtrate to adjust... With a pH of 7, ozone is introduced into the reaction column at a rate of 1.5 BV / h, while simultaneously, ozone at a concentration of 25 mg / L is introduced into the reaction column at a rate of 0.3 L / min. Feeding is stopped when the COD value of the effluent exceeds 50 mg / L, completing the treatment of the organic waste liquid and obtaining purified effluent. The reaction column is then purged with nitrogen, and a 70 wt% ethanol solution is introduced into the reaction column at a rate of 1.6 BV / h. Feeding is stopped when the concentration of raspberry ketone in the effluent is less than 1% of the initial concentration, resulting in a raspberry ketone recovery solution, thereby recovering raspberry ketone from the organic waste liquid.

[0029] Example 2 Add 21g TEOS and 6g APTES to 300g of 97wt% ethanol solution, stir at 500rpm for 10min, adjust the pH to 5.5 by adding 10wt% acetic acid solution dropwise, stir at 400rpm for 1.5h, add 5g of PEG with an average molecular weight of 1200g / mol, stir at 600rpm for 10min to obtain the inner layer precursor solution; mix 73g styrene, 21g divinylbenzene, 105g toluene, 4.2g poloxamer (preferably poloxamer P123) and 1.5g AIBN, stir at 300rpm for 10min, add 11g 45wt% ethanol solution... VBTAC aqueous solution was stirred at 1000 rpm for 5 min to obtain the outer layer precursor solution; 2.5 g sodium dodecyl sulfate was added to 210 g deionized water and stirred at 300 rpm for 5 min to obtain the dispersion; 36 g of active microspheres were added to 276 g of inner layer precursor solution, ultrasonically dispersed at 500 W for 30 min, stirred at 600 rpm for 4 h, filtered, washed 3 times with toluene, added to 200 g toluene, stirred at 2000 rpm for 15 min, and then 6 g VTMS, 3 g APTES and 6 g were added. A 98 wt% ethanol solution was stirred at 500 rpm for 10 min, and a 10 wt% acetic acid solution was added dropwise to adjust the pH to 5.5. The mixture was stirred at 400 rpm for 1.5 h, filtered, washed three times with toluene, and added to 188 g of the outer precursor solution. The mixture was stirred at 2000 rpm for 15 min to obtain an oil phase mixture, which was then added to the dispersion. The mixture was emulsified at 8000 rpm for 20 min, heated to 65 °C, and stirred at 2000 rpm for 3 h. The mixture was filtered, washed three times with toluene, and washed three times with anhydrous ethanol. The mixture was placed in an oven and thermally desorbed at 115 °C for 5 h. The mixture was then added to 500 g of a 50 wt% ethanol solution, stirred at 1000 rpm for 20 min, and stirred at 300 rpm for 1 h. The mixture was filtered, washed three times with anhydrous ethanol, and dried at 60 °C and 25 kPa for 10 h to obtain the catalyst. The catalyst was then packed into a fixed-bed column to obtain a reaction column.

[0030] The concentration of p-hydroxybenzaldehyde in the organic waste liquid was determined by chromatography, and the mass of p-hydroxybenzaldehyde was calculated based on the volume of the organic waste liquid to be treated. The pH of the organic waste liquid was adjusted to 8 by adding 15 wt% sodium hydroxide solution, followed by adding 15 wt% potassium permanganate solution and stirring at 200 rpm for 1 hour. Sodium sulfite was then added and stirred at 200 rpm for 15 minutes. The mass ratio of p-hydroxybenzaldehyde, 17 wt% potassium permanganate solution, and sodium sulfite in the organic waste liquid was 1:7:2.5. The solution was filtered, and 30 wt% sulfuric acid solution was added to the filtrate to adjust... The pH value was adjusted to 7, and ozone was introduced into the reaction column at a rate of 2 BV / h. At the same time, ozone at a concentration of 20 mg / L was introduced into the reaction column at a rate of 0.2 L / min. When the COD value of the effluent was higher than 50 mg / L, the feed was stopped, completing the treatment of the organic waste liquid and obtaining purified effluent. The reaction column was then purged with nitrogen, and a 70 wt% ethanol solution was introduced into the reaction column at a rate of 1.5 BV / h. When the concentration of raspberry ketone in the effluent was less than 1% of the initial concentration, the feed was stopped, resulting in a raspberry ketone recovery solution, thereby recovering raspberry ketone from the organic waste liquid.

