A catalyst for the oxidative pyrolysis of medical waste salt melt organic flue gas

Abstract

The present application relates to a kind of catalyst for medical waste salt melting organic flue gas cracking oxidation.The present application utilizes sol-gel method to load perovskite type metal oxide on silica-alumina molecular sieve, form the catalyst with cracking oxidation characteristics, and further load a layer of transition metal oxide on the above-mentioned catalyst by chemical reduction method, for regulating the cracking oxidation performance of catalyst.The catalyst prepared by the present application has abundant acid sites and oxidation sites, can crack macromolecular organic matter in medical waste salt melting organic flue gas into gaseous small molecules at lower temperature, and then oxidize completely into harmless substances by deep oxidation, effectively avoiding the problems of high purification temperature and low efficiency of medical waste salt melting organic flue gas;And low energy consumption, little secondary pollution, wide application range, can effectively replace the second combustion chamber to degrade macromolecular organic matter in medical waste salt melting organic flue gas, and the concentration of non-methane total hydrocarbon in purified tail gas is reduced to 40 mg / Nm 3 The following.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of environmental protection, and particularly relates to a catalyst for medical waste salt melting organic flue gas cracking oxidation. TECHNICAL BACKGROUND

[0002] With the steady and rapid development of China's industry, metallurgy, chemical industry, medicine, printing and dyeing and other industries inevitably produce a large amount of industrial waste salt. According to incomplete statistics, the output of industrial waste salt in China exceeds 50 million tons per year, among which, medical waste salt accounts for about 10% of industrial waste salt. In view of the characteristics of high content of organic pollutants and complex types of waste salt in the pharmaceutical industry, the removal of organic impurities needs to be focused on. At present, the treatment and utilization technology of waste salt at home and abroad mainly has two types, i.e. harmless and resource.

[0003] Among them, the high-temperature melting treatment method is to remove the organic matter in the industrial waste salt at a high temperature of 800-1200℃ in a molten state, and the removal effect of organic matter is good. Chinese patent CN109579025A discloses "an efficient melting incineration device for industrial waste salt", which uses high-temperature melting method to treat industrial waste salt, so that the organic matter in the industrial waste salt is completely decomposed in a molten state, but the energy consumption is high, and incineration flue gas is generated at the same time. The incineration flue gas still contains part of the macromolecular organic matter, mainly halogenated hydrocarbons, benzene series and condensed ring compounds and other refractory organic matter, and a large amount of combustion-supporting fuel needs to be added in the secondary combustion chamber unit to effectively burn and remove the organic matter. The tail gas after the secondary combustion of the incineration flue gas contains dioxin, and the secondary pollution is large, the energy consumption is high and the effect is not good. Therefore, a low-temperature and high-efficiency method is needed to replace the secondary combustion chamber to degrade macromolecular organic matter.

[0004] Catalytic combustion method is widely used in the treatment of chlorine-containing organic matter, and its main advantages are low operating temperature, high elimination efficiency, small energy consumption, and treatment of low-concentration waste gas at relatively low temperature (<500℃). However, in the oxidation process of chlorine-containing organic compounds and aromatic hydrocarbons, the by-products (especially chlorinated aromatic hydrocarbons) may form more toxic and persistent polychlorinated dibenzofurans (PCDFs), polychlorinated dibenzodioxins (PCDDs) and biphenyls (PCBs) at 250-400℃, which cause great harm to the atmospheric environment. Catalytic hydrogenation dechlorination refers to the hydrogenation dechlorination of chlorine-containing organic compounds under mild conditions (temperature is generally room temperature <350℃), so as to convert chlorine-containing organic compounds into harmless HCl and hydrocarbons. The HCl produced in this reaction can be separated by absorbing NaOH lye, and the hydrocarbons can be easily eliminated or recovered. Although catalytic hydrogenation dechlorination technology is efficient and environmentally friendly, it has some shortcomings such as poor selection and stability of catalyst, high equipment investment, large energy consumption and potential safety and environmental risks, which need to be continuously optimized and improved.

