CN113845201B - Si-Fe/gamma-Al 2 O 3 Application of catalyst in degradation of phenol-containing wastewater - Google Patents
Si-Fe/gamma-Al 2 O 3 Application of catalyst in degradation of phenol-containing wastewater Download PDFInfo
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Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
- B01J23/745—Iron
-
- B01J35/615—
-
- B01J35/633—
-
- B01J35/647—
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
- C02F2101/345—Phenols
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
The invention discloses a Si-Fe/gamma-Al 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater comprises the following steps: s1: regulating pH of the phenolic wastewater to 2.5-3.5, and adding Si-Fe/gamma-Al 2 O 3 Stirring and dispersing the catalyst, and then dropwise adding H 2 O 2 Stirring the solution uniformly to obtain mixed reaction suspension; s2: and magnetically stirring and mixing the reaction suspension at 20-35 ℃ for 40-80 min to finish the catalytic wet oxidation degradation process. The invention uses Si-Fe/gamma-Al for the first time 2 O 3 The catalyst is used as a heterogeneous catalyst for catalyzing wet oxidation of phenolic wastewater, and can rapidly and efficiently degrade phenolic compounds under the conditions of low temperature and normal pressure, and the method adopts Si element as a cocatalyst, fe element as an active component and gamma-Al for the first time 2 O 3 Si-Fe/gamma-Al prepared for a support 2 O 3 The catalyst has good degradation effect on the COD of the phenolic wastewater, is easy to separate, can be used for a second time, effectively reduces the wastewater treatment cost and is beneficial to sustainable development.
Description
Technical Field
The invention belongs to the technical field of phenol-containing wastewater treatment, and in particular relates to Si-Fe/gamma-Al 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater.
Background
The phenol-containing wastewater is wastewater mainly containing volatile phenol and non-volatile phenol discharged in the industrial production process, and mainly originates from industries such as coking, oil refining, petrochemical industry, gas power stations, plastics, resins, insulating materials, wood corrosion prevention, pesticides, chemical industry, papermaking, synthetic fibers and the like. The phenol-containing wastewater has the characteristics of high toxicity, difficult degradation and the like, and when the phenol compounds enter the human body and react correspondingly, the cell denaturation or cell inactivation is caused, and even the tissue protein coagulation is caused. Long-term drinking of phenol-contaminated water can cause chronic accumulated poisoning, and even if the phenol concentration in drinking water is only 0.002mg/L, the phenol concentration can also be harmful to human health. Phenolic compounds also have poisoning effects on aquatic organisms, crops, for example: when the concentration of phenol in rivers and lakes reaches 0.1-0.2 mg/L, fish and shrimp have odor and cannot be eaten; when the concentration of phenol is increased to 1mg/L, fish spawning can be affected; when the concentration is increased to 6.5-9.3 mg/L, the fishes die in a large amount; when field crops are irrigated with water sources having phenol concentrations in excess of 100mg/L, significant reductions in crop yield and even death of the crop can result. Therefore, how to treat the phenol-containing wastewater with high toxicity and difficult degradation efficiently and simply, realize sustainable development and have great significance for environmental protection.
At present, the degradation technology of the phenol-containing wastewater mainly comprises wet air oxidation technology, catalytic wet oxidation technology, photocatalytic oxidation technology, ozone catalytic oxidation technology and the like. Wherein, the wet air oxidation technology is called WAO for short, and organic matters are oxidized into CO 2 And H 2 O or small molecular substances are further removed to achieve the aim of purifying the wastewater, the purification effect is good, the oxidation speed is high, the application field is wide, the secondary pollution is small, but WAO needs to be degraded at the high temperature of 125-320 ℃ and the high pressure condition of 0.5-20 MPa, the energy consumption is high, and the equipment cost is high; the catalytic wet oxidation technology is called CWAO for short, on the basis of WAO, a catalyst is introduced to reduce the activation energy of the reaction, and meanwhile, the degradation rate of organic matters is accelerated, so that the method has the advantages of wide application field, low energy consumption, small secondary pollution, no sludge generation and the like, but the degradation effect is often not ideal due to the difference of the types of the catalyst; the photo-catalytic oxidation technology is to perform photo-oxidation under the action of a photo-catalyst, wherein the photo-catalyst generates electron hole pairs after light irradiation, hydroxyl groups or water are adsorbed, active centers are formed on the surface, organic substances such as phenols in the water are adsorbed, and then higher-activity OH is formed, and the phenols are oxidized and decomposed, but the traditional TiO 2 The photocatalyst has no visible light catalytic activity and has a photocatalytic effect only under the excitation action of ultraviolet rays; the ozone catalytic oxidation technology is that ozone forms a large amount of hydroxyl free radicals (OH) under the action of a catalyst, and organic matters are oxidized by utilizing the free radicals, but an ozone generator has high energy consumption, easy damage and high equipment and treatment cost, and a single ozone catalytic oxidation reaction has selectivity and poor degradation effect on chlorophenols and naphthols.
