An electric-driven catalyst for catalytic purification of chlorinated aromatic hydrocarbons and its preparation method and use method

Abstract

The present invention provides an electric-driven catalyst for catalytically purifying chloroaromatic hydrocarbons, which belongs to the technical field of chloroaromatic hydrocarbon treatment. The electric-driven catalyst comprises Sb@SnO x (N) a conductive support material and a mixed oxide active component of Cr, Ce, and Co. The present invention also provides a method for preparing and using an electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons. The present invention provides an electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons, as well as its preparation and use methods, which are highly efficient in catalytically purifying chloroaromatic hydrocarbons with low energy consumption.

Description

Technical Field

[0001] The present invention relates to the technical field of chlorinated aromatic hydrocarbon treatment, and in particular to an electrically driven catalyst for catalytically purifying chlorinated aromatic hydrocarbons, and a preparation method and a use method thereof. Background Art

[0002] Industrial sources are the main emission sources of chlorinated volatile organic compounds (Cl-VOCs) and dioxin-like organic pollutants in my country. These chlorinated organic pollutants are highly toxic, chemically stable, and difficult to degrade, posing serious threats to the environment and human health.

[0003] The widespread use of chlorinated volatile organic compounds (VOCs) in industries like pharmaceuticals, petrochemicals, and packaging and printing results in high concentrations of these compounds in exhaust gases. For example, the chemically stable chlorinated aromatic hydrocarbon chlorobenzene is now subject to emission control for atmospheric pollutants from the petrochemical and pharmaceutical industries (GB 31572-2015, DB 31 / 310005-2021) and is included in the list of hazardous pollutants. Emission control of highly toxic dioxin-like pollutants remains a key focus of environmental oversight in key industries like waste incineration and steelmaking.

[0004] Among organized emission sources, end-of-pipe purification technology is the main reliance and last line of defense for controlling the emission of chlorinated organic pollutants. The development and application of high-efficiency purification technology has always been the focus of industry research.

[0005] Catalytic oxidation offers low energy consumption, high purification efficiency, and a wide range of applications. It can also serve as a key supplementary technology for ensuring that existing end-of-pipe treatment systems consistently meet emission standards or achieve ultra-low emissions. Currently, achieving high-efficiency, low-carbon catalytic degradation of chlorinated organic pollutants in industrial processes has become a pressing challenge in the field of industrial waste gas purification.

[0006] Catalytic oxidation technology can completely decompose chlorinated organic pollutants into non-toxic inorganic products such as CO2, H2O, and HCl, which are then purified and released into the environment. However, current catalytic degradation of chlorinated organic pollutants faces major drawbacks, including poor catalyst activity at low temperatures and susceptibility to chlorine poisoning. Currently, improving catalyst performance through methods such as optimizing catalyst composition and structure has been difficult to achieve significant breakthroughs, necessitating an urgent need to improve catalytic performance by altering the catalytic method.

[0007] By applying an external electric field to the catalyst bed in the temperature field (electric assistance) and directly electrifying the integral conductive material or conductive catalyst material loaded with the catalyst (electric drive), a unique current / electric field-Joule heat multi-field coupling effect is exhibited, which is expected to solve the problems of poor low-temperature activity and easy poisoning of catalysts in conventional thermal catalytic degradation technology.

[0008] The current catalytic oxidation treatment technology for catalytically oxidizing dioxins and other chlorinated organic pollutants has high energy consumption and relatively low efficiency in catalytically oxidizing dioxins and other chlorinated organic pollutants. At the same time, the preparation efficiency of this type of catalyst is also relatively low.

[0009] Therefore, there is an urgent need for an electrically driven catalyst with low energy consumption and high efficiency for catalytic purification of chlorinated aromatics and a preparation method thereof. Summary of the Invention

[0010] The technical problem to be solved by the present invention is to provide an electrically driven catalyst capable of catalytically purifying chlorinated aromatics with low energy consumption and high efficiency, as well as a preparation method and a use method thereof.

