Phenolic wastewater treatment method

Abstract

The invention relates to the field of wastewater treatment, in particular to a phenol-containing wastewater treatment method. The method comprises the following steps: in the presence of a catalyst and chloride ions, carrying out contact oxidation on the phenol-containing wastewater and an oxidant; the concentration of chloride ions in the system during contact oxidation is 50-350mg / L. By adopting the method disclosed by the invention, the content of organic matters in the phenolic wastewater can be effectively reduced, the removal rate of COD in the phenolic wastewater is high, the removal rate of organic matters containing phenolic groups is high, and a better technical effect is achieved.

Description

Technical Field

[0001] The invention relates to the field of wastewater treatment, and in particular to a method for treating phenol-containing wastewater. Background Art

[0002] The hydrogenation process wastewater of the refinery contains a large amount of pollutants such as ammonia, hydrogen sulfide, oil, phenol, etc. It has complex composition, high toxicity, high COD, and is difficult to treat. Advanced oxidation technology produces hydroxyl free radicals with strong oxidizing ability to oxidize large molecular refractory organic matter into low-toxic or non-toxic small molecular substances, which is green, efficient and environmentally friendly.

[0003] Phenol is one of the most common pollutants in industrial wastewater. Due to the large-scale use of plastics, varnishes, pharmaceuticals, textiles, metallurgical products, oil, natural gas and coke ovens, phenol is involved in some stages of their production process, so almost all wastewater from these industrial units contains phenol or phenolic compounds. This has led to more and more people around the world paying attention to the source of phenol pollution.

[0004] In current research, the main methods for treating phenol wastewater at home and abroad include physical method, biological method, chemical oxidation method and electrochemical method.

[0005] The physical method uses a physical separation method to collect phenol from phenol wastewater to separate phenol from water. It has the advantages of easy operation, low investment, and economic savings. The most common physical methods are adsorption separation and solvent extraction separation. The adsorption separation method has high requirements for adsorbents, and it is necessary to select suitable adsorbents to achieve better separation effects. The extraction and separation process of the solvent extraction separation method will inevitably introduce a large amount of organic solvents, and organic solvents are difficult to completely separate from water bodies, which can easily cause secondary pollution of water bodies. At the same time, the difficulty of recycling organic solvents is also a key problem that needs to be solved in this method.

[0006] The biological method uses microorganisms to adsorb and decompose pollutants in water to purify phenol wastewater, mainly including anaerobic activated sludge method, bioaugmentation method and enzyme catalysis technology. The biological method has the advantages of low residues and by-products, but despite this, due to the toxicity of phenol to microorganisms, it is still difficult to treat phenol wastewater using existing biological methods. The chemical oxidation method oxidizes phenol into easily oxidizable intermediates, and then further completely oxidizes the intermediates into carbon dioxide and water. However, the stable chemical properties of phenol increase the difficulty of oxidation. If chemical catalysts are added, it will cause secondary pollution and other problems.

[0007] CN109133241A invention discloses a FU-type composite extractant suitable for treating coal tar hydrogenation wastewater and its application in treating coal tar hydrogenation wastewater. The composite tray and the extractant are integrated to achieve deacidification, deamination and dephenolization. However, the method has many processes and the degradation of pollutants in the wastewater is not sufficient.

[0008] 201510625617.7 discloses a method for deep treatment of phenol-cyanide wastewater, which first uses photocatalytic oxidation to oxidize and decompose COD and other substances in the wastewater, then adds solid adsorbents to adsorb residual COD, chromaticity, and especially cyanide in the wastewater, and then adds flocculants to perform coagulation and sedimentation. This method simultaneously utilizes photooxidation degradation, adsorption, and coagulation and sedimentation. The photooxidation degradation method requires conditions such as light radiation and catalysts, and has high requirements for equipment. The adsorption method uses porous solid adsorbents to adsorb harmful substances in wastewater to purify the wastewater. Porous solid adsorbents such as activated carbon and resins are relatively expensive, difficult to regenerate, and have high operating costs. Sometimes, in order to enhance the adsorption effect, it is also necessary to add iron-containing reagents, which further increases the difficulty of separating and regenerating solid adsorbents. Summary of the invention

[0009] The purpose of the present invention is to overcome the problems of low COD removal rate of phenol-containing wastewater in the prior art, especially low removal rate of organic pollutants containing phenol groups, and to provide a method for treating phenol-containing wastewater, which has the advantages of high COD removal rate and efficient removal of organic pollutants containing phenol groups in phenol-containing wastewater.