[0005] The main advantages of the photocatalytic oxidation method are that the degradation of pollutants is complete, and the reaction conditions are mild, and the reaction can be carried out at normal temperature and pressure. However, the industrial application of the photocatalyst is restricted due to the wide band gap, narrow absorption range, low solar energy utilization rate and low activity of the photocatalyst. In addition, the decomposition products of chlorine-containing organic compounds, such as Cl elements, can block the active sites on the surface of the photocatalyst, thereby reducing the catalytic activity. SUMMARY

[0006] In order to solve the problems existing in the above-mentioned conventional technology, the present application provides a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melting organic flue gas, which uses a catalyst with pyrolysis and oxidation function to purify the pharmaceutical waste salt melting flue gas. The abundant acid sites on the pyrolysis and oxidation catalyst can pyrolyze the macromolecular organic matter in the pharmaceutical waste salt melting organic flue gas into gaseous small molecules at a lower temperature. In addition, the oxidation sites on the catalyst can further oxidize the gaseous small molecules into harmless substances such as CO2 and H2O, thereby realizing the low-temperature and high-efficiency purification of the pharmaceutical waste salt melting organic flue gas. Therefore, the use of the pyrolysis and oxidation catalyst to purify the pharmaceutical waste salt melting organic flue gas can achieve the purpose of replacing the two-burner degradation of macromolecular organic matter.

[0007] In order to achieve the above-mentioned purpose, the technical scheme adopted by the present application is as follows:

[0008] In a first aspect, the present application provides a preparation method of a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melting organic flue gas. The metal inorganic salt, preferably perovskite metal oxide, is loaded on a silicon-aluminum molecular sieve by a sol-gel method to form a catalyst with pyrolysis and oxidation characteristics. The transition metal oxide film is loaded on the catalyst by a chemical reduction method to further regulate the pyrolysis and oxidation performance of the catalyst, thereby obtaining the catalyst for the low-temperature and high-efficiency deep purification of the pharmaceutical waste salt melting organic flue gas.

[0009] In a specific embodiment, the transition metal oxide is manganese oxide.

[0010] In a specific embodiment, the method specifically comprises the following steps:

[0011] Step 1: Dilute the metal inorganic salt, citric acid and silicon-aluminum molecular sieve in deionized water in proportion to form a solution, and heat and stir until a sol is formed;

[0012] Step 2: Dry the sol obtained in step 1, continue to calcine, and obtain catalyst A;

[0013] Step 3: Disperse catalyst A obtained in step 2 and potassium permanganate in deionized water, stir at room temperature, then add metal inorganic salt, heat and stir, filter, wash with water and ethanol three times, dry at room temperature, continue to dry by heating, and finally calcine to obtain the catalyst.

[0014] In a specific embodiment, in step 1, the metal cation in the metal inorganic salt is a combination of two of Cu 2+ , Ce 2+ , La 3+ , Mn 2+ or Co 3+ , preferably a combination of La 3+ and Mn 2+ , wherein the mass ratio of La 3+ to Mn 2+ is 0.2-5:1.

[0015] In a more specific embodiment, the perovskite metal oxide is selected from a combination of any two of copper oxide, cerium oxide, lanthanum oxide, manganese oxide, cobalt oxide.

[0016] In a specific embodiment, in step 1, the silicon-aluminum molecular sieve is one of ZSM-5, HZSM-5, H-Y, preferably ZSM-5. Preferably, the silicon-aluminum ratio of the silicon-aluminum molecular sieve is 10-500, more preferably 25-100.

[0017] In a specific embodiment, in step 1, the molar ratio of the metal inorganic salt to citric acid monohydrate is 0.5-2:1, and the mass ratio of the metal cation in the metal inorganic salt to the silicon-aluminum molecular sieve is 1:4-99.

[0018] The amount of the deionized water used in step 1 is not particularly limited and can be in the range of amounts conventionally used in the art.

[0019] In a specific embodiment, in step 1, the temperature for heating and stirring is 60-90°C, and the time is 3-6h, preferably 80°C for 5h.

[0020] In a specific embodiment, in step 2, the drying temperature is 100-120°C, and the time is 10-14h, preferably 110°C for 12h.

[0021] In a specific embodiment, in step 2, the calcination temperature is 600-700°C, and the time is 3-5h, preferably 650°C for 4h.

[0022] In a specific embodiment, in step 3, the mass ratio of the metal inorganic salt, catalyst A and potassium permanganate is 1:80-120:1, preferably 1:100:1. The metal cation in the metal inorganic salt is Mn 2+ .