[0011] In order to solve the above technical problems, the present invention provides an electric-driven catalyst for catalytically purifying chlorinated aromatic hydrocarbons, wherein the electric-driven catalyst comprises Sb@SnO x (N) a mixture of a conductive support material and active components of Cr, Ce, and Co oxides;

[0012] The Sb@SnO x (N) The mole percentage of Sb in the conductive carrier material is 5 to 13 mol %, and the resistivity is 0.8 to 1.3 Ω / cm;

[0013] The Cr oxide active component includes Cr 6+ / Cr 3+ Two valence states of oxide active components, Cr 6+ The proportion of elements in two valence states is higher than 40%;

[0014] The Ce oxide active component includes Ce 4+ / Ce 3+ Two valence states of oxide active components, Ce 3+ The proportion of two valence elements is higher than 35%;

[0015] The Co oxide active component includes Co 3+ / Co 2+ Two valence states of oxide active components, Co 3+ The proportion of elements in two valence states is higher than 40%;

[0016] In the electrically driven catalyst, the molar ratio of Cr:Sn is 0.005-0.08, the molar ratio of Ce:Sn is 0.005-0.05, and the molar ratio of Co:Sn is 0.005-0.05.

[0017] Furthermore, the structure of the electrically driven catalyst is a porous monolithic structure.

[0018] Furthermore, the cross-sectional shape of the electrically driven catalyst perpendicular to the reaction gas flow is circular, square or other shapes that can fill the cross-sectional area of ​​the catalytic reactor.

[0019] The present invention also provides a method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics, comprising the following steps:

[0020] Take Sb@SnO x (N) a conductive support material and an active component precursor of oxides of Cr, Ce, and Co;

[0021] Dispersing active component precursors of oxides of Cr, Ce, and Co in ultrapure water to obtain dissolving solutions, and then mixing the dissolving solutions to obtain a mixed solution;

[0022] The mixed solution was mixed with Sb@SnO x (N) mixing the conductive carrier material and pre-extruding the mixture under vacuum to obtain a plastic mud material;

[0023] The plastic clay is filled into a mold and extruded to obtain a catalyst rough blank;

[0024] The catalyst rough body is dried and calcined in sequence to obtain an electrically driven catalyst.

[0025] Furthermore, the Sb@SnO x (N) The conductive support material is prepared by the following steps:

[0026] (1) Antimony trichloride and tin tetrachloride are dissolved in methanol, ammonia water is added after dissolution, and ultrasonic treatment is performed at 40-60°C for 90-110 minutes to obtain a solution containing antimony and tin elements;

[0027] (2) The solution containing antimony and tin elements was placed in a hydrothermal reactor, and the temperature was raised to 180-220°C at a rate of 2.5-3.5°C / min. After maintaining the temperature at 180-220°C for 350-380 min, the solution was naturally cooled to room temperature to obtain Sb@SnO x (N) a solution of a precursor;

[0028] (3) Containing Sb@SnO x (N) The precursor solution was filtered to obtain a solid mixture, and the solid mixture was washed with ultrapure water until the pH value of the supernatant was 7 to obtain Sb@SnO x (N) Precursor;

[0029] (4) Sb@SnO x The (N) precursor was dried at 70-90 °C for 250-350 min and then calcined at 500-700 °C for 250-350 min to obtain Sb@SnO x (N) Conductive carrier material.

[0030] Furthermore, the Cr oxide active component precursor is at least one of chromium nitrate and chromium trioxide, the Ce oxide active component precursor is two or more of cerium (III) nitrate hexahydrate, cerium (IV) nitrate, cerium oxide or ammonium cerium nitrate, and the Co oxide active component precursor is at least one of cobalt nitrate and cobalt oxide.

[0031] Furthermore, when the oxide active component precursors of Cr, Ce, and Co are dispersed in ultrapure water respectively, the ultrapure water temperature is 40-60° C., and the stirring and dispersing time is 150-200 min; when the dissolving solutions are mixed, the stirring and mixing is performed for 100-150 min to obtain a mixed solution.

[0032] Furthermore, the drying of the catalyst rough blank comprises:

[0033] Maintain at 55-65°C for 75-85 minutes, then increase the temperature to 80-90°C at a rate of 2.5-3.5°C / min;

[0034] After maintaining at 80-90°C for 75-85 min, heat to 100-110°C at a rate of 1.5-2.5°C / min;

[0035] After maintaining at 100-110°C for 55-65 min, cool naturally to room temperature.

[0036] Furthermore, the calcination of the catalyst rough body includes:

[0037] Raise the temperature from room temperature to 75-85°C at a rate of 1.5-2.5°C / min;

[0038] After maintaining at 75-85°C for 55-65 min, heat to 350-450°C at a rate of 2.5-3.5°C / min;

[0039] After maintaining at 350-450°C for 170-190 min, it is naturally cooled to room temperature.