Based on the above, the invention uses Si-Fe/gamma-Al for the first time 2 O 3 Catalyst as heterogeneous catalystThe phenolic compound can be rapidly and efficiently degraded under the condition of low temperature and normal pressure by chemical wet oxidation of phenolic wastewater, when the reaction temperature is 30 ℃, the pH value of the phenolic wastewater is 3.5, 1.5mL of H with mass concentration of 30% is added 2 O 2 The mass ratio of Si element to Fe element in the solution and the catalyst is 0.1, when the adding amount of the catalyst is 0.15g, the activation energy of the reaction can be effectively reduced, the phenolic wastewater is efficiently catalyzed and degraded, and the COD removal rate reaches 82.85%. Fe/gamma-Al containing less Si element 2 O 3 The COD removal rate of the catalyst to the phenolic wastewater is 65.78%, and the removal rate is greatly improved.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a Si-Fe/gamma-Al 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater.
The technical scheme of the invention is summarized as follows:
Si-Fe/gamma-Al 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater comprises the following steps:
s1: regulating pH of the phenolic wastewater to 2.5-3.5, and adding Si-Fe/gamma-Al 2 O 3 Stirring and dispersing the catalyst, and then dropwise adding H 2 O 2 Stirring the solution uniformly to obtain mixed reaction suspension;
s2: and magnetically stirring and mixing the reaction suspension at 20-35 ℃ for 40-80 min to finish the catalytic wet oxidation degradation process.
Preferably, the concentration of phenolic substances in the phenolic wastewater is 0.5-300 mg/L.
Preferably, the phenolic substance comprises one or more of phenol, cresol, xylenol, aminophenol, benzenediol, nitrophenol, chlorophenol and naphthol.
Preferably, the Si-Fe/gamma-Al 2 O 3 The catalyst takes Si element as a cocatalyst, fe element as an active component and gamma-Al 2 O 3 Is a carrier; the Si element, fe element and gamma-Al 2 O 3 The mass ratio of (0.05-0.2): 1:10.
preferably, the Si-Fe/gamma-Al 2 O 3 A method for preparing a catalyst comprising the steps of:
s1: crushing boehmite into particles with the particle size of 0.250-0.425 mm to obtain boehmite powder for standby;
s2: heating boehmite powder to 550-650 ℃ at a speed of 5-10 ℃/min, and heating at constant temperature for 3-6 h to prepare gamma-Al 2 O 3 Powder;
s3: dissolving structure directing agent in deionized water, and adding Fe (NO) 3 ) 3 ·9H 2 O, after stirring until the mixture is completely dissolved, dripping tetraethyl orthosilicate, and uniformly stirring to obtain a mixed solution;
s4: to gamma-Al 2 O 3 Dropwise adding the mixed solution obtained in the step S3 into the powder, and stirring and reacting for 6-18 h at 25 ℃ to obtain a catalyst precursor;
s5: drying the catalyst precursor at 80-120 deg.c, transferring into crucible, covering, roasting in muffle furnace at 400-500 deg.c for 3-5 hr, and naturally cooling to 25 deg.c to obtain Si-Fe/gamma-Al 2 O 3 A catalyst.
Preferably, the structure directing agent comprises one or more of polyethylene glycol, cetyltrimethylammonium bromide, triblock copolymer P123, triblock copolymer F127.
Preferably, the structure directing agent, deionized water, fe (NO 3 ) 3 ·9H 2 O, tetraethyl orthosilicate, gamma-Al 2 O 3 The dosage proportion of the powder is (0.08-0.15) g: (4-5) mL:3.6173g: (0.1854-0.7418) g:5.0g.
Preferably, the H 2 O 2 The mass concentration of the solution is 25-35%.