[0010] In order to achieve the above-mentioned purpose, the present invention provides a method for treating phenol-containing wastewater, which comprises: in the presence of a catalyst and chloride ions, contacting and oxidizing the phenol-containing wastewater with an oxidant; the concentration of chloride ions in the system during the contact oxidation is 50-350 mg / L.

[0011] Through the above technical solution, the present invention has the following advantages:

[0012] The method of the present invention can effectively degrade the organic matter content in phenol-containing wastewater, the COD removal rate of the phenol-containing wastewater is high, and the removal rate of organic matter containing phenol groups is high, thereby achieving good technical effects. DETAILED DESCRIPTION

[0013] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0014] The present invention provides a method for treating phenol-containing wastewater, which comprises: contacting and oxidizing the phenol-containing wastewater with an oxidant in the presence of a catalyst and chloride ions; the concentration of chloride ions in the system during the contact oxidation is 50-350 mg / L, for example, 50 mg / L, 60 mg / L, 70 mg / L, 80 mg / L, 90 mg / L, 100 mg / L, 150 mg / L, 250 mg / L, and 350 mg / L.

[0015] The method of the present invention can effectively degrade the organic matter content in phenol-containing wastewater, and the COD removal rate of the phenol-containing wastewater is high, and the removal rate of organic matter containing phenol groups is high.

[0016] According to a preferred embodiment of the present invention, the chloride ion content in the system during the contact oxidation is 50-150 mg / L, preferably 50-100 mg / L. By adopting the above preferred scheme, the COD removal rate and the removal rate of phenol-containing wastewater containing phenolic groups can be further improved.

[0017] According to a preferred embodiment of the present invention, the content of phenolic compounds in the phenol-containing wastewater is 300-5000 mg / L, preferably 500-3000 mg / L. By adopting the above preferred scheme, the COD removal rate and the removal rate of phenol-containing organic matter in the phenol-containing wastewater can be further improved.

[0018] In the present invention, the phenolic compound includes phenol and / or methylphenol.

[0019] According to a preferred embodiment of the present invention, the COD of the phenol-containing wastewater is 5000-40000 mg / L, preferably 10000-30000 mg / L.

[0020] According to a preferred embodiment of the present invention, the chloride ion content in the phenol-containing wastewater is no more than 500 mg / L.

[0021] In the present invention, the phenol-containing wastewater can be a conventional choice in the art. According to a preferred embodiment of the present invention, the phenol-containing wastewater is selected from waste oil hydrogenation wastewater and / or resin wastewater.

[0022] In the present invention, the type of the oxidant can be a conventional choice in the art. According to a preferred embodiment of the present invention, the oxidant is selected from at least one of hydrogen peroxide, oxygen, and ozone, preferably hydrogen peroxide.

[0023] According to a preferred embodiment of the present invention, when the concentration of chloride ions in the phenol-containing wastewater is less than 500 mg / L and greater than 350 mg / L, preferably greater than 150, and more preferably greater than 100, the phenol-containing wastewater is pretreated with a first chlorine precipitant and a second chlorine precipitant and then contacted with an oxidant for oxidation.

[0024] In the present invention, the type of the first chlorine precipitant can be a conventional choice in the art. According to a preferred embodiment of the present invention, the first chlorine precipitant is at least one of polyacrylamide, sodium polyacrylate, and polyaluminium chloride, preferably polyacrylamide. By adopting the above preferred scheme, the COD removal rate of phenol-containing wastewater and the removal rate of phenol-containing organic matter can be further improved.

[0025] In the present invention, the first chlorine precipitant is dissolved in a solvent such as water to a mass concentration of 2-5%.

[0026] In the present invention, the type of the second chlorine precipitant can be a conventional choice in the art. According to a preferred embodiment of the present invention, the second chlorine precipitant is copper salt and / or ascorbic acid, preferably a mixture of copper salt and ascorbic acid, and more preferably the mass ratio of copper salt to ascorbic acid in the mixture is 0.5-10. By adopting the above preferred embodiment, the COD removal rate of phenol-containing wastewater and the removal rate of phenol-containing organic matter can be further improved.