[0040] The present invention further provides a method for using an electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons, wherein the electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons comprises the following steps:

[0041] The electrically driven catalyst is placed in a catalytic reactor, which is then installed after a laboratory simulation generator or before an industrial waste gas purification device;

[0042] Controlling the operating temperature of the electrically driven catalyst to 100-250°C;

[0043] A DC power supply with an output power of 0.79 to 102 W is connected to both ends of the electric-driven catalyst to perform electric-driven catalytic purification on chlorinated aromatics passing through the electric-driven catalyst.

[0044] The present invention provides an electrically driven catalyst for catalytically purifying chlorinated aromatic hydrocarbons, comprising a conductive antimony-doped tin oxide nano-oxide material (i.e., Sb@SnO x (N) conductive support material) and mixed oxide active components of Cr, Ce, and Co. The electric driven catalyst is Sb@SnO x (N) Conductive carrier material is used as a carrier, loaded with multivalent metal oxides (such as Cr 6+ / 3+ O x 、Ce 4+ / 3+ O x 、Co 3+ / 2+ O x As the active component of the electric-driven catalyst, the electric-driven catalyst can be simply expressed as CrO x -CeO x -CoO x / Sb@SnO x (N) Electrically driven catalyst.

[0045] Among them, in Sb@SnO x (N) Conductive carrier material, SnO x It is a commonly used transition metal oxide type catalyst carrier, and its conductivity is low, but its conductivity can be improved by adding Sb elements, thus realizing Sb@SnO x (N) The conductive carrier material forms a conductive path under the support of direct current, generating Joule heating effect. x (N) is a nanomaterial, which is beneficial to the active component (CrO x 、CeO x 、CoO x ) are highly dispersed on the surface, increasing the number of surface active sites and the stability of the active components, thereby enhancing the catalyst's low-temperature catalytic activity. Furthermore, the interaction between the active components and the support promotes the dechlorination of chlorinated organic pollutants during the catalytic oxidation process, thereby improving the catalyst's resistance to chlorine poisoning.

[0046] Precious metals have excellent catalytic oxidation activity as catalysts, but they have disadvantages such as susceptibility to chlorination deactivation / loss and high cost. Transition metal oxides such as Cr, Ce, and Co, which have high electron mobility and positive oxidation states, are highly stable and exhibit better resistance to chlorine poisoning.

[0047] Among them, the active component CrO x Good catalytic oxidation performance and highly dispersed Cr on the catalytic interface 6+and surrounding acid sites can effectively promote the deep oxidation of chlorinated aromatic organic pollutants.

[0048] Active component CeO x It has excellent oxygen storage capacity and oxygen activation conversion performance, good surface acidity and oxygen mobility, and is environmentally friendly and has low toxicity. x Oxygen vacancies are easily formed on the surface, and adding them into the catalytic system is beneficial to promote the formation of low-valent CrO x Oxidation to a high valence level can improve the low-temperature oxidation performance of the catalyst.

[0049] Active component CoO x With excellent redox ability, CoO x The catalyst can exhibit good resistance to chlorine poisoning and stability, and can effectively inhibit the formation of by-products, especially polychlorinated by-products, thereby improving the selectivity of non-toxic inorganic products such as CO2, H2O, and HCl.

[0050] Therefore, the present invention provides a method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics, wherein CrO x 、CeO x 、CoO x Mixed active components loaded on Sb@SnO x (N) CrO was prepared on a conductive carrier material. x -CeO x -CoO x / Sb@SnO x (N) The porous monolithic electrically driven catalyst not only does not affect the conductivity of the catalyst, but also promotes the x -CeO x -CoO x / Sb@SnO x (N) Conductive properties of electrically driven catalysts.

[0051] The CrO prepared by the present invention x -CeO x -CoO x / Sb@SnO x (N) The electrically driven catalyst is placed in a catalytic reactor, which is then installed after a laboratory simulation generator or before an industrial waste gas purification device. The catalytic reaction temperature is 100-250°C, and then the CrO x -CeO x -CoO x / Sb@SnO x(N) A DC power supply is connected to both ends of the electric-driven catalyst to keep the catalyst in a conductive state. When the chlorinated aromatic hydrocarbon flue gas contacts the catalyst surface, the active components in the electric-driven catalyst can efficiently catalyze the oxidation of dioxins, chlorobenzenes and other chlorinated aromatic hydrocarbon organic pollutants in the chlorinated aromatic hydrocarbon flue gas at a relatively low temperature of 100 to 250°C.