Preferably, the phenol-containing wastewater, si-Fe/gamma-Al 2 O 3 Catalyst, H 2 O 2 The dosage ratio of the solution is 50mL: (0.12-0.18) g: (1.0-3.5) mL.
Preferably, the phenol-containing wastewater, si-Fe/gamma-Al 2 O 3 Catalyst, H 2 O 2 The dosage ratio of the solution is 50mL:0.15g:1.5mL.
The invention has the beneficial effects that:
1. the invention uses Si-Fe/gamma-Al for the first time 2 O 3 The catalyst is used as a heterogeneous catalyst for catalyzing wet oxidation of phenolic wastewater, phenolic compounds can be rapidly and efficiently degraded under the conditions of low temperature and normal pressure, when the reaction temperature is 30 ℃, the pH of the phenolic wastewater is 3.5, 1.5mL of H with mass concentration of 30% is added 2 O 2 The mass ratio of Si element in the solution and the catalyst is 0.1, when the adding amount of the catalyst is 0.15g, the activation energy of the reaction can be effectively reduced, the phenol-containing wastewater is efficiently catalyzed and degraded, and the COD removal rate reaches 82.85%. Fe/gamma-Al containing less Si element 2 O 3 The removal rate of the catalyst to COD is 65.78%, and the removal rate of COD is greatly improved.
2. Si-Fe/gamma-Al of the invention 2 O 3 The catalyst takes Si element as a cocatalyst for the first time, fe element as an active component and gamma-Al 2 O 3 The carrier has good degradation effect on the COD of the phenolic wastewater, is easy to separate, can be used secondarily, effectively reduces the wastewater treatment cost, is beneficial to sustainable development, and has the following action mechanism:
Si-Fe/γ-Al 2 O 3 catalyst +H 2 O 2 →O 2 +H 2 O+·OH
RH→R － +H +
R － +·OH→CO 2 +H 2 O (R represents a phenolic substance).
The catalytic degradation effect of the catalyst on phenolic compounds is greatly improved due to the doping of Si element. The reason for this is that: on the one hand, the outermost layer of the Si element has a hollow orbit which can accept electron pairs, so that the surface of the catalyst presents Lewis acid property, and the acidity and alkalinity of the surface of the catalyst are further changed, so that Si-Fe/gamma-Al is realized 2 O 3 The catalyst has electrophilic properties, and the phenolic compound is used as an electron pair donor, thus the Si-Fe/gamma-Al 2 O 3 The catalyst has high selectivity and catalytic activity on phenolic compounds, so that the catalytic degradation effect on phenolic wastewater is effectively improved; on the other hand, due to the partial hydrolysis of tetraethyl orthosilicate, in gamma-Al 2 O 3 Mesoporous SiO is formed on the surface of the carrier 2 The microphase structure further improves the specific surface area of the catalyst and the adsorption performance of the catalyst on phenolic substances, so that the catalyst is fully contacted with the phenolic substances, and further improves the catalytic degradation effect.
Drawings
FIG. 1 shows the Si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 Catalyst and Fe/gamma-Al prepared in comparative example 1 2 O 3 SEM spectrum of catalyst, wherein (a) represents Fe/gamma-Al prepared in comparative example 1 2 O 3 (b) represents Si obtained in example 1 0.05 -Fe/γ-Al 2 O 3 (c) Si obtained in example 2 0.10 -Fe/γ-Al 2 O 3 (d) represents Si obtained in example 3 0.20 -Fe/γ-Al 2 O 3 ；
FIG. 2 shows the Si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 Catalyst and Fe/gamma-Al prepared in comparative example 1 2 O 3 Adsorption isotherms of the catalyst;
FIG. 3 shows the Si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 Catalyst and Fe/gamma-Al prepared in comparative example 1 2 O 3 Pore size distribution of the catalyst;
FIG. 4 shows Si-Fe/γ -Al produced in examples 1 to 3 and comparative example 1 2 O 3 XRD patterns of the catalyst;
FIG. 5 is a plot showing the effect of reaction temperature on COD removal rate of phenol wastewater in examples 4 to 6 and comparative example 2;
FIG. 6 shows H in examples 6, 8 to 10 and comparative example 3 2 O 2 A line diagram of the influence of the dosage on the COD removal rate of the phenol wastewater;
FIG. 7 is a graph showing the effect of pH on COD removal rate of phenol wastewater in examples 6, 11 to 12 and comparative examples 4 to 5;
FIG. 8 shows the Si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 Catalyst and Fe/gamma-Al prepared in comparative example 1 2 O 3 A bar graph of the removal rate of the catalyst to the COD of the phenol wastewater;
FIG. 9 shows Si-Fe/gamma-Al of the present invention 2 O 3 Preparation of the catalystA method flow chart.
