Preparation method of catalyst for removing chlorophenol pollutants in organic solid waste gas

Abstract

The invention discloses a preparation method of a catalyst for removing chlorophenol pollutants in organic solid waste fuel gas, and relates to the technical field of fuel gas dechlorination. The method comprises the following steps: firstly, calcining dolomite, and modifying the dolomite by using acid, so that the modified dolomite has a rich pore structure; co (NO3) 3.6 H2O, Ni (NO3) 3.6 H2O and a nitrogen source are mixed with the modified dolomite, the obtained mixture is added into absolute ethyl alcohol, and a first material loaded with Co-Ni-P is obtained through stirring, heating, drying, calcination and phosphorization; uniformly mixing Fe (NO3) 3.9 H2O, urea and ammonium fluoride, adding the mixture into the first material, and sequentially heating, washing, filtering and drying to obtain the catalyst. The catalyst prepared by the method is high in inactivation resistance and good in catalytic effect.

Description

Technical Field

[0001] The invention relates to the technical field of gas dechlorination, and in particular to a method for preparing a catalyst for removing chlorophenol pollutants in organic solid waste gas. Background Art

[0002] With the continuous development of social economy, the annual output of organic solid waste has exceeded 6 billion tons. The graded pyrolysis gasification technology of organic solid waste with gas as the target product has become one of the main ways to clean and efficiently utilize organic solid waste because of its advantages such as small footprint, high degree of reduction, and high efficiency of gasification combined power generation.

[0003] Organic solid waste has a high chlorine content. During the gasification process, HCl and organic chlorine will enter the fuel gas, accelerating the corrosion of downstream equipment and pipelines, causing serious harm to the environment. Among them, there are mainly chlorine-containing compounds such as chlorobenzene, chlorophenol and C6Cl6, which in turn generate highly toxic dioxins. Since C-Cl bonds are important precursors for the generation of dioxins, the efficient removal of organic chlorine in the fuel gas from organic solid waste gasification has become a key issue.

[0004] There are several main methods for removing chlorinated organic matter, including adsorption, oxidation and hydrodechlorination. Although the adsorption method is simple and effective, its pore structure leads to limited adsorption capacity, and regeneration and replacement require greater costs. The oxidation method can fundamentally remove chlorophenols, but the finished product may be a more toxic substance. Hydrodechlorination is a more promising degradation technology due to its low energy demand and the fact that highly toxic chlorophenols are effectively converted into less harmful substances, significantly reducing their eco-toxicity. At present, dechlorination research in the prior art has made certain progress, but there are still drawbacks. For example, application number 202111557600.4 discloses a method for preparing a material for removing chloromethane, dichloromethane, etc. and inorganic chlorine in petroleum. Although the removal efficiency is high, the material manufacturing process is complicated, and chlorinated organic and inorganic substances are mainly removed by adsorption, and secondary treatment problems are still involved after removal.

[0005] This shows that the prior art needs to be further improved. Summary of the invention

[0006] The object of the present invention is to provide a method for preparing a catalyst for removing chlorophenol pollutants in organic solid waste gas, the catalyst having strong anti-deactivation ability and good catalytic effect.

[0007] In order to achieve the above object, the present invention adopts the following technical solutions:

[0008] A method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas comprises the following steps:

[0009] Step 1: calcining dolomite and modifying it with acid so that the modified dolomite has a rich pore structure;

[0010] Step 2: Co(NO3)3·6H2O, Ni(NO3)3·6H2O, a nitrogen source and the modified dolomite are mixed, and the resulting mixture is added to anhydrous ethanol, and the mixture is stirred, heated, dried, calcined and phosphated to obtain a first material loaded with Co-Ni-P; the phosphating temperature is 300-400°C;

[0011] Step 3: Evenly mix Fe(NO3)3·9H2O, urea and ammonium fluoride, add them to the first material, and sequentially heat, wash, filter and dry in a reactor to obtain a catalyst;

[0012] In step 3, Fe in Fe(NO3)3·9H2O interacts with Co and Ni in the first material, and the combination of Fe, Ni and Co enhances the activity and sintering resistance of the active component; the urea and ammonium fluoride are auxiliary substances used to promote the formation of Fe(OH)3 and promote the formation of P-OH groups to promote the overflow of active hydrogen and enhance the breaking of C-Cl bonds;

[0013] The mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 1-4:1-4;

[0014] The mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 1 to 9:1;

[0015] The mass ratio of the sum of the masses of the Co(NO3)3·6H2O and the Ni(NO3)3·6H2O to the modified dolomite is 1:1-10.