[0023] In a specific embodiment, in step 3, the stirring time at room temperature is 20-40min, preferably 30min at room temperature.

[0024] In specific embodiments, in step 3, the temperature of the heated stirring is 60-80℃, the time is 2-4h, preferably stirring at 70℃ for 3h.

[0025] In specific embodiments, in step 3, the time of drying at room temperature is 20-28h, preferably drying at room temperature for 24h.

[0026] In specific embodiments, in step 3, the temperature of the continued heating drying is 60-80℃, the time is 10-14h, preferably drying at 70℃ for 12h.

[0027] In specific embodiments, in step 3, the temperature of the calcination is 300-400℃, the time is 1-3h, preferably calcination at 350℃ for 22h.

[0028] In a second aspect, the present application provides a catalyst prepared by the above preparation method.

[0029] In a third aspect, the present application further provides an application of the above catalyst in the oxidative pyrolysis of pharmaceutical waste salt molten organic flue gas.

[0030] In a fourth aspect, the present application further provides an application of the above catalyst in the preparation of products of the oxidative pyrolysis of pharmaceutical waste salt molten organic flue gas.

[0031] In some specific embodiments, the use method of the above catalyst comprises the following steps:

[0032] The pharmaceutical waste salt molten organic flue gas is brought into and through the oxidative pyrolysis catalyst by the air flow, and the reaction temperature is controlled, so as to deeply purify the macromolecular organic matter in the pharmaceutical waste salt molten organic flue gas. The concentration of non-methane total hydrocarbon in the purified tail gas is determined according to the specified detection method, and the change of the concentration of non-methane total hydrocarbon in the pharmaceutical waste salt molten organic flue gas before and after purification by the oxidative pyrolysis catalyst is determined.

[0033] In specific embodiments, the air flow has a space velocity range of 5000-20000ml / g cat ·h, preferably 12000ml / g cat ·h.

[0034] In specific embodiments, the reaction temperature range is 300-500℃, preferably 350℃.

[0035] The detection method in the above steps is from the regulation “Determination of Total Hydrocarbon, Methane and Non-Methane Total Hydrocarbon in Waste Gas from Stationary Sources by Gas Chromatography” (HJ 38-2017).

[0036] Compared with the prior art, the present application has the following beneficial effects:

[0037] (1) The catalyst provided by the present application can be used to crack and oxidize macromolecular organic matter in the organic flue gas of medical waste salt melting at a lower temperature, which can effectively replace the two combustion chambers to degrade macromolecular organic matter in the organic flue gas of medical waste salt melting, realize deep purification of macromolecular organic matter in the organic flue gas of medical waste salt melting at a lower temperature, reduce energy consumption, and the preparation method of the catalyst is simple and can be reused.

[0038] (2) Compared with the low-efficiency purification of macromolecular organic matter in the organic flue gas of medical waste salt melting by other treatment methods, the catalyst for cracking and oxidizing the organic flue gas of medical waste salt melting provided by the present application can reduce the non-methane total hydrocarbon content of the purified tail gas to 40mg / Nm 3 The following.

[0039] (3) In the present application, the silica-alumina molecular sieve with a large number of surface acid sites and the perovskite metal oxide with a large number of oxidation sites can be uniformly compounded by the above preparation method, and the synergistic effect of cracking and oxidation is adjusted by chemical reduction method to obtain a catalyst for cracking and oxidizing the organic flue gas of medical waste salt melting, which can effectively generate benzene quinone intermediates from macromolecular organic matter in the organic flue gas of medical waste salt melting through nucleophilic substitution reaction, and further crack into low-carbon linear organic matter, and finally oxidize into harmless substances, and the non-methane total hydrocarbon content of the purified tail gas is reduced to 20mg / Nm 3 The following.

[0040] Specific mode implementation

[0041] The catalyst involved in the present application is applied to the effect of the cracking and oxidation process of the organic flue gas of medical waste salt melting, which is further illustrated by the following examples and comparative examples.