[0052] Since the electric-driven catalyst prepared by the present invention can catalytically purify chloroaromatic hydrocarbons at a relatively low reaction temperature, not only the energy consumption is low, but also the electric-driven catalyst prepared by the present invention has good electrical conductivity and uses a mixed oxide of Cr, Ce, and Co as the active component for catalytic oxidation, therefore, the efficiency of catalytic purification of chloroaromatic hydrocarbons is relatively high. x (N) The conductive carrier material loads oxides of transition metals such as Cr, Ce, and Co as active components, so that the prepared electric-driven catalyst has good resistance to chlorine poisoning and good low-temperature activity.

[0053] Compared with the prior art, the electrically driven catalyst for catalytically purifying chlorinated aromatics provided by the present invention and its preparation method and use method have the following beneficial effects.

[0054] 1. The electrically driven catalyst for catalytic purification of chlorinated aromatic hydrocarbons provided by the present invention can make up for the shortcomings of conventional non-conductive catalysts currently developed in laboratories and commercially used in the catalytic degradation of chlorinated aromatic hydrocarbon organic pollutants, thereby achieving efficient degradation and removal of various chlorinated aromatic hydrocarbon pollutants such as dioxins and chlorobenzene.

[0055] 2. The electrically driven catalyst for catalytic purification of chlorinated aromatics provided by the present invention can achieve efficient catalysis in the temperature range of 100 to 250°C, which makes up for the shortcomings of existing conventional non-conductive catalysts such as high reaction temperature, high energy consumption and low efficiency, and can significantly save system operating costs.

[0056] 3. The reaction temperature of an electrically driven catalyst for catalytically purifying chlorinated aromatics provided by the present invention is maintained by the Joule heat effect generated by the electric drive, which can achieve a rapid response of the reaction temperature in milliseconds, making up for the shortcomings of the existing conventional non-conductive catalysts, such as slow reaction temperature control rate and delayed target temperature rise. The reaction temperature can be regulated in real time and responded quickly through flexible control methods.

[0057] 4. The electrically driven catalyst for catalytically purifying chlorinated aromatics provided by the present invention has the advantage of better resistance to chlorine and water poisoning under low temperature conditions.

[0058] 5. The electric-driven catalyst for catalytically purifying chlorinated aromatics provided by the present invention has the advantages of easy operation and simple process during use. It does not require the consumption of reheated steam to increase the flue gas temperature, can directly replace existing catalytic purification process facilities, and can solve a large amount of energy consumption, reduce the actual operating costs of the enterprise, and has important application value in solving the emission problem of difficult-to-degrade chlorinated aromatics such as dioxins and chlorobenzene in industrial waste gas. BRIEF DESCRIPTION OF THE DRAWINGS

[0059] Figure 1 A flow chart of a method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics provided in an embodiment of the present invention;

[0060] Figure 2 A flow chart showing the catalytic oxidation of dioxins and chlorobenzene in a catalytic reactor after a laboratory simulation generator using an electrically driven catalyst for catalytic purification of chlorinated aromatics provided in an embodiment of the present invention;

[0061] Figure 3 A flow chart of catalytically oxidizing dioxins and chlorobenzene in which an electrically driven catalyst for catalytically purifying chlorinated aromatics provided in an embodiment of the present invention is installed in a catalytic reactor preceding an industrial waste gas purification device. DETAILED DESCRIPTION

[0062] An embodiment of the present invention provides an electrically driven catalyst for catalytically purifying chlorinated aromatic hydrocarbons, comprising a conductive antimony-doped tin oxide nano-oxide material (ie, Sb@SnO x (N) conductive support material) and mixed oxide active components of Cr, Ce, and Co.

[0063] Among them, Sb@SnO x (N) The molar percentage of Sb in the conductive carrier material is 5-13 mol%, Sb@SnO x (N) The resistivity of the conductive support material is 0.8 to 1.3 Ω / cm.

[0064] Among them, the active components of Cr oxide include Cr 6+ / Cr 3+ Two valence states of oxide active components, and Cr 6+ The proportion of the two valence elements is higher than 40%.