[0027] According to a preferred embodiment of the present invention, when the concentration of chloride ions in the phenol-containing wastewater is less than 500 mg / L and greater than 350 mg / L, preferably greater than 150, and more preferably greater than 100, the pretreatment step includes: adding a first chlorine precipitant to the phenol-containing wastewater for a first mixing, a first solid-liquid separation, adding a second chlorine precipitant for a second mixing, and a second solid-liquid separation. By adopting the aforementioned preferred scheme, the COD removal rate and the phenol-containing group organic matter removal rate of the phenol-containing wastewater can be further improved.

[0028] According to a preferred embodiment of the present invention, the mass ratio of the copper salt in the second chlorine precipitant added as copper ions to the chloride ions in the phenol-containing wastewater is 1-20, preferably 2-10. By adopting the above preferred scheme, the COD removal rate and the phenol-containing organic matter removal rate of the phenol-containing wastewater can be further improved.

[0029] According to a preferred embodiment of the present invention, the pH value of the liquid phase obtained by the first solid-liquid separation is adjusted to 2-5, and then a second chlorine precipitant is added. By adopting the above preferred scheme, the COD removal rate and the removal rate of phenol-containing wastewater containing phenolic groups can be further improved.

[0030] In the present invention, the first mixing conditions can be selected according to conventional techniques in the art. According to a preferred embodiment of the present invention, the first mixing conditions include: a temperature of 10-50° C., and / or a time of 5-10 min.

[0031] In the present invention, the second mixing conditions can be selected according to conventional techniques in the art. According to a preferred embodiment of the present invention, the second mixing conditions include: a temperature of 10-50° C., and / or a time of 10-30 min.

[0032] According to a preferred embodiment of the present invention, when the concentration of chloride ions in the phenol-containing wastewater is less than 50 mg / L, a chlorine source is added to make the chloride ion concentration in the system 50-100 mg / L.

[0033] In the present invention, the type of the chlorine source can be a conventional choice in the art. According to a preferred embodiment of the present invention, the chlorine source is a soluble salt of chlorine, preferably sodium chloride or potassium chloride.

[0034] According to a preferred embodiment of the present invention, the conditions of the contact reaction include: the volume of phenol-containing wastewater and H 2 O 2 The mass ratio is 20-100mL / g.

[0035] According to a preferred embodiment of the present invention, the conditions of the contact reaction include: the reaction temperature is 20-80°C, preferably 40-60°C.

[0036] According to a preferred embodiment of the present invention, the conditions of the contact reaction include: the reaction time is 0.5-4h, preferably 1-2h.

[0037] According to a preferred embodiment of the present invention, the conditions of the contact reaction include: pH 2-7, preferably 6-7.

[0038] By adopting the aforementioned preferred contact reaction conditions, the COD removal rate and the phenol-containing organic matter removal rate of phenol-containing wastewater can be further improved.

[0039] According to a preferred embodiment of the present invention, the pH regulator used in the present invention is selected from sodium hydroxide and / or sulfuric acid.

[0040] According to a preferred embodiment of the present invention, the catalyst comprises a carrier and an active component, and the active component comprises a Group VIIB metal oxide and a Group VIII metal oxide. By adopting the above preferred scheme, the COD removal rate and the removal rate of phenol-containing wastewater containing phenolic groups can be further improved.

[0041] According to a preferred embodiment of the present invention, based on 100 parts by weight, the catalyst comprises 1-95 parts of a carrier, preferably 70-95 parts of a carrier; 5-99 parts of an active component, preferably 5-30 parts of an active component.

[0042] According to a preferred embodiment of the present invention, based on 100 parts by weight, the catalyst comprises 1-5 parts of MnO2 、0.1-10 parts Fe 2 O 3 and 0.1-5 parts of CoO, and the balance is carrier.

[0043] According to a preferred embodiment of the present invention, the carrier and MnO 2 The weight ratio is (10-60):1, preferably (20-40):1.

[0044] According to a preferred embodiment of the present invention, Fe 2 O 3 and MnO 2 The weight ratio is (0.01-3):1, preferably (0.1-1):1.

[0045] According to a preferred embodiment of the present invention, CoO and MnO 2 The weight ratio is (0.01-5):1, preferably (0.1-2):1.

[0046] By adopting the above-mentioned preferred catalyst composition, the COD removal rate and the phenol-containing organic matter removal rate of phenol-containing wastewater can be further improved.