FIG. 10 shows Si-Fe/gamma-Al of the present invention 2 O 3 An application flow chart of the catalyst in the degradation of phenol-containing wastewater.
Detailed Description
The present invention is described in further detail below with reference to examples to enable those skilled in the art to practice the same by referring to the description.
The invention provides an embodiment of Si-Fe/gamma-Al 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater comprises the following steps:
s1: adjusting the pH value of the phenol-containing wastewater to be between 0.5 and 300mg/L to be between 2.5 and 3.5, and then adding Si-Fe/gamma-Al 2 O 3 Stirring and dispersing the catalyst, and then dropwise adding H with the mass concentration of 25-35% 2 O 2 Stirring the solution uniformly to obtain mixed reaction suspension; the phenolic substances in the phenolic wastewater comprise one or more of phenol, cresol, xylenol, aminophenol, benzenediol, nitrophenol, chlorophenol and naphthol; the phenolic wastewater and Si-Fe/gamma-Al 2 O 3 Catalyst, H 2 O 2 The dosage ratio of the solution is 50mL: (0.12-0.18) g: (1.0-3.5) mL; further, the phenolic wastewater and Si-Fe/gamma-Al 2 O 3 Catalyst, H 2 O 2 The dosage ratio of the solution is 50mL:0.15g:1.5mL;
s2: magnetically stirring and mixing the reaction suspension at 20-35 ℃ for 40-80 min to finish the catalytic wet oxidation and degradation process, determining the COD of the phenolic wastewater before and after the catalyst treatment by using a potassium dichromate method, and calculating the COD removal rate (E) according to a formula (I):
wherein, COD 0 Is the initial COD of the phenolic wastewater, COD 1 The COD of the phenol-containing wastewater treated by the catalyst is added.
Si-Fe/gamma-Al used in this example 2 O 3 The catalyst takes Si element as a cocatalyst and Fe element as a catalyst promoterActive component, gamma-Al 2 O 3 Is a carrier; the Si element, fe element and gamma-Al 2 O 3 The mass ratio of (0.05-0.2): 1:10; the Si-Fe/gamma-Al 2 O 3 A method for preparing a catalyst comprising the steps of:
s1: crushing boehmite into particles with the particle size of 0.250-0.425 mm to obtain boehmite powder for standby;
s2: heating boehmite powder to 550-650 ℃ at a speed of 5-10 ℃/min, and heating at constant temperature for 3-6 h to prepare gamma-Al 2 O 3 Powder;
s3: dissolving structure directing agent in deionized water, and adding Fe (NO) 3 ) 3 ·9H 2 O, after stirring until the mixture is completely dissolved, dripping tetraethyl orthosilicate, and uniformly stirring to obtain a mixed solution; the structure directing agent comprises one or more of polyethylene glycol, cetyl trimethyl ammonium bromide, triblock copolymer P123 and triblock copolymer F127;
s4: to gamma-Al 2 O 3 Dropwise adding the mixed solution obtained in the step S3 into the powder, and stirring and reacting for 6-18 h at 25 ℃ to obtain a catalyst precursor; the structure directing agent, deionized water, fe (NO) 3 ) 3 ·9H 2 O, tetraethyl orthosilicate, gamma-Al 2 O 3 The dosage proportion of the powder is (0.08-0.15) g: (4-5) mL:3.6173g: (0.1854-0.7418) g:5.0g;
s5: drying the catalyst precursor at 80-120 deg.c, transferring into crucible, covering, roasting in muffle furnace at 400-500 deg.c for 3-5 hr, and naturally cooling to 25 deg.c to obtain Si-Fe/gamma-Al 2 O 3 A catalyst.