[0016] In the above-mentioned method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, in step 1, the calcination step of dolomite is: placing the dolomite in a muffle furnace at 10°C·min -1 The dolomite is heated to 800-1000° C. at a speed of 1000° C. and calcined for 3-5 hours. The acid used for modification is 50 vol.% acetic acid, and the ratio of the molar amount of acetic acid to the sum of the molar amounts of Ca and Mg in the dolomite is 1.5-2.5:1.

[0017] The above-mentioned method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, the nitrogen source is g-C3N4, and the ratio of the mass of the nitrogen source to the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O is 1:0.5~5.

[0018] The above-mentioned method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, in step 2, the stirring time is 10 to 14 hours, the mixture and anhydrous ethanol are heated at 80°C until the solvent evaporates, dried at 80°C for 24 hours, and calcined at 500 to 600°C in an air atmosphere for 0.5 to 1.5 hours.

[0019] In the above-mentioned method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, in step 2, the phosphating step is to place the calcined material downstream of a tubular furnace, and NaH2PO2 is installed upstream of the tubular furnace, and phosphating is carried out for 1 to 3 hours under an argon atmosphere.

[0020] In the above-mentioned method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, in step three, the mass ratios of Fe(NO3)3·9H2O, urea and ammonium fluoride are 0.1-2:1-10:0.1-1 respectively.

[0021] In the above-mentioned method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, in step three, the heating temperature is 70 to 90° C. and the heating time is 3 to 5 hours.

[0022] Compared with the prior art, the present invention brings the following beneficial technical effects:

[0023] (1) From the preparation method, firstly, the present invention uses dolomite as raw material and modifies it with acid to obtain modified dolomite. The modified dolomite has rich pore structure, large specific surface area and relatively developed pore structure. Secondly, g-C3N4, Co(NO3)3·6H2O and Ni(NO3)3·6H2O are added to generate N-doped active components, so that the active components are not easy to sinter. After phosphating by low-temperature phosphating method, the structure is more stable and closer to the activity of precious metals. After phosphating, the first material loaded with Co-Ni-P is obtained; then Fe(NO3)3·9H2O, urea and ammonium fluoride are mixed evenly and added to the first material. The combined action of iron, cobalt and nickel enhances the activity and anti-sintering ability of the active components. The hydroxyl group and P form P-OH groups and the existence of Fe(OH)3 promote the overflow of active hydrogen and enhance the breaking of C-Cl bonds. This catalyst material with high dispersion, rich pores and strong resistance to deactivation is conducive to the full interaction between hydrogen and the active sites of the catalyst, making the catalytic effect of the catalyst more ideal.

[0024] (2) The catalyst obtained by the preparation method of the present invention has a long service life and good regeneration performance. The present invention provides a method using abundant dolomite as a carrier, which is clean, efficient and simple in preparation process, and provides a method for removing chlorophenols from fuel gas to dolomite-loaded N, Fe and hydroxyl-doped phosphide bimetallic catalysts. The efficiency of removing chlorophenols from fuel gas prepared by the method of the present invention can reach more than 95%.

[0025] (3) The preparation method of the catalyst for removing chlorophenol pollutants from organic solid waste gas of the present invention uses dolomite, which is abundant and renewable, cheap and easy to obtain, and easy to react with organic acid to form a porous structure. Through the proportional loading of Co-Ni-P-Fe, chlorophenol in the gas can be removed, and the removal efficiency can reach 95%. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] The present invention will be further described below in conjunction with the accompanying drawings:

[0027] Figure 1 This is a comparison chart of the efficiencies of the catalysts prepared in Examples 1 to 10;

[0028] Figure 2 This is a comparison chart of the efficiencies of the catalysts prepared in Comparative Examples 1 to 3. DETAILED DESCRIPTION

[0029] The present invention proposes a method for preparing a catalyst for removing chlorophenol pollutants in organic solid waste gas. In order to make the advantages and technical solutions of the present invention clearer and more specific, the present invention is further described below in conjunction with specific embodiments.

[0030] The raw materials described in the present invention can be purchased through commercial channels.

[0031] The specific preparation steps of g-C3N4 described in the present invention are: placing urea in a crucible, heating it at 550°C in an air atmosphere for 4 hours, and grinding it into powder.