[0047] According to a preferred embodiment of the present invention, the carrier of the catalyst is selected from at least one of aluminum oxide, titanium oxide, zirconium oxide and cerium oxide, preferably titanium oxide.

[0048] The present invention will be described in detail below through examples.

[0049] In the embodiment:

[0050] COD was determined using a Hach DR3900 spectrophotometer;

[0051] The concentration of organic matter containing phenolic groups was measured by Agilent7890A gas chromatograph;

[0052] All raw materials are commercially available.

[0053] Example 1

[0054] 1. Catalyst preparation

[0055] 80 g of spherical TiO 2 The catalyst support was immersed in 100 mL of an aqueous solution containing 10 g of manganese nitrate hexahydrate, 10 g of ferric nitrate nonahydrate and 8 g of cobalt nitrate hexahydrate overnight, dried at 80° C. for 12 h, and calcined in a muffle furnace at 500° C. for 8 h to obtain a catalyst.

[0056] 2. Pretreatment: The wastewater from the waste oil hydrogenation process (chloride ion concentration 447 mg / L, phenol (including phenol methylphenol, the same below) content 3558 mg / L) was flocculated with a 2% PAM (polyacrylamide) aqueous solution, filtered after standing, and the pH of the filtrate was adjusted to 4 with a 2% sulfuric acid aqueous solution. The pretreatment agent ascorbic acid was added to each liter of the filtrate and stirred for 30 minutes, and then the filtrate I was obtained by filtering.

[0057] First chlorine precipitant: 2% PAM aqueous solution, dosage: 1mL / L wastewater;

[0058] Flocculation stirring time: 10min;

[0059] Pretreatment agent: CuSO 4 ·5H 2 O, dosage: 4g / L wastewater; ascorbic acid, dosage: 1g / L wastewater;

[0060] Pretreatment time: 30min;

[0061] Chloride ion content of material I: 75 mg / L.

[0062] 3. Advanced oxidation: 2% sodium hydroxide aqueous solution was used to adjust the pH of the filtrate (material I) to 7. In the presence of a catalyst, 30 g H 2 O 2 Oxidants

[0063] Wastewater retention time: 1h;

[0064] Fixed bed reactor volume: 520 ml;

[0065] Catalyst loading: 500 ml;

[0066] Reaction temperature: 60°C;

[0067] The reaction results are shown in Table 1.

[0068] Example 2

[0069] 1. Catalyst preparation

[0070] 80 g of spherical TiO 2 The catalyst support was immersed in 100 mL of an aqueous solution containing 13.2 g of manganese nitrate hexahydrate, 1.4 g of ferric nitrate nonahydrate and 1.55 g of cobalt nitrate hexahydrate overnight, dried at 80° C. for 12 h, and calcined in a muffle furnace at 500° C. for 8 h to obtain a catalyst.

[0071] 2. Pretreatment: The wastewater from the waste oil hydrogenation process (chloride ion concentration 447 mg / L, phenol content 3558 mg / L) was flocculated with a 5% PAM (polyacrylamide) aqueous solution, filtered after standing, and the pH of the filtrate was adjusted to 2 with a 2% sulfuric acid aqueous solution. The pretreatment agent ascorbic acid was added to each liter of the filtrate and stirred for 30 minutes, and then the filtrate I was obtained by filtering.

[0072] First chlorine precipitant: 2% PAM aqueous solution, dosage: 1mL / L wastewater;

[0073] Flocculation stirring time: 5min;

[0074] Pretreatment agent: CuSO 4 ·5H 2 O, dosage: 1.8g / L wastewater;

[0075] Ascorbic acid, dosage: 3.6 g / L wastewater;

[0076] Pretreatment time: 20min;

[0077] Chloride ion content of material I: 100 mg / L.

[0078] 3. Advanced oxidation: 2% sodium hydroxide aqueous solution was used to adjust the pH of the filtrate (material I) to 7. In the presence of a catalyst, 50 g of H2O was used per liter of filtrate. 2 O 2 Oxidants.

[0079] Wastewater retention time: 1h;

[0080] Fixed bed reactor volume: 520 ml;

[0081] Catalyst loading: 500 ml;

[0082] Reaction temperature: 50°C;

[0083] The reaction results are shown in Table 1.