[0031] The active microspheres used in this embodiment were prepared in Preparation Example 1.

[0032] Example 3 Add 23g TEOS and 7g APTES to 295g of 97.5wt% ethanol solution, stir at 500rpm for 10min, adjust the pH to 5.6 by adding 10wt% acetic acid solution dropwise, stir at 400rpm for 2h, add 5.5g of PEG with an average molecular weight of 1250g / mol, stir at 600rpm for 10min to obtain the inner layer precursor solution; mix 76g styrene, 19g divinylbenzene, 110g toluene, 4.3g poloxamer (preferably poloxamer P123) and 2g AIBN, stir at 300rpm for 10min, add 13g 42wt% ethanol solution... VBTAC aqueous solution was stirred at 1000 rpm for 5 min to obtain the outer layer precursor solution; 3 g sodium dodecyl sulfate was added to 205 g deionized water and stirred at 300 rpm for 5 min to obtain the dispersion; 32 g of active microspheres were added to 282 g of inner layer precursor solution, ultrasonically dispersed at 500 W for 30 min, stirred at 600 rpm for 5 h, filtered, washed 3 times with toluene, added to 200 g toluene, stirred at 2000 rpm for 15 min, and then 7 g VTMS, 2.5 g APTES and 8 g were added. A 97wt% ethanol solution was stirred at 500 rpm for 10 min, and a 10wt% acetic acid solution was added dropwise to adjust the pH to 5.6. The mixture was stirred at 400 rpm for 1.7 h, filtered, washed three times with toluene, and added to 180 g of the outer precursor solution. The mixture was stirred at 2000 rpm for 15 min to obtain an oil phase mixture, which was then added to the dispersion. The mixture was stirred at 8500 rpm for 25 min to emulsify, heated to 70 °C, and stirred at 2000 rpm for 4 h. The mixture was filtered, washed three times with toluene, and washed three times with anhydrous ethanol. The mixture was placed in an oven and thermally desorbed at 113 °C for 5.5 h. The mixture was then added to 500 g of a 52wt% ethanol solution, stirred at 1000 rpm for 20 min, and stirred at 300 rpm for 1.5 h. The mixture was filtered, washed three times with anhydrous ethanol, and dried at 55 °C and 20 kPa for 12 h to obtain the catalyst. The catalyst was then packed into a fixed-bed column to obtain the reaction column.

[0033] The concentration of p-hydroxybenzaldehyde in the organic waste liquid was determined by chromatography, and its mass was calculated based on the volume of the waste liquid. The pH of the waste liquid was adjusted to 8.3 by adding 15 wt% sodium hydroxide solution, followed by 16 wt% potassium permanganate solution and stirring at 200 rpm for 1.2 h. Sodium sulfite was then added and stirred at 200 rpm for 20 min. The mass ratio of p-hydroxybenzaldehyde, 17 wt% potassium permanganate solution, and sodium sulfite in the waste liquid was 1:7.1:2.6. The solution was filtered, and 30 wt% sulfuric acid solution was added to the filtrate. The pH was adjusted to 6.8, and ozone was introduced into the reaction column at a rate of 1 BV / h. Simultaneously, ozone at a concentration of 22 mg / L was introduced into the reaction column at a rate of 0.25 L / min. Feeding was stopped when the COD value of the effluent exceeded 50 mg / L, completing the treatment of the organic waste liquid and obtaining purified effluent. The reaction column was then purged with nitrogen, and a 65 wt% ethanol solution was introduced into the reaction column at a rate of 1.3 BV / h. Feeding was stopped when the concentration of raspberry ketone in the effluent was less than 1% of the initial concentration, resulting in a raspberry ketone recovery solution, thus recovering raspberry ketone from the organic waste liquid.

[0034] The active microspheres used in this embodiment were prepared in Preparation Example 2.