[0032] Specific inspection measures:

[0033] The prepared material was placed in an existing organic solid waste pyrolysis simulation device and 30 ml / min -1 of H2 gas and 30ml·min -1 A mixture of chlorophenol and nitrogen (the concentration of chlorophenol in the mixture is 100 ppm) is heated to 350 degrees and kept warm for 30 minutes. The inlet and outlet gases are analyzed and tested by gas chromatography.

[0034] Embodiment 1:

[0035] A method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas comprises the following steps:

[0036] Step 1, calcining the dolomite and modifying it with acid so that the modified dolomite has a rich porous structure; specifically, placing the dolomite in a muffle furnace, calcining it at a temperature of 800° C. for 3 hours, reacting it in 50 vol.% acetic acid for 2 hours, the ratio of the molar amount of acetic acid to the sum of the molar amounts of Ca and Mg in the dolomite is 1.5:1, and drying it in an oven at 120° C. for 8 hours to obtain the modified dolomite.

[0037] Step 2: Mix Co(NO3)3·6H2O, Ni(NO3)3·6H2O and g-C3N4 with the modified dolomite, add the resulting mixture into 20 mL of anhydrous ethanol, stir for 12 h, heat at 80°C until the solvent evaporates, dry at 80°C for 24 h, calcine at 550°C in an air atmosphere for 1 hour, and then adopt a low-temperature phosphating method with a phosphating temperature of 350°C; that is, place the resulting mixture downstream of a tubular furnace, and install NaH2PO2 upstream, heat at 350°C for 2 hours under an argon atmosphere, and cool naturally.

[0038] Step 3: Evenly mix Fe(NO3)3·9H2O, urea and ammonium fluoride, and add them to the first material. The mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 1:1; the mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 9:1; the mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to the modified dolomite is 1:2.

[0039] Among them, Fe in Fe(NO3)3·9H2O interacts with Co and Ni in the first material, and the combination of Fe, Ni and Co enhances the activity and anti-sintering ability of the active component; the urea and ammonium fluoride are auxiliary substances, which promote the formation of Fe(OH)3 and the formation of P-OH groups, promote the overflow of active hydrogen, and enhance the breaking of C-Cl bonds; the catalyst is obtained by heating, washing, filtering and drying in a reactor in sequence.

[0040] Results: The catalyst prepared in this example was used to remove chlorophenol pollutants from organic solid waste gas. The specific removal steps were: H2 reacted on the material to generate active H atoms, and the C-Cl bonds on the chlorophenols reacted and broke on the material to generate phenol and HCl.

[0041] From the above, it can be seen that the catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol can reach 95%, the effective time is long, and the removal efficiency is still above 55% when the number of cycles reaches 8.

[0042] Embodiment 2:

[0043] The difference from Example 1 is that the mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 4:1.

[0044] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 87%, the effective time is long, and the removal efficiency is still above 45% when the number of cycles reaches 8.

[0045] Embodiment 3:

[0046] The difference from Example 1 is that the mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 2:1.

[0047] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 88%, the effective time is long, and the removal efficiency is still above 45% when the number of cycles reaches 8.

[0048] Embodiment 4:

[0049] The difference from Example 1 is that the mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 1:2.

[0050] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 86%, the effective time is long, and the removal efficiency is still above 44% when the number of cycles reaches 8.

[0051] Embodiment 5:

[0052] The difference from Example 1 is that the mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 1:4.

[0053] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 86%, the effective time is long, and the removal efficiency is still above 44% when the number of cycles reaches 8.

[0054] It can be seen from the above-mentioned Examples 1 to 3 that in the preparation process of the impregnation material of the present invention, the mass ratio of Co(NO3)2·6H2O and Ni(NO3)3·6H2O should be controlled at 1:1. Different ratios have different effects on the distribution of Co and Ni, affecting the contact reaction efficiency of hydrogen and chlorophenol at the active sites, thereby ultimately affecting the removal of chlorophenol.

[0055] Embodiment 6:

[0056] The difference from Example 1 is that the mass ratio of the sum of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 1:1.

[0057] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 75%, the effective time is long, and the removal efficiency is still above 35% when the number of cycles reaches 8.

[0058] Embodiment 7:

[0059] The difference from Example 1 is that the mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 3:1.

[0060] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 82%, the effective time is long, and the removal efficiency is still above 38% when the number of cycles reaches 8.

[0061] Embodiment 8:

[0062] The difference from Example 1 is that the mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 5:1.

[0063] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 84%, the effective time is long, and the removal efficiency is still above 41% when the number of cycles reaches 8.