[0084] Example 3

[0085] 1. Catalyst preparation

[0086] 80 g of a spherical TiO2 catalyst carrier with a diameter of 5 mm was immersed in 100 mL of an aqueous solution containing 6.6 g of manganese nitrate hexahydrate, 7 g of ferric nitrate nonahydrate and 15.5 g of cobalt nitrate hexahydrate overnight, dried at 80°C for 12 h, and calcined in a muffle furnace at 500°C for 8 hours to obtain a catalyst.

[0087] 2. Pretreatment: The waste oil hydrogenation process wastewater (chloride ion concentration 447 mg / L, phenol content 3558 mg / L) was flocculated with a 3% PAM (polyacrylamide) aqueous solution, filtered after standing, and the filtrate pH was adjusted to 5 with a 2% sulfuric acid aqueous solution. The pretreatment agent ascorbic acid was added to each liter of the filtrate and stirred for 30 minutes, and then the filtrate I was obtained by filtering.

[0088] First chlorine precipitant: 3% PAM aqueous solution, dosage: 1mL / L wastewater;

[0089] Flocculation stirring time: 10min;

[0090] Pretreatment agent: CuSO 4 ·5H 2 O, dosage: 35g / L wastewater;

[0091] Ascorbic acid, dosage: 3.5 g / L wastewater;

[0092] Pretreatment time: 10min;

[0093] Chloride ion content of material I: 50 mg / L.

[0094] 3. Advanced oxidation: 2% sodium hydroxide aqueous solution was used to adjust the pH of the filtrate (material I) to 6. In the presence of a catalyst, 10 g of H2O2 was used per liter of filtrate. 2 O 2 Oxidants.

[0095] Wastewater retention time: 1h;

[0096] Fixed bed reactor volume: 520 ml;

[0097] Catalyst loading: 500 ml;

[0098] Reaction temperature: 40°C;

[0099] The reaction results are shown in Table 1.

[0100] Example 4

[0101] The method described in Example 1 was followed, except that in step (2), CuSO 4 ·5H 2 O, dosage: 0.5g / L wastewater; ascorbic acid dosage: 4.5g / L wastewater.

[0102] The phenol content and COD in the treated wastewater and effluent were determined, and the phenol removal rate and COD removal rate were calculated. The results are shown in Table 1.

[0103] Example 5

[0104] The operation was carried out in accordance with the method described in Example 1, except that in step (2), the amount of copper sulfate pentahydrate used was 0.9 g / L wastewater.

[0105] The phenol content and COD in the treated wastewater and effluent were determined, and the phenol removal rate and COD removal rate were calculated. The results are shown in Table 1.

[0106] Example 6

[0107] The catalyst preparation and advanced oxidation operation were carried out according to the method described in Example 1, except that step (2) was replaced by using phenol wastewater without chloride ions as material I.

[0108] Phenol wastewater: phenol content 3700mg / L, no chloride ions.

[0109] Add chlorine source: sodium chloride, so that the chloride ion content of the system is: 50 mg / L.

[0110] The phenol content and COD in the treated wastewater and effluent were determined, and the phenol removal rate and COD removal rate were calculated. The results are shown in Table 1.

[0111] Example 7

[0112] The method described in Example 1 was followed, except that in the catalyst preparation step, cobalt nitrate was replaced by ferric nitrate nonahydrate (cobalt oxide was replaced by an equal mass of iron oxide).

[0113] The phenol content and COD in the treated wastewater and effluent were determined, and the phenol removal rate and COD removal rate were calculated. The results are shown in Table 1.

[0114] Comparative Example 1

[0115] The same as Example 1, except that step 2 is not performed, and the waste oil hydrogenation process wastewater is directly treated by advanced oxidation.

[0116] The phenol content and COD in the treated wastewater and effluent were determined, and the phenol removal rate and COD removal rate were calculated. The results are shown in Table 1.

[0117] Comparative Example 2

[0118] The same as Example 6, except that no chlorine source was added. The phenol content and COD in the treated wastewater and effluent were measured, and the phenol removal rate and COD removal rate were calculated. The results are shown in Table 1.

[0119] Comparative Example 3

[0120] The same as Example 1, except that the first chlorine precipitant and the second chlorine precipitant are used together with the advanced oxidation catalyst to treat the waste oil hydrogenation process wastewater.

[0121] The reaction results are shown in Table 1.