Example 1 preparation of Si 0.05 -Fe/γ-Al 2 O 3 Catalyst
S1: crushing boehmite into particles with the particle size of 0.250-0.425 mm to obtain boehmite powder for standby;
s2: heating boehmite powder to 550 ℃ at a speed of 5 ℃/min, and heating at constant temperature for 3 hours to prepare gamma-Al 2 O 3 Powder;
s3: 0.1g of hexadecaneThe trimethylammonium bromide was dissolved in 4mL deionized water, and 3.6173g Fe (NO) 3 ) 3 ·9H 2 O, after stirring until the mixture is completely dissolved, dropwise adding 0.1854g of tetraethyl orthosilicate, and uniformly stirring to obtain a mixed solution;
s4: to 5.0g of gamma-Al 2 O 3 Dropwise adding the mixed solution obtained in the step S3 into the powder, and stirring at 25 ℃ for reacting for 12 hours to obtain a catalyst precursor;
s5: drying the catalyst precursor at 120 ℃, transferring into a crucible, covering, putting into a muffle furnace, roasting at 500 ℃ for 4 hours, naturally cooling to room temperature at 25 ℃ to obtain the Si-Fe/gamma-Al 2 O 3 A catalyst in which Si element, fe element, gamma-Al 2 O 3 The mass ratio of (2) is 0.05:1:10.
EXAMPLE 2 preparation of Si 0.10 -Fe/γ-Al 2 O 3 Catalyst
S1: crushing boehmite into particles with the particle size of 0.250-0.425 mm to obtain boehmite powder for standby;
s2: heating boehmite powder to 600 ℃ at a speed of 5 ℃/min, and heating at constant temperature for 4 hours to prepare gamma-Al 2 O 3 Powder;
s3: 0.1g of polyethylene glycol 4000 was dissolved in 4mL of deionized water, and 3.6173g of Fe (NO) 3 ) 3 ·9H 2 O, after stirring until the mixture is completely dissolved, dropwise adding 0.3709g of tetraethyl orthosilicate, and uniformly stirring to obtain a mixed solution;
s4: to 5.0g of gamma-Al 2 O 3 Dropwise adding the mixed solution obtained in the step S3 into the powder, and stirring at 25 ℃ for reacting for 12 hours to obtain a catalyst precursor;
s5: drying the catalyst precursor at 120 ℃, transferring into a crucible, covering, putting into a muffle furnace, roasting at 500 ℃ for 4 hours, naturally cooling to room temperature at 25 ℃ to obtain the Si-Fe/gamma-Al 2 O 3 A catalyst in which Si element, fe element, gamma-Al 2 O 3 The mass ratio of (2) is 0.1:1:10.
EXAMPLE 3 preparation of Si 0.20 -Fe/γ-Al 2 O 3 Catalyst: the procedure is as in example 2, with the difference that: use of tetraethyl orthosilicateThe amount of Si-Fe/gamma-Al is 0.7418g 2 O 3 Si element, fe element and gamma-Al element of catalyst 2 O 3 The mass ratio of (2) is 0.2:1:10.
comparative example 1 preparation of Fe/gamma-Al 2 O 3 Catalyst: the procedure is as in example 2, with the difference that: in S3, tetraethyl orthosilicate is not added.
Physicochemical analyses of the catalysts prepared in examples 1 to 3 and comparative example 1 were performed as shown in table 1:
TABLE 1
| Specific surface area (m) 2 ·g -1 ) | Average pore diameter (nm) | Pore volume (mL. G) -1 ) | |
| Comparative example 1 | 198.3409 | 4.9778 | 0.296780 |
| Example 1 | 184.4339 | 5.4895 | 0.298924 |
| Example 2 | 182.6367 | 5.2452 | 0.263968 |
| Example 3 | 195.8779 | 5.1391 | 0.291877 |
As is clear from Table 1, si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 The catalyst has a nano-scale microporous structure, and the specific surface area is between 180 and 200m 2 ·g -1 Has a certain adsorption effect on phenolic pollutants.
The Si produced in example 2 was used in examples 4 to 12 and comparative examples 1 to 5 below 0.10 -Fe/γ-Al 2 O 3 The catalyst degrades phenol wastewater, the concentration of the phenol wastewater to be treated is 100mg/L, and the initial COD of the phenol wastewater is measured by a potassium dichromate method in advance and is recorded as COD 0 。
Examples 4 to 6 and comparative example 2 study of the effect of reaction temperature on COD degradation of phenol wastewater
Example 4
S1: 50mL of 100mg/L phenol wastewater was adjusted to pH 3.5, and 0.15. 0.15gSi was added 0.10 -Fe/γ-Al 2 O 3 After stirring and dispersing the catalyst, 1.5mL of H with the mass concentration of 30% is added dropwise 2 O 2 Stirring the solution uniformly to obtain mixed reaction suspension;
s2: the reaction suspension is magnetically stirred and mixed at 20 ℃ for 60min, thus completing the catalytic wet oxidation degradation process, and the COD of the phenol wastewater treated by the catalyst is measured by a potassium dichromate method and is recorded as COD 1 And calculating the COD removal rate (E) according to the formula (I):
example 5 is identical to example 4, except that in S2 the reaction temperature is 25 ℃.