[0064] Embodiment 9:

[0065] The difference from Example 1 is that the mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 7:1.

[0066] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 89%, the effective time is long, and the removal efficiency is still above 48% when the number of cycles reaches 8.

[0067] It can be seen from the above-mentioned Example 1 and Examples 6 to 9 that in the preparation process of the impregnation material of the present invention, the mass ratio of the sum of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O should be controlled at 9:1. Different mass ratios have different effects on the distribution of Co, Ni and Fe, and at the same time affect the proportion of P-OH groups, affect the contact reaction efficiency of hydrogen and chlorophenol at the active sites, and ultimately affect the removal of chlorophenol.

[0068] Embodiment 10:

[0069] The difference from Example 1 is that the phosphating temperature in step 2 is 300°C.

[0070] Results: The catalyst prepared by the present invention can effectively remove chlorine from chlorophenol and generate HCl. The removal efficiency of chlorophenol is 82%, the effective time is long, and the removal efficiency is still above 46% when the number of cycles reaches 8.

[0071] It can be seen from the above Examples 1 to 10 that the phosphating temperature should be controlled above 350° C. If the phosphating temperature is too low, it may lead to incomplete phosphating and affect the dechlorination efficiency.

[0072] Comparative Example 1:

[0073] A method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas comprises the following steps:

[0074] Step 1: calcine the dolomite at 800° C. in a muffle furnace for 3 hours, react in an acetic acid solution having a molar ratio of acetic acid to Ca and Mg of 1.5:1 for 2 hours, and dry in an oven at 120° C. for 8 hours to obtain the modified dolomite.

[0075] Step 2: Mix Co(NO3)3·6H2O, Ni(NO3)3·6H2O, Fe(NO3)3·9H2O and g-C3N4 with the modified dolomite, add the resulting mixture into 20 mL of anhydrous ethanol, stir for 12 h, heat at 80°C until the solvent evaporates, dry at 80°C for 24 h, calcine at 550°C in an air atmosphere for 1 hour, and then adopt a low-temperature phosphating method with a phosphating temperature of 350°C; that is, place the resulting mixture downstream of a tubular furnace, and install NaH2PO2 upstream, heat at 350°C for 2 hours under an argon atmosphere, and cool naturally.

[0076] In step 2, the mass ratio of Co(NO3)2·6H2O, Ni(NO3)3·6H2O and Fe(NO3)3·9H2O is 9:9:2. The mass ratio of the total mass of Co(NO3)2·6H2O, Ni(NO3)3·6H2O and Fe(NO3)3·9H2O to the modified dolomite is 1:2.

[0077] Experimental results: The chlorine in chlorophenol can be effectively removed and HCl can be generated. The removal efficiency of chlorophenol can reach 89%. After being recycled for 8 times, the removal efficiency is 32%.

[0078] Comparative Example 2:

[0079] A method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas comprises the following steps:

[0080] Step 1: calcine the dolomite at 800° C. in a muffle furnace for 3 hours, react in an acetic acid solution having a molar ratio of acetic acid to Ca and Mg of 1.5:1 for 2 hours, and dry in an oven at 120° C. for 8 hours to obtain the modified dolomite.

[0081] Step 2: Add Co(NO3)3·6H2O and Ni(NO3)3·6H2O, modified dolomite and g-C3N4 into 20 mL of anhydrous ethanol, stir for 12 hours, heat at 80°C until the solvent evaporates, dry at 80°C overnight, calcine at 550°C in air atmosphere for 1 hour, and use the low-temperature phosphating method. The material is placed downstream of the tubular furnace and NaH2PO2 is placed upstream. Under argon atmosphere, heat at 350°C for 2 hours and cool naturally.

[0082] In step 2, the mass ratio of Co(NO3)2·6H2O and Ni(NO3)3·6H2O is 1:1.

[0083] Experimental results: The catalyst prepared in this comparative example can effectively remove chlorine from chlorophenol to generate HCl. The removal efficiency of chlorophenol can reach 88%. After being recycled for 8 times, the removal efficiency is 42%.

[0084] Comparative Example 3:

[0085] A method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas comprises the following steps:

[0086] Step 1: Mix Co(NO3)3·6H2O, Ni(NO3)3·6H2O and g-C3N4 with dolomite, add the resulting mixture into 20 mL of anhydrous ethanol, stir for 12 h, heat at 80°C until the solvent evaporates, dry at 80°C for 24 h, calcine at 550°C in air atmosphere for 1 hour, adopt low-temperature phosphating method, and the phosphating temperature is 300°C; that is, the resulting mixture is placed downstream of the tubular furnace, and NaH2PO2 is placed upstream, heated at 350°C for 2 hours under argon atmosphere, and naturally cooled.