[0122] Table 1

[0123]

[0124]

[0125] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A method for treating phenol-containing wastewater, characterized in that: The method comprises: in the presence of a catalyst and chloride ions, phenol-containing wastewater is contacted with an oxidant for oxidation; The concentration of chloride ions in the system during the contact oxidation is 50-350 mg / L.

2. The processing method according to claim 1, wherein: During the contact oxidation, the chloride ion content in the system is 50-150 mg / L, preferably 50-100 mg / L.

3. The processing method according to claim 1 or 2, wherein: The COD of the phenol-containing wastewater is 5000-40000 mg / L, preferably 10000-30000 mg / L; and / or The content of phenolic compounds in the phenol-containing wastewater is 300-5000 mg / L, preferably 500-3000 mg / L, and more preferably the phenolic compounds include phenol and / or methylphenol; and / or The chloride ion content of the phenol-containing wastewater is not more than 500 mg / L; and / or The phenol-containing wastewater is selected from waste oil hydrogenation wastewater and / or resin wastewater; and / or The oxidant is selected from at least one of hydrogen peroxide, ozone and oxygen, preferably hydrogen peroxide.

4. The processing method according to any one of claims 1 to 3, wherein: When the concentration of chloride ions in the phenol-containing wastewater is less than 500 mg / L and greater than 350 mg / L, preferably greater than 150, and more preferably greater than 100, the phenol-containing wastewater is pretreated with a first chlorine precipitant and a second chlorine precipitant and then contacted with an oxidant for oxidation; Preferably, The first chlorine precipitant is at least one of polyacrylamide, sodium polyacrylate and polyaluminium chloride, preferably polyacrylamide; and / or The second chlorine precipitant is copper salt and / or ascorbic acid, preferably a mixture of copper salt and ascorbic acid, more preferably the mass ratio of copper salt to ascorbic acid in the mixture is 0.5-10.

5. The processing method according to claim 4, wherein: The pretreatment step comprises: adding a first chlorine precipitant to the phenol-containing wastewater for a first mixing, a first solid-liquid separation, adding a second chlorine precipitant for a second mixing, and a second solid-liquid separation; preferably, The mass ratio of the copper salt in the second chlorine precipitant added to the chloride ions in the phenol-containing wastewater is 1-20, preferably 2-10, in terms of copper ions; and / or adjusting the pH value of the liquid phase obtained by the first solid-liquid separation to 2-5, and then adding a second chlorine precipitant; and / or The first mixing conditions include: a temperature of 10-50° C., and / or a time of 5-10 min; and / or The second mixing conditions include: a temperature of 10-50° C., and / or a time of 10-30 min.

6. The processing method according to any one of claims 1 to 5, wherein: When the concentration of chloride ions in the phenol-containing wastewater is less than 50 mg / L, a chlorine source is added to make the chloride ion concentration in the system 50-100 mg / L. Preferably, The chlorine source is a soluble salt of chlorine.

7. The processing method according to any one of claims 1 to 6, wherein: The conditions of the contact reaction include: The ratio of the volume of phenol-containing wastewater to the mass of H2O2 is 20-100 mL / g; and / or The reaction temperature is 20-80°C, preferably 40-60°C; and / or The reaction time is 0.5-4h, preferably 1-2h; and / or The pH is 2-7, preferably 6-7.

8. The processing method according to any one of claims 1 to 7, wherein: The catalyst comprises a carrier and an active component, wherein the active component comprises a Group VIIB metal oxide and a Group VIII metal oxide. Preferably, Based on 100 parts by weight, the catalyst comprises 1-95 parts of a carrier, preferably 60-95 parts of a carrier; 5-99 parts of an active component, preferably 5-40 parts of an active component.

9. The processing method according to any one of claims 1 to 8, wherein: Based on 100 parts by weight, the catalyst comprises 1-5 parts of MnO2, 0.1-10 parts of Fe2O3 and 0.1-5 parts of CoO, and the remainder is a carrier; preferably, The weight ratio of the carrier to MnO2 is (10-60):1, preferably (20-40):1; and / or The weight ratio of Fe2O3 to MnO2 is (0.01-3):1, preferably (0.1-1):1; and / or The weight ratio of CoO to MnO2 is (0.01-5):1, preferably (0.1-2):

1.

10. The processing method according to any one of claims 1 to 9, wherein: The carrier of the catalyst is selected from at least one of aluminum oxide, titanium oxide, zirconium oxide and cerium oxide, preferably titanium oxide.

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