Example 6 is identical to example 4, except that in S2 the reaction temperature is 30 ℃.
Example 7 is identical to example 4, except that in S2 the reaction temperature is 35 ℃.
Comparative example 2 was the same as example 4 except that in S2, the reaction temperature was 45 ℃.
FIG. 5 is a plot showing the effect of reaction temperature on COD removal rate of phenol wastewater for examples 4 to 7 and comparative example 2: as can be seen from fig. 5, as the reaction temperature increases, the COD removal rate of the phenol-simulated wastewater shows positive correlation, and after reaching the peak, the two begin to show negative correlation. When the reaction temperature is increased from 20 ℃ to 30 ℃, the activity of the catalyst can be increased by increasing the temperature, the activation energy of the reaction can be effectively reduced, and the reaction is promoted. When the temperature exceeds 30 ℃, the Si is caused to rise 0.10 -Fe/γ-Al 2 O 3 The activity of the catalyst is reduced, H is caused by overhigh temperature 2 O 2 The solution is decomposed, so that the concentration of OH is reduced, side reaction occurs, and the reaction rate of positive reaction is reduced. As can be seen from fig. 5, when the water bath temperature is 30 ℃, the removal rate of the phenol wastewater COD can reach a peak value, and under the condition, the activity of the catalyst is the best, the maximum catalytic effect can be achieved, and the removal rate is the maximum and reaches 82.85%.
EXAMPLES 6, 8 TO 10 and COMPARATIVE EXAMPLE 3 study H 2 O 2 Influence of the amount on COD degradation of phenol wastewater
Example 8 is the same as example 6, except that in S1, H 2 O 2 The dosage is 1.0mL.
Example 9 is the same as example 6, except that in S1, H 2 O 2 The dosage is 2.0mL.
Example 10 is the same as example 6, except that in S1, H 2 O 2 The dosage is 3.5mL.
Comparative example 3 is the same as example 6 except that H is not added in S1 2 O 2 。
FIG. 6 shows H in examples 6, 8 to 10 and comparative example 3 2 O 2 Removal of COD from phenol wastewater by using amountImpact line graph of rate: as can be seen from fig. 6, as H is added 2 O 2 The volume of the solution is gradually increased, the COD removal rate of the phenol simulated wastewater is positive correlation firstly, and the phenol simulated wastewater reaches a peak value, and the phenol simulated wastewater and the COD removal rate are negative correlation and gradually tend to be balanced. When H is 2 O 2 When the addition amount of the solution is small, H is added along with 2 O 2 The amount of OH to be used increases, but when H is added 2 O 2 After the solution exceeds 1.5mL, H is added 2 O 2 Solution-formed OH and residual H 2 O 2 The solution reacts to form OH with a rate slightly less than H 2 O 2 The rate of consumption of the reaction, and thus the degradation reaction, si 0.10 -Fe/γ-Al 2 O 3 The degradation rate of the catalyst is somewhat reduced when H is added 2 O 2 After the solution exceeds 2mL, the rate of formation of OH is substantially equal to H 2 O 2 The rate at which the solution is consumed by the reaction and therefore the rate of degradation of the catalyst is substantially unchanged. As is evident from fig. 6, when H is added 2 O 2 When the solution is 1.5mL, the removal rate of the phenol simulated wastewater COD can reach a peak value, at the moment, the activity of the catalyst is best, the resource saving is facilitated, the catalytic effect is best, and the removal rate is maximum and reaches 82.85%.
Examples 6, 11 to 12 and comparative examples 4 to 5 examined the effect of pH on COD degradation of phenol wastewater
Example 11 is the same as example 6 except that in S1, the pH of the phenol wastewater is adjusted to 2.5.
Example 12 is the same as example 6 except that in S1, the pH of the phenol wastewater is adjusted to 3.0.
Comparative example 4 is the same as example 6 except that in S1, the pH of the phenol wastewater is adjusted to 2.0.
Comparative example 5 is the same as example 6 except that in S1, the pH of the phenol wastewater is adjusted to 4.0.