[0035] Example 4 Add 24g TEOS and 6g APTES to 295g of 97.5wt% ethanol solution, stir at 500rpm for 10min, adjust the pH to 5.6 by adding 10wt% acetic acid solution dropwise, stir at 400rpm for 2h, add 5.5g of PEG with an average molecular weight of 1250g / mol, stir at 600rpm for 10min to obtain the inner layer precursor solution; mix 74g styrene, 23g divinylbenzene, 107g toluene, 5g poloxamer (preferably poloxamer P123) and 1.7g AIBN, stir at 300rpm for 10min, add 13g 42wt% ethanol solution... VBTAC aqueous solution was stirred at 1000 rpm for 5 min to obtain the outer layer precursor solution; 2.7 g sodium dodecyl sulfate was added to 220 g deionized water and stirred at 300 rpm for 5 min to obtain the dispersion; 37 g of active microspheres were added to 278 g of inner layer precursor solution, ultrasonically dispersed at 500 W for 30 min, stirred at 600 rpm for 5 h, filtered, washed 3 times with toluene, added to 200 g toluene, stirred at 2000 rpm for 15 min, and then 5.5 g VTMS, 2.6 g APTES and 8 g of [unclear text - possibly a continuation of the previous sentence] were added. A 97wt% ethanol solution was stirred at 500 rpm for 10 min, and a 10wt% acetic acid solution was added dropwise to adjust the pH to 5.6. The mixture was stirred at 400 rpm for 1.7 h, filtered, washed three times with toluene, and added to 185 g of the outer precursor solution. The mixture was stirred at 2000 rpm for 15 min to obtain an oil phase mixture, which was then added to the dispersion. The mixture was stirred at 8500 rpm for 25 min to emulsify, heated to 70 °C, and stirred at 2000 rpm for 4 h. The mixture was filtered, washed three times with toluene, and washed three times with anhydrous ethanol. The mixture was placed in an oven and thermally desorbed at 113 °C for 5.5 h. The mixture was then added to 500 g of a 52wt% ethanol solution, stirred at 1000 rpm for 20 min, and stirred at 300 rpm for 1.5 h. The mixture was filtered, washed three times with anhydrous ethanol, and dried at 55 °C and 20 kPa for 12 h to obtain the catalyst. The catalyst was then packed into a fixed-bed column to obtain the reaction column.

[0036] The concentration of p-hydroxybenzaldehyde in the organic waste liquid was determined by chromatography, and its mass was calculated based on the volume of the waste liquid. The pH of the waste liquid was adjusted to 8.3 by adding 15 wt% sodium hydroxide solution, followed by 16 wt% potassium permanganate solution and stirring at 200 rpm for 1.2 h. Sodium sulfite was then added and stirred at 200 rpm for 20 min. The mass ratio of p-hydroxybenzaldehyde, 17 wt% potassium permanganate solution, and sodium sulfite in the waste liquid was 1:7.1:2.6. The solution was filtered, and 30 wt% sulfuric acid solution was added to the filtrate. The pH was adjusted to 6.8, and ozone was introduced into the reaction column at a rate of 1 BV / h. Simultaneously, ozone at a concentration of 22 mg / L was introduced into the reaction column at a rate of 0.25 L / min. Feeding was stopped when the COD value of the effluent exceeded 50 mg / L, completing the treatment of the organic waste liquid and obtaining purified effluent. The reaction column was then purged with nitrogen, and a 65 wt% ethanol solution was introduced into the reaction column at a rate of 1.3 BV / h. Feeding was stopped when the concentration of raspberry ketone in the effluent was less than 1% of the initial concentration, resulting in a raspberry ketone recovery solution, thus recovering raspberry ketone from the organic waste liquid.

[0037] The active microspheres used in this embodiment were prepared in Preparation Example 2.