[0065] Ce oxide active components include Ce 4+ / Ce 3+ Two valence states of oxide active components, and Ce 3+ + The proportion of elements in both valence states is higher than 35%.

[0066] The active components of Co oxide include Co 3+ / Co 2+Two valence states of oxide active components, and Co 3+ The proportion of the two valence elements is higher than 40%.

[0067] That is, the electric driven catalyst provided by the present invention is Sb@SnO x (N) Conductive carrier material is used as a carrier, loaded with Cr 6+ / 3+ O x 、Ce 4+ / 3+ O x 、Co 3+ / 2+ O x Components composed of multivalent metal oxides as active components of electric-driven catalysts

[0068] The electrically driven catalyst of the present invention can be simply represented as CrO x -CeO x -CoO x / Sb@SnO x (N) Electrically driven catalyst.

[0069] The molar ratio of Cr:Sn elements is 0.005-0.08, the molar ratio of Ce:Sn elements is 0.005-0.05, and the molar ratio of Co:Sn elements is 0.005-0.05.

[0070] Furthermore, the structure of the electrically driven catalyst provided by the present invention is a porous monolithic structure.

[0071] The cross-sectional shape of the electrically driven catalyst of the porous monolithic structure perpendicular to the reaction gas flow is circular, square or other shapes that can fill the cross-sectional area of ​​the catalytic reactor.

[0072] The present invention provides an electric driven catalyst for catalytic purification of chlorinated aromatic hydrocarbons, wherein the Sb@SnO x (N) Conductive carrier material, in SnO x Doping Sb into SnO can improve x conductivity, thus achieving Sb@SnO x (N) The conductive carrier material forms a conductive path under the support of direct current, generating a Joule heating effect, which is conducive to a rapid response at low reaction temperatures and improves the low-temperature conductivity of the electrically driven catalyst.

[0073] Furthermore, the Sb@SnO x (N) is a nanomaterial, which is beneficial to the active component (CrO x 、CeO x 、CoO x) are highly dispersed on its surface, increasing the number of surface active sites and the stability of active components, thereby improving the low-temperature catalytic activity of the catalyst and improving the low-temperature conductivity of the electrically driven catalyst.

[0074] At the same time, in the electrically driven catalyst of the present invention, the oxides of transition metals such as Cr, Ce, and Co with high electron mobility and positive oxidation states are highly stable and exhibit better resistance to chlorine poisoning. The interaction between the active components and the carrier in the electrically driven catalyst is also beneficial to promoting the dechlorination effect during the catalytic oxidation of chlorinated organic pollutants, thereby improving the catalyst's resistance to chlorine poisoning.

[0075] See also Figure 1 The present invention provides a method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics, comprising the following steps:

[0076] Step 1) Take Sb@SnO x (N) Conductive support material and oxide active component precursors of Cr, Ce, and Co.

[0077] Among them, the Cr oxide active component precursor is at least one of chromium nitrate and chromium trioxide, the Ce oxide active component precursor is two or more of cerium (III) nitrate hexahydrate, cerium (IV) nitrate, cerium oxide or ammonium cerium nitrate, and the Co oxide active component precursor is at least one of cobalt nitrate and cobalt oxide.

[0078] The molar ratio of Cr:Sn elements is 0.005-0.08, the molar ratio of Ce:Sn elements is 0.005-0.05, and the molar ratio of Co:Sn elements is 0.005-0.05.

[0079] Therefore, when weighing Sb@SnO x (N) When the precursor of the carrier material and the oxide active components of Cr, Ce, and Co are prepared, Sb@SnO x (N) Support material and precursor of the active components of Cr, Ce, and Co oxides.

[0080] Among them, Sb@SnO x (N) The conductive support material is prepared by the following steps:

[0081] (1) Press Sb@SnO x (N) The molar percentage of Sb in the conductive carrier material is 5 to 13 mol%. Antimony trichloride and tin tetrachloride are dissolved in methanol. After dissolution, ammonia water is added and the mixture is ultrasonically treated at 40 to 60° C. for 90 to 110 minutes to obtain a solution containing antimony and tin elements.

[0082] As a best embodiment of the present invention, measured antimony trichloride and tin tetrachloride are dissolved in methanol, vigorously stirred for 180 minutes, and then a certain amount of ammonia water is added. The mixture is ultrasonically treated at 50° C. for 100 minutes to obtain a solution containing antimony and tin elements.