FIG. 7 is a graph showing the effect of pH on COD removal rate of phenol wastewater in examples 6, 11 to 12 and comparative examples 4 to 5: as can be seen from FIG. 7, as the pH of the phenol wastewater gradually increases, the phenol simulates the COD removal of the wastewaterThe positive correlation is presented first, and after the peak value is reached, the positive correlation and the negative correlation are presented again. When the pH is small, H in the solution + Higher concentration inhibits forward progress of phenol decomposition reaction, while when the pH is higher, OH in the solution － Can affect the adsorption and decomposition of phenol on the surface of the catalyst. As is clear from FIG. 7, when the pH of the phenol wastewater was 3.5, the removal rate of the phenol-simulated wastewater COD reached the peak value, and the activity of the catalyst was the best, the maximum catalytic effect was achieved, and the removal rate was the maximum, which was 82.85%.
Study of the Effect of the catalysts of examples 1 to 3 and comparative example 1 with different Si contents on the COD degradation of phenol wastewater
Since the catalyst used in example 6 is Si in example 2 0.10 -Fe/γ-Al 2 O 3 The catalyst, therefore, was used as the degradation treatment test of example 2, and Si in example 1 was measured as in example 6 0.05 -Fe/γ-Al 2 O 3 Catalyst, si in example 3 0.20 -Fe/γ-Al 2 O 3 Catalyst, fe/gamma-Al in comparative example 1 2 O 3 The catalyst has COD degradation effect on phenol wastewater.
FIG. 8 shows the Si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 Catalyst and Fe/gamma-Al prepared in comparative example 1 2 O 3 Bar graph of catalyst to phenol wastewater COD removal rate: as can be seen from fig. 8, when the mass ratio of Si to Fe is 0.1:1, namely the removal rate of the catalyst prepared in the embodiment 2 to the COD of the phenol wastewater is maximum and reaches 82.85%, and the catalytic oxidation effect is optimal; meanwhile, si-Fe/gamma-Al produced in examples 1 to 3 2 O 3 The degradation effect of the catalyst on phenol wastewater is obviously better than that of Fe/gamma-Al in comparative example 1 2 O 3 Catalyst, which illustrates Si element doping for Fe/gamma-Al 2 O 3 The catalytic activity of the catalyst has a great improving effect, and when the mass ratio of Si to Fe is 0.2:1, the excessive tetraethyl orthosilicate aggravates the hydrolysis reaction, so that the SiO on the surface of the catalyst 2 The content is too high, but on the contrary, for Fe element or Fe 3+ Has certain embedding shielding effect and reduces the catalytic activity.
Examples 4 to 12 for the first time with Si-Fe/gamma-Al 2 O 3 The catalyst is used as a heterogeneous catalyst for catalyzing wet oxidation of phenolic wastewater, phenolic compounds can be rapidly and efficiently degraded under the conditions of low temperature and normal pressure, when the reaction temperature is 30 ℃, the pH of the phenolic wastewater is 3.5, 1.5mL of H with mass concentration of 30% is added 2 O 2 The mass ratio of Si element to Fe element in the solution and the catalyst is 0.1, when the adding amount of the catalyst is 0.15g, the activation energy of the reaction can be effectively reduced, the phenolic wastewater is efficiently catalyzed and degraded, and the COD removal rate reaches 82.85%.
Si-Fe/gamma-Al in examples 1 to 12 2 O 3 The catalyst takes Si element as a cocatalyst for the first time, fe element as an active component and gamma-Al 2 O 3 The carrier has good degradation effect on the COD of the phenolic wastewater, is easy to separate, can be used secondarily, effectively reduces the wastewater treatment cost, is beneficial to sustainable development, and has the following action mechanism:
Si-Fe/γ-Al 2 O 3 catalyst +H 2 O 2 →O 2 +H 2 O+·OH
RH→R － +H +
R － +·OH→CO 2 +H 2 O (R represents a phenolic substance).