[0038] Example 5 Add 25g TEOS and 5g APTES to 304g of 98wt% ethanol solution, stir at 500rpm for 10min, adjust the pH to 5.7 by adding 10wt% acetic acid solution dropwise, stir at 400rpm for 1.8h, add 6g of PEG with an average molecular weight of 1300g / mol, stir at 600rpm for 10min to obtain the inner layer precursor solution; mix 72g styrene, 22g divinylbenzene, 109g toluene, 4.4g poloxamer and 1g AIBN, stir at 300rpm for 10min, add 14g 40wt% ethanol solution... VBTAC aqueous solution was stirred at 1000 rpm for 5 min to obtain the outer layer precursor solution; 2 g sodium dodecyl sulfate was added to 209 g deionized water and stirred at 300 rpm for 5 min to obtain the dispersion; 38 g of active microspheres were added to 284 g of inner layer precursor solution, ultrasonically dispersed at 500 W for 30 min, stirred at 600 rpm for 4.5 h, filtered, washed 3 times with toluene, added to 200 g toluene, stirred at 2000 rpm for 15 min, and then 6.5 g VTMS and 2.8 g [other components] were added. APTES and 7g of 97.5wt% ethanol solution were stirred at 500rpm for 10min. The pH was adjusted to 5.7 by adding 10wt% acetic acid solution dropwise. The mixture was stirred at 400rpm for 2h, filtered, washed three times with toluene, and added to 190g of the outer precursor solution. The mixture was stirred at 2000rpm for 15min to obtain an oil phase mixture, which was then added to the dispersion. The mixture was emulsified at 9000rpm for 15min, heated to 75℃, and stirred at 2000rpm for 3.5h. The mixture was filtered, washed three times with toluene, and then three times with anhydrous ethanol. The mixture was placed in an oven and thermally desorbed at 112℃ for 6h. The mixture was then added to 500g of 55wt% ethanol solution, stirred at 1000rpm for 20min, and then stirred at 300rpm for 2h. The mixture was filtered, washed three times with anhydrous ethanol, and dried at 58℃ and 22kPa for 11h to obtain the catalyst. The catalyst was then packed into a fixed-bed column to obtain the reaction column.

[0039] The concentration of p-hydroxybenzaldehyde in the organic waste liquid was determined by chromatography, and the mass of p-hydroxybenzaldehyde was calculated based on the volume of the organic waste liquid to be treated. The pH of the organic waste liquid was adjusted to 8.5 by adding 15wt% sodium hydroxide solution, followed by 17wt% potassium permanganate solution and stirring at 200 rpm for 2 hours. Sodium sulfite was then added and stirred at 200 rpm for 25 minutes. The mass ratio of p-hydroxybenzaldehyde, 17wt% potassium permanganate solution, and sodium sulfite in the organic waste liquid was 1:7.2:2.7. The solution was filtered, and 30wt% sulfuric acid solution was added to the filtrate to adjust... The pH value was adjusted to 6.5, and ozone was introduced into the reaction column at a rate of 1.5 BV / h. Simultaneously, ozone at a concentration of 25 mg / L was introduced into the reaction column at a rate of 0.3 L / min. Feeding was stopped when the COD value of the effluent exceeded 50 mg / L, thus completing the treatment of the organic waste liquid and obtaining purified effluent. The reaction column was then purged with nitrogen, and a 60 wt% ethanol solution was introduced into the reaction column at a rate of 1.6 BV / h. Feeding was stopped when the concentration of raspberry ketone in the effluent was less than 1% of the initial concentration, resulting in a raspberry ketone recovery solution, thereby recovering raspberry ketone from the organic waste liquid.

[0040] The active microspheres used in this embodiment were prepared in Preparation Example 3.

[0041] Example 6 Add 25g TEOS and 5g APTES to 304g of 98wt% ethanol solution, stir at 500rpm for 10min, adjust the pH to 5.7 by adding 10wt% acetic acid solution dropwise, stir at 400rpm for 1.8h, add 6g of PEG with an average molecular weight of 1300g / mol, stir at 600rpm for 10min to obtain the inner layer precursor solution; mix 72g styrene, 22g divinylbenzene, 109g toluene, 4.4g poloxamer and 1g AIBN, stir at 300rpm for 10min, add 14g 40wt% ethanol solution... VBTAC aqueous solution was stirred at 1000 rpm for 5 min to obtain the outer layer precursor solution; 2 g sodium dodecyl sulfate was added to 209 g deionized water and stirred at 300 rpm for 5 min to obtain the dispersion; 38 g of active microspheres were added to 284 g of inner layer precursor solution, ultrasonically dispersed at 500 W for 30 min, stirred at 600 rpm for 4.5 h, filtered, washed 3 times with toluene, added to 200 g toluene, stirred at 2000 rpm for 15 min, and then 6.5 g VTMS and 7 g of [unclear text - possibly a continuation of the previous sentence] were added. A 97.5 wt% ethanol solution was stirred at 500 rpm for 10 min, and the pH was adjusted to 5.7 by adding 10 wt% acetic acid solution dropwise. The mixture was stirred at 400 rpm for 2 h, filtered, washed three times with toluene, and added to 190 g of the outer precursor solution. The mixture was stirred at 2000 rpm for 15 min to obtain an oil phase mixture, which was then added to the dispersion. The mixture was stirred at 9000 rpm for 15 min to emulsify, heated to 75 °C, and stirred at 2000 rpm for 3.5 h. The mixture was filtered, washed three times with toluene, and washed three times with anhydrous ethanol. The mixture was placed in an oven and thermally desorbed at 112 °C for 6 h. The mixture was then added to 500 g of a 55 wt% ethanol solution, stirred at 1000 rpm for 20 min, and stirred at 300 rpm for 2 h. The mixture was filtered, washed three times with anhydrous ethanol, and dried at 58 °C and 22 kPa for 11 h to obtain the catalyst. The catalyst was then packed into a fixed-bed column to obtain the reaction column.