[0042] Some components in the examples and comparative examples are as follows:

[0043] The medical waste salt melting organic flue gas simulation gas: the same medical waste salt melting organic flue gas simulation gas is used in the following examples, which is obtained by blowing air into 3-methyl chlorobenzyl liquid, and the non-methane total hydrocarbon concentration of the medical waste salt melting organic flue gas simulation gas is about 4000mg / Nm 3 Although the same method is used to generate the simulation gas of the medical waste salt melting organic flue gas in the following examples, due to the arrangement of the experimental time and the inherent error of the non-methane total hydrocarbon test, the non-methane total hydrocarbon content of the medical waste salt melting organic flue gas simulation gas without catalyst treatment has slight fluctuations. However, these differences are within the acceptable error range.

[0044] The following numbers in the carriers of the catalysts used in the following examples and comparative examples represent the silicon-aluminum ratio, such as "ZSM-5" in ZSM-5-40 represents the silicon-aluminum molecular sieve, and "40" represents the silicon-aluminum ratio of the silicon-aluminum molecular sieve.

[0045] Example 1

[0046] This example provides a method for cracking and oxidizing organic flue gas from melting of medical waste salt, which is as follows:

[0047] (1) Catalyst A preparation: 0.78 g of La(NO3)2·6H2O, 1.14 g of Mn(NO3)2·4H2O, 1.21 g of citric acid monohydrate, and 5 g of ZSM-5-40 carrier were weighed into 50 ml of deionized water, heated and stirred at 80°C for 4 h until a sol was formed, then dried at 110°C for 12 h, and finally calcined in a muffle furnace at 650°C for 4 h. After calcination, a lanthanum-manganese perovskite bimetallic oxide catalyst was obtained. The mass ratio of La to Mn in the catalyst was 1:1, and the mass percentage of La and Mn in the catalyst was 10% based on the mass percentage of the catalyst being 100%;

[0048] (2) Catalyst preparation: 1 g of catalyst A and 0.01 g of KMnO4 were dispersed in 25 mL of deionized water and stirred for 30 min. Then 0.01 g of Mn(NO3)2 was added and stirred at 70°C for 2 h. Filtration, washing with water and ethanol three times. The obtained precursor was first dried at room temperature for 24 h, and then dried at 70°C for 12 h. Finally, the prepared sample was calcined at 350°C for 2 h.

[0049] (3) The cracking and oxidation of the simulated organic flue gas from melting of medical waste salt was carried out at a reaction space velocity of 12000 ml / (g cat ·h) and a reaction temperature of 350°C, and the non-methane total hydrocarbon concentration of the purified tail gas was determined by gas chromatography.

[0050] Example 2

[0051] This example provides a method for cracking and oxidizing organic flue gas from melting of medical waste salt, which is different from Example 1 only in that:

[0052] The catalyst carrier ZSM-5-40 in step (1) of Example 1 is replaced by an equal amount of ZSM-5-25;

[0053] The other conditions are the same as in Example 1.

[0054] Example 3

[0055] This example provides a method for cracking and oxidizing organic flue gas from melting of medical waste salt, which is different from Example 1 only in that:

[0056] The catalyst carrier ZSM-5-40 in step (1) of Example 1 was replaced with equal mass of ZSM-5-60;

[0057] Other conditions were the same as Example 1.

[0058] Example 4

[0059] This example provides a method for melting organic flue gas cracking oxidation of medical waste salt, which is only different from Example 1 in that:

[0060] The catalyst carrier ZSM-5-40 in step (1) of Example 1 was replaced with equal mass of ZSM-5-80;

[0061] Other conditions were the same as Example 1.

[0062] Example 5

[0063] This example provides a method for melting organic flue gas cracking oxidation of medical waste salt, which is only different from Example 1 in that:

[0064] The catalyst carrier ZSM-5-40 in step (1) of Example 1 was replaced with equal mass of ZSM-5-100;

[0065] Other conditions were the same as Example 1.