On one hand, the outermost layer of Si element has empty orbit which can accept electron pair, so that the surface of the catalyst presents Lewis acid property, and the acidity and alkalinity of the surface of the catalyst are changed, so that Si-Fe/gamma-Al is realized 2 O 3 The catalyst has electrophilic properties, and the phenolic compound is used as an electron pair donor, thus the Si-Fe/gamma-Al 2 O 3 The catalyst has high selectivity and catalytic activity on phenolic compounds, so that the catalytic degradation effect on phenolic wastewater is effectively improved; on the other hand, due to the partial hydrolysis of tetraethyl orthosilicate, in gamma-Al 2 O 3 Mesoporous SiO is formed on the surface of the carrier 2 The microphase structure further improves the specific surface area of the catalyst and the adsorption performance of the catalyst on phenols, so that the catalyst and the phenolsThe substances are fully contacted, so that the catalytic degradation effect is improved.
Although embodiments of the present invention have been disclosed above, it is not limited to the use of the description and embodiments, it is well suited to various fields of use for the invention, and further modifications may be readily apparent to those skilled in the art, and accordingly, the invention is not limited to the particular details without departing from the general concepts defined in the claims and the equivalents thereof.
Claims (6)
1. Si-Fe/gamma-Al 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater is characterized by comprising the following steps:
s1: regulating pH of the phenolic wastewater to 2.5-3.5, and adding Si-Fe/gamma-Al 2 O 3 Stirring and dispersing the catalyst, and then dropwise adding H 2 O 2 Stirring the solution uniformly to obtain mixed reaction suspension;
s2: magnetically stirring and mixing the reaction suspension at 20-35 ℃ for 40-80 min to finish the catalytic wet oxidation degradation process;
the Si-Fe/gamma-Al 2 O 3 The catalyst takes Si element as a cocatalyst, fe element as an active component and gamma-Al 2 O 3 Is a carrier; the Si element, fe element and gamma-Al 2 O 3 The mass ratio of (0.05-0.2): 1:10;
the Si-Fe/gamma-Al 2 O 3 A method for preparing a catalyst comprising the steps of:
s1: crushing boehmite into particles with the particle size of 0.250-0.425 mm to obtain boehmite powder for standby;
s2: heating boehmite powder to 550-650 ℃ at a speed of 5-10 ℃/min, and heating at constant temperature for 3-6 h to prepare gamma-Al 2 O 3 Powder;
s3: dissolving structure directing agent in deionized water, and adding Fe (NO) 3 ) 3 ·9H 2 O, after stirring until the mixture is completely dissolved, dripping tetraethyl orthosilicate, and uniformly stirring to obtain a mixed solution;
s4: to gamma-Al 2 O 3 Dropwise adding the mixed solution obtained in the step S3 into the powder, and stirring and reacting for 6-18 h at 25 ℃ to obtain a catalyst precursor;
s5: drying the catalyst precursor at 80-120 deg.c, transferring into crucible, covering, roasting in muffle furnace at 400-500 deg.c for 3-5 hr, and naturally cooling to 25 deg.c to obtain Si-Fe/gamma-Al 2 O 3 A catalyst;
the structure directing agent, deionized water, fe (NO) 3 ) 3 ·9H 2 O, tetraethyl orthosilicate, gamma-Al 2 O 3 The dosage proportion of the powder is (0.08-0.15) g: (4-5) mL:3.6173g: (0.1854-0.7418) g:5.0g;
the phenolic wastewater and Si-Fe/gamma-Al 2 O 3 Catalyst, H 2 O 2 The dosage ratio of the solution is 50mL: (0.12-0.18) g: (1.0-3.5) mL.
2. A Si-Fe/gamma-Al according to claim 1 2 O 3 The application of the catalyst in the degradation of the phenolic wastewater is characterized in that the concentration of phenolic substances in the phenolic wastewater is 0.5-300 mg/L.
3. A Si-Fe/gamma-Al according to claim 2 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater is characterized in that the phenolic substances comprise one or more of phenol, cresol, xylenol, aminophenol, benzenediol, nitrophenol, chlorophenol and naphthol.
4. A Si-Fe/gamma-Al according to claim 1 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater is characterized in that the structure directing agent comprises one or more of polyethylene glycol, cetyltrimethylammonium bromide, triblock copolymer P123 and triblock copolymer F127.
5. A Si-Fe/gamma-Al according to claim 1 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater,characterized in that the H 2 O 2 The mass concentration of the solution is 25-35%.
6. A Si-Fe/gamma-Al according to claim 1 2 O 3 The application of the catalyst in the degradation of phenol-containing wastewater is characterized in that the phenol-containing wastewater and Si-Fe/gamma-Al 2 O 3 Catalyst, H 2 O 2 The dosage ratio of the solution is 50mL:0.15g:1.5mL.
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