[0042] The concentration of p-hydroxybenzaldehyde in the organic waste liquid was determined by chromatography, and the mass of p-hydroxybenzaldehyde was calculated based on the volume of the organic waste liquid to be treated. The pH of the organic waste liquid was adjusted to 8.5 by adding 15wt% sodium hydroxide solution, followed by 17wt% potassium permanganate solution and stirring at 200 rpm for 2 hours. Sodium sulfite was then added and stirred at 200 rpm for 25 minutes. The mass ratio of p-hydroxybenzaldehyde, 17wt% potassium permanganate solution, and sodium sulfite in the organic waste liquid was 1:7.2:2.7. The solution was filtered, and 30wt% sulfuric acid solution was added to the filtrate to adjust... The pH value was adjusted to 6.5, and ozone was introduced into the reaction column at a rate of 1.5 BV / h. Simultaneously, ozone at a concentration of 25 mg / L was introduced into the reaction column at a rate of 0.3 L / min. Feeding was stopped when the COD value of the effluent exceeded 50 mg / L, thus completing the treatment of the organic waste liquid and obtaining purified effluent. The reaction column was then purged with nitrogen, and a 60 wt% ethanol solution was introduced into the reaction column at a rate of 1.6 BV / h. Feeding was stopped when the concentration of raspberry ketone in the effluent was less than 1% of the initial concentration, resulting in a raspberry ketone recovery solution, thereby recovering raspberry ketone from the organic waste liquid.

[0043] The active microspheres used in this embodiment were prepared in Preparation Example 3.

[0044] The present invention also includes comparative examples and related experiments.

[0045] Comparative Example 1 The difference between this comparative example and Example 5 is that potassium permanganate solution was not used to treat the organic waste liquid. The remaining operation steps and reaction conditions are the same as in Example 5, resulting in purified effluent and raspberry ketone recovery solution.

[0046] Comparative Example 2 The difference between this comparative example and Example 5 is that the active microspheres prepared in Example 3 were packed into a fixed-bed column to obtain a reaction column. The remaining operation steps and reaction conditions were the same as in Example 5, resulting in purified effluent and raspberry ketone recovery solution.

[0047] Comparative Example 3 The difference between this comparative example and Example 5 is that the outer layer precursor solution was not used to treat the active microspheres. The remaining operation steps and reaction conditions were the same as in Example 5, resulting in purified effluent and raspberry ketone recovery solution.

[0048] Comparative Example 4 The difference between this comparative example and Example 5 is that the outer precursor solution does not contain an aqueous solution of BVTAC. The remaining operating steps and reaction conditions are the same as in Example 5, resulting in purified effluent and raspberry ketone recovery solution.

[0049] Organic waste liquid treatment test p-hydroxybenzaldehyde and raspberry ketone were added to deionized water for emulsification and dispersion, with the concentration of raspberry ketone controlled at 800 mg / L and the concentration of p-hydroxybenzaldehyde at 1200 mg / L, to simulate organic waste liquid with an initial COD value of approximately 4230 mg / L.