[0087] Step 2: Fe(NO3)3·9H2O, urea and ammonium fluoride are mixed evenly and added to the first material. The mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 1:1; the mass ratio of the sum of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 9:1; the mass ratio of the sum of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to the modified dolomite is 1:2. The catalyst is obtained by heating, washing, filtering and drying in sequence.

[0088] Experimental results: Since the dolomite was not modified, the porosity was low and only a small amount of active components were loaded, the chlorine removal rate in chlorophenol was low, only 45%. After being recycled 8 times, it had a removal efficiency of 17%.

[0089] The catalysts prepared in Examples 1 to 10 and Comparative Examples 1 to 3 were tested, and the dechlorination efficiency was as follows: Figure 1 , 2 shown.

[0090] Parts not described in the present invention can be implemented by referring to the existing technology.

[0091] Those skilled in the art should recognize that the above embodiments are only used to illustrate the present application and are not intended to be limiting of the present application. As long as they are within the spirit and scope of the present application, appropriate changes and modifications to the above embodiments are within the scope of protection claimed in the present application.

Claims

1. A method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas, characterized in that: The following steps are involved: Step 1: calcining dolomite and modifying it with acid so that the modified dolomite has a rich pore structure; Step 2: Co(NO3)3·6H2O, Ni(NO3)3·6H2O, a nitrogen source and the modified dolomite are mixed, and the resulting mixture is added to anhydrous ethanol, and the mixture is stirred, heated, dried, calcined and phosphated to obtain a first material loaded with Co-Ni-P; the phosphating temperature is 300-400°C; Step 3: Evenly mix Fe(NO3)3·9H2O, urea and ammonium fluoride, add them to the first material, and sequentially heat, wash, filter and dry to obtain a catalyst; In step 3, Fe in Fe(NO3)3·9H2O interacts with Co and Ni in the first material, and the combination of Fe, Ni and Co enhances the activity and sintering resistance of the active component; the urea and ammonium fluoride are auxiliary substances used to promote the formation of Fe(OH)3 and promote the formation of P-OH groups to promote the overflow of active hydrogen and enhance the breaking of C-Cl bonds; The mass ratio of Co(NO3)3·6H2O to Ni(NO3)3·6H2O is 1-4:1-4; The mass ratio of the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O to Fe(NO3)3·9H2O is 1 to 9:1; The mass ratio of the sum of the masses of the Co(NO3)3·6H2O and the Ni(NO3)3·6H2O to the modified dolomite is 1:1-10.

2. The method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas according to claim 1, characterized in that: In step 1, the calcination step of dolomite is as follows: placing the dolomite in a muffle furnace at 10°C·min -1 The dolomite is heated to 800-1000° C. at a speed of 1000° C. and calcined for 3-5 hours. The acid used for modification is 50% acetic acid by volume, and the ratio of the molar amount of acetic acid to the sum of the molar amounts of Ca and Mg in the dolomite is 1.5-2.5:

1.

3. The method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas according to claim 1, characterized in that: In step 2, the nitrogen source is g-C3N4, and the ratio of the mass of the nitrogen source to the sum of the masses of Co(NO3)3·6H2O and Ni(NO3)3·6H2O is 1:0.5-5.

4. The method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas according to claim 1, characterized in that: In step 2, the stirring time is 10 to 14 hours, the mixture and anhydrous ethanol are heated at 80° C. until the solvent evaporates, dried at 80° C. for 24 hours, and calcined at 500 to 600° C. in an air atmosphere for 0.5 to 1.5 hours.

5. The method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas according to claim 1, characterized in that: In step 2, the phosphating step is to place the calcined material downstream of a tubular furnace, with NaH2PO2 installed upstream of the tubular furnace, and phosphate for 1 to 3 hours under an argon atmosphere.

6. The method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas according to claim 1, characterized in that: In step 3, the mass ratios of Fe(NO3)3·9H2O, urea and ammonium fluoride are 0.1-2:1-10:0.1-1 respectively.

7. The method for preparing a catalyst for removing chlorophenol pollutants from organic solid waste gas according to claim 1, characterized in that: In step 3, the heating temperature is 70-90° C. and the heating time is 3-5 hours.

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