[0066] Comparative Example 1

[0067] This comparative example provides a method for melting organic flue gas cracking oxidation of medical waste salt, which is as follows:

[0068] (1) Catalyst A preparation: 0.78 g of La(NO3)2·6H2O, 1.14 g of Mn(NO3)2·4H2O, 1.21 g of citric acid monohydrate and 5 g of HZSM-5-40 carrier were weighed into 50 ml of deionized water, heated and stirred at 80°C for 4 h until a sol was formed, then dried at 110°C for 12 h, and finally calcined in a muffle furnace at 650°C for 4 h. After calcination, a lanthanum-manganese perovskite bimetallic oxide catalyst was obtained; the mass ratio of La to Mn in the catalyst was 1:1, and the mass percentage of La and Mn in the catalyst was 10% based on the mass percentage content of the catalyst being 100%;

[0069] (2) Catalyst preparation: 1 g of catalyst A and 0.01 g of KMnO4 were dispersed in 25 mL of deionized water and stirred for 30 min. Then 0.01 g of Mn(NO3)2 was added and stirred at 70°C for 2 h. Filtration, washing with water and ethanol three times. The obtained precursor was first dried at room temperature for 24 h, and then dried at 70°C for 12 h. Finally, the prepared sample was calcined at 350°C for 2 h.

[0070] (3) The pharmaceutical waste salt melt organic flue gas simulation gas was cracked and oxidized at a reaction space velocity of 12000 ml / (g cat The non-methane total hydrocarbon concentration of the purified tail gas was determined by gas chromatography.

[0071] Comparative Example 2

[0072] The present embodiment provides a method for cracking and oxidizing pharmaceutical waste salt melt organic flue gas, which is as follows:

[0073] (1) Catalyst A preparation: 0.78 g of La(NO3)2·6H2O, 1.14 g of Mn(NO3)2·4H2O, 1.21 g of citric acid monohydrate, and 5 g of H-Y-40 carrier were weighed into 50 ml of deionized water, heated and stirred at 80°C for 4 h until a sol was formed, then dried at 110°C for 12 h, and finally calcined in a muffle furnace at 650°C for 4 h. After calcination, a lanthanum-manganese perovskite bimetallic oxide catalyst was obtained. The mass ratio of La to Mn in the catalyst was 1:1, and the mass percentage of La and Mn in the catalyst was 10% based on the mass percentage content of the catalyst being 100%;

[0074] (2) Catalyst preparation: 1 g of catalyst A and 0.01 g of KMnO4 were dispersed in 25 mL of deionized water and stirred for 30 min. Then 0.01 g of Mn(NO3)2 was added and stirred at 70°C for 2 h. Filtration, washing with water and ethanol three times. The obtained precursor was first dried at room temperature for 24 h, and then dried at 70°C for 12 h. Finally, the prepared sample was calcined at 350°C for 2 h.

[0075] (3) The pharmaceutical waste salt melt organic flue gas simulation gas was cracked and oxidized at a reaction space velocity of 12000 ml / (g cat The non-methane total hydrocarbon concentration of the purified tail gas was determined by gas chromatography.

[0076] The non-methane total hydrocarbon concentration of the pharmaceutical waste salt melt organic flue gas simulation gas before and after cracking and oxidation in the above embodiment was determined, and the results are shown in Table 1 below.

[0077] Table 1

[0078]

[0079]

[0080] The protection scope of the present application is not limited to the above-mentioned embodiments. Changes and advantages that can be thought of by those skilled in the art without departing from the spirit and scope of the present application are included in the present application and are protected by the appended claims.

Claims

1. A method for preparing a catalyst for the cracking and oxidation of pharmaceutical waste salt melted organic flue gas, characterized in that: The catalyst is obtained by loading a calcium ore-type metal oxide onto a silica-alumina molecular sieve using a sol-gel method to form a catalyst having cracking and oxidation properties, and loading a transition metal oxide film onto the catalyst by a chemical reduction method to further regulate the cracking and oxidation properties of the catalyst. The method specifically comprises the following steps: Step 1: Dilute the metal inorganic salt, citric acid monohydrate and silica-alumina molecular sieve in deionized water in proportion to form a solution, and heat and stir until a sol is formed; Step 2: drying the sol obtained in step 1 and continuing calcination to obtain catalyst A; Step 3: Dispersing the catalyst A obtained in step 2 and potassium permanganate in deionized water and stirring at room temperature, then adding a metal inorganic salt, heating and stirring, filtering, washing three times with water and ethanol, drying at room temperature, continuing to heat and dry, and finally calcining to obtain the catalyst; wherein the metal cation in the metal inorganic salt is Mn2+; In step 1, the metal cations in the metal inorganic salt are a combination of two of Cu2+, Ce2+, La3+, Mn2+ or Co3+.

2. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 1, wherein the combination is a combination of La3+ and Mn2+, wherein: The mass ratio of La3+ and Mn2+ is 0.2~5:

1.

3. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 1, characterized in that: In step 1, the silica-alumina molecular sieve is one of ZSM-5, HZSM-5, and HY; in step 1, the molar ratio of the metal inorganic salt to citric acid monohydrate is 0.5 to 2:1, and the mass ratio of the cation in the metal inorganic salt to the silica-alumina molecular sieve is 1:4 to 99.

4. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 3, characterized in that: In step 1, the silicon-alumina molecular sieve is ZSM-5.

5. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 4, characterized in that: In step 1, the silicon-aluminum ratio of the silicon-aluminum molecular sieve is 10-500.

6. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 5, characterized in that: In step 1, the silicon-aluminum ratio of the silicon-aluminum molecular sieve is 25-100.

7. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 1, characterized in that: In step 1, the heating and stirring temperature is 60 to 90° C., and the time is 3 to 6 hours.

8. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 7, characterized in that: In step 1, the heating and stirring temperature is 80° C. and stirring is performed for 5 h.

9. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 1, characterized in that: In step 2, the drying temperature is 100-120° C. and the drying time is 10-14 hours.

10. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 9, characterized in that: In step 2, the drying temperature is 110° C. for 12 h.

11. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 1, characterized in that: In step 2, the calcination temperature is 600-700° C. and the calcination time is 3-5 hours.

12. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 11, characterized in that: In step 2, the calcination temperature is 650° C. for 4 h.

13. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salt melted organic flue gas according to claim 1, characterized in that: In step 3, the mass ratio of the metal inorganic salt, catalyst A and potassium permanganate is 1:80 to 120:

1.

14. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 13, characterized in that: In step 3, the mass ratio of the metal inorganic salt, catalyst A and potassium permanganate is 1:100:

1.

15. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 1, characterized in that: In step 3, the stirring time at room temperature is 20 to 40 minutes.

16. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 15, characterized in that: In step 3, the stirring time at room temperature is 30 min.

17. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 1, characterized in that: In step 3, the heating and stirring temperature is 60 to 80° C., and the time is 2 to 4 hours.

18. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 17, characterized in that: In step 3, the temperature of heating and stirring is 70° C. and the time is 3 h.

19. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 1, characterized in that: In step 3, the drying time at room temperature is 20 to 28 hours.

20. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 19, characterized in that: In step 3, the drying time at room temperature is 24 hours.

21. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 1, characterized in that: In step 3, the drying temperature is continued to be 60-80° C. and the drying time is 10-14 hours.

22. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 21, characterized in that: In step 3, the drying temperature is continued to be 70° C. and the drying time is 12 h.

23. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 1, characterized in that: In step 3, the calcination temperature is 300-400° C. and the calcination time is 1-3 hours.

24. The method for preparing a catalyst for the pyrolysis and oxidation of pharmaceutical waste salts by molten organic flue gas according to claim 23, characterized in that: In step 3, the calcination temperature is 350° C. and the calcination time is 2 h.

25. The catalyst prepared by the preparation method according to any one of claims 1 to 24.

26. The catalyst according to claim 25 is used in any one of the following (A1)-(A2): (A1) Application in the pyrolysis and oxidation of pharmaceutical waste salts in molten organic flue gas; (A2) Application in the preparation of products obtained by pyrolysis and oxidation of molten organic flue gas from pharmaceutical waste salts.

27. The use according to claim 26, characterized in that The method for using the catalyst comprises the following steps: using air flow to bring the organic smoke of molten pharmaceutical waste salt into the gas, passing through a cracking oxidation catalyst, and controlling the reaction temperature to deeply purify the macromolecular organic matter in the organic smoke of molten pharmaceutical waste salt.

28. The use according to claim 27, characterized in that The air velocity range of the air flow is 5000 to 20000 ml / gcat·h.

29. The use according to claim 28, characterized in that The space velocity of the air flow is 12000 ml / gcat·h.

30. The use according to claim 27, characterized in that The reaction temperature ranges from 300 to 500°C.

31. The use according to claim 30, characterized in that The reaction temperature is 350°C.

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