[0050] 50g of the catalysts prepared in each example and Comparative Examples 1, 3, and 4 were packed into a fixed-bed column to obtain a reaction column. For Comparative Example 2, 50g of the active microspheres prepared in Preparation Example 3 were packed into a fixed-bed column to obtain a reaction column. 5.5L of organic waste liquid was introduced into each reaction column at a rate of 1.5 BV / h, while ozone at a concentration of 20mg / L was introduced into the reaction column at a rate of 0.2L / min to obtain purified effluent. The reaction column was then purged with nitrogen, and 1L of [unspecified substance] was introduced into the reaction column at a rate of 1.5 BV / h. A 70wt% ethanol solution was used to obtain a raspberry ketone recovery solution, which was recorded as the completion of the first cycle of the reaction column. The reaction column was then cycled multiple times. During the 1st, 5th, 15th, 30th, and 50th cycles, the COD value (mg / L) of the purified water was detected using the potassium dichromate method. The volume of the raspberry ketone recovery solution was measured, and the concentration of raspberry ketone in it was detected using chromatography, according to the following formula: Raspberry ketone yield =

[0051] The yield (%) of raspberry ketone was calculated, and the results are shown in Table 1. Figure 1 This is a chromatogram of the raspberry ketone recovery solution obtained in Example 5.

[0052] Table 1

[0053] According to Table 1 and Figure 1It can be seen that the yield of raspberry ketone in Example 5 is higher than that in Example 6, indicating that introducing a primary amino group between the inner and outer shell layers via APTES can further prevent raspberry ketone from diffusing to the active site and being decomposed and wasted. The yield of raspberry ketone in Example 5 is higher than that in Comparative Example 1, indicating that potassium permanganate can oxidize p-hydroxybenzaldehyde to p-hydroxybenzoic acid, and selectively remove p-hydroxybenzoic acid by utilizing the hydrophilicity and ionization of its carboxyl group, thus achieving effective recovery of raspberry ketone. When the reaction column is used at the same frequency, the C of the purified effluent obtained in Example 5 is higher. The OD value was lower than that of Comparative Example 2, and the yield of raspberry ketone was higher than that of Comparative Example 2. This indicates that constructing an inner shell and an outer shell layer outside the active microspheres can recover raspberry ketone while removing p-hydroxybenzoic acid, thus avoiding the decomposition and waste of raspberry ketone. Compared with Comparative Examples 3 and 4, the COD value of the purified effluent obtained in Example 5 was lower, and the yield of raspberry ketone was higher. This indicates that the outer precursor liquid containing BVTAC can form a positively charged outer shell layer outside the catalyst, which is beneficial for catalyst enrichment and retention of raspberry ketone, while accelerating the mass transfer and decomposition of p-hydroxybenzoic acid.

Claims

1. A purification process for organic waste liquid containing raspberry ketone, characterized in that, Includes the following steps: S1. Mesoporous silica is dispersed in an aqueous solution of cerium nitrate, impregnated, washed, dried, calcined, cooled, and then subjected to surface hydroxylation treatment to obtain active microspheres; S2. The active microspheres are dispersed in the inner layer precursor solution for reaction, washed, and after surface alkenylation treatment, dispersed in the outer layer precursor solution. They are then added to the dispersion solution for emulsification, heated for reaction, washed, and obtained as a catalyst after thermal removal, extraction and drying. The inner layer precursor solution is prepared by reacting TEOS and APTES under acidic conditions and then mixing them with PEG; the outer layer precursor solution is prepared by mixing styrene, divinylbenzene, toluene, poloxamer, initiator and VBTAC aqueous solution. S3. The organic waste liquid is subjected to aldehyde oxidation treatment. After adjusting the pH value, it is mixed with ozone and catalyst through a reaction column to complete the treatment of the organic waste liquid. The catalyst is then eluted to obtain a raspberry ketone recovery solution.

2. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 1, characterized in that, In step S1, mesoporous silica is dispersed in a 0.6-0.9wt% cerium nitrate aqueous solution and immersed for 10-12 hours. After washing with deionized water, it is dried in an environment of 85-95℃ for 10-12 hours, heated to 550-560℃ and calcined for 3-4 hours. After cooling, it is treated with water vapor plasma at 50-60W radio frequency power for 5-6 minutes to obtain active microspheres.

3. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 2, characterized in that, The active microspheres comprise the following raw materials in parts by weight: 40-45 parts mesoporous silica and 300-310 parts of 0.6-0.9wt% cerium nitrate aqueous solution.

4. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 1, characterized in that, The inner layer precursor solution is prepared by mixing 97-98 wt% ethanol solution, TEOS and APTES, adjusting the pH to 5.5-5.7 by adding acetic acid solution dropwise, reacting for 1.5-2 hours, adding PEG and mixing to obtain the inner layer precursor solution; the outer layer precursor solution is prepared by mixing styrene, divinylbenzene, toluene, poloxamer and initiator AIBN, dispersing in 40-45 wt% VBTAC aqueous solution to obtain the outer layer precursor solution; the average molecular weight of the PEG is 1200-1300 g / mol.

5. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 2, characterized in that, In step S2, the active microspheres are dispersed in the inner precursor solution and reacted for 4-5 hours. After washing with toluene, they are dispersed in toluene, VTMS and 97-98 wt% ethanol solution are added and mixed. Acetic acid solution is added dropwise to adjust the pH to 5.5-5.7, and the reaction is carried out for 1.5-2 hours. After washing with toluene, they are dispersed in the outer precursor solution and added to the dispersion. The mixture is emulsified at 8000-9000 rpm for 15-25 minutes, heated to 65-75℃ and reacted for 3-4 hours. After washing with toluene and anhydrous ethanol, the mixture is placed in an environment of 112-115℃ for thermal desorption for 5-6 hours. The mixture is then dispersed in a 50-55 wt% ethanol solution for extraction for 1-2 hours. After washing with anhydrous ethanol, the mixture is placed in an environment of 55-60℃ and 20-25 kPa for drying for 10-12 hours to obtain the catalyst.

6. The purification process for raspberry ketone-containing organic waste liquid according to claim 5, characterized in that, In step S2, the active microspheres that have reacted with the inner layer precursor solution are dispersed in toluene, and then VTMS, APTES and 97-98 wt% ethanol solution are added and mixed.

7. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 1, characterized in that, The catalyst comprises the following raw materials in parts by weight: 32-38 parts of active microspheres, 276-284 parts of inner layer precursor solution, 5-7 parts of VTMS, 0-3 parts of APTES, 6-8 parts of 97-98 wt% ethanol solution, and 180-190 parts of outer layer precursor solution; the inner layer precursor solution comprises the following raw materials in parts by weight: 295-304 parts of 97-98 wt% ethanol solution, 20-25 parts of TEOS, 5-7 parts of APTES, and 5-6 parts of PEG; the outer layer precursor solution comprises the following raw materials in parts by weight: 72-76 parts of styrene, 19-23 parts of divinylbenzene, 100-110 parts of toluene, 11-14 parts of 40-45 wt% BVTAC aqueous solution, and 4-5 parts of poloxamer; the dispersion comprises 200-220 parts by weight of deionized water and 2-3 parts by weight of sodium dodecyl sulfate.

8. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 1, characterized in that, The organic waste liquid is pretreated by aldehyde oxidation as follows: sodium hydroxide solution is added to the organic waste liquid to adjust the pH value to 8-8.5, 15-17wt% potassium permanganate solution is added and reacted for 1-2 hours, sodium sulfite is added and stirred for 15-25 minutes, filtered, and sulfuric acid solution is added to the filtrate to adjust the pH value to 6.5-7, thus completing the pretreatment of the organic waste liquid.

9. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 8, characterized in that, The mass ratio of p-hydroxybenzaldehyde, 15-17wt% potassium permanganate solution, and sodium sulfite in the organic waste liquid is 1:(7-7.2):(2.5-2.7).

10. The purification and treatment process for raspberry ketone-containing organic waste liquid according to claim 8, characterized in that, In step S3, the catalyst is loaded into a fixed-bed column to obtain a reaction column. The organic waste liquid after aldehyde oxidation treatment and ozone are simultaneously introduced into the reaction column to complete the treatment of the organic waste liquid and obtain purified effluent. A 60-70wt% ethanol solution is introduced into the reaction column for elution to obtain a raspberry ketone recovery solution. The flow rate of the organic waste liquid after aldehyde oxidation treatment is 1-2 BV / h; the concentration of ozone is 20-25 mg / L and the flow rate is 0.2-0.3 L / min; the flow rate of the 60-70wt% ethanol solution is 1.3-1.6 BV / h.

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