[0083] The stirring speed during vigorous stirring is above 400 r / min.

[0084] (2) The solution containing antimony and tin elements was placed in a hydrothermal reactor, and the temperature was raised to 180-220°C at a rate of 2.5-3.5°C / min. After maintaining the temperature at 180-220°C for 350-380 min, the solution was naturally cooled to room temperature to obtain Sb@SnO x (N) Precursor solution.

[0085] As a best embodiment of the present invention, a solution containing antimony and tin elements is placed in a hydrothermal reactor, heated to 200°C at a rate of 3°C / min, maintained at 200°C for 360 minutes, and then naturally cooled to room temperature to obtain Sb@SnO x (N) Precursor solution.

[0086] (3) Containing Sb@SnO x (N) The precursor solution was filtered to obtain a solid mixture, which was then rinsed with ultrapure water several times until the pH value of the supernatant reached 7, thereby obtaining Sb@SnO x (N) Precursor.

[0087] (4) Sb@SnO x The (N) precursor was dried at 70-90 °C for 250-350 min and then calcined at 500-700 °C for 250-350 min to obtain Sb@SnO x (N) Conductive carrier material.

[0088] As a best embodiment of the present invention, the obtained Sb@SnOx(N) precursor is dried at 80°C for 300 min and calcined at 600°C for 300 min to obtain the Sb@SnOx(N) conductive support material.

[0089] Step 2) The oxide active component precursors of Cr, Ce, and Co are dispersed in ultrapure water respectively, stirred and dissolved to obtain three dissolving solutions, and then the three dissolving solutions are mixed to obtain a mixed solution.

[0090] When the oxide active component precursors of Cr, Ce and Co are dispersed and dissolved in ultrapure water respectively, the ultrapure water temperature is 40-60° C. and the stirring and dispersing time is 150-200 minutes; when the dissolving solutions are mixed, the stirring and mixing is performed for 100-150 minutes to obtain a mixed solution.

[0091] As a best embodiment of the present invention, the precursors of the oxide active components of Cr, Ce, and Co are respectively stirred in ultrapure water at 50° C. for 180 min to obtain three dissolving solutions, and then the three dissolving solutions are mixed and stirred for another 120 min to obtain a mixed solution.

[0092] Step 3) Mix the mixed solution with Sb@SnO x (N) Conductive carrier materials are mixed and pre-extruded in vacuum to obtain plastic mud.

[0093] Step 4) The plastic clay is filled into a mold and extruded to obtain a catalyst rough billet.

[0094] Step 5) The catalyst rough body is dried and calcined in sequence to obtain a porous monolithic electric-driven catalyst.

[0095] The drying process of the catalyst rough blank includes:

[0096] First, the catalyst blank is kept at 55-65°C for 75-85 minutes, and then heated to 80-90°C at a rate of 2.5-3.5°C / min.

[0097] Then, after maintaining at 80-90°C for 75-85 min, the temperature was raised to 100-110°C at a rate of 1.5-2.5°C / min.

[0098] Then keep it at 100-110℃ for 55-65 min and then cool it naturally to room temperature.

[0099] As an optimal specific embodiment of the present invention, the temperature conditions of the catalyst rough drying process are preferably: maintain at 60°C for 80 min, and increase the temperature to 85°C at a rate of 3°C / min; maintain at 85°C for 80 min, and then increase the temperature to 105°C at a rate of 2°C / min; maintain at 105°C for 60 min, and then naturally cool to room temperature.

[0100] The heating rate in the drying process is 3°C / min.

[0101] The calcination of the catalyst rough blank includes:

[0102] First, the dried catalyst rough billet is heated from room temperature to 75-85°C at a rate of 1.5-2.5°C / min.

[0103] Then, after maintaining at 75-85°C for 55-65 min, the temperature is raised to 350-450°C at a rate of 2.5-3.5°C / min.

[0104] Finally, after maintaining the temperature at 350-450° C. for 170-190 min, the porous monolithic electric-driven catalyst was obtained by naturally cooling to room temperature.

[0105] As an optimal specific embodiment of the present invention, the temperature conditions of the catalyst rough calcination process are preferably: heating from room temperature to 80°C at a rate of 2°C / min; maintaining at 80°C for 60 min, then heating to 400°C at a rate of 3°C / min; maintaining at 400°C for 180 min, and then naturally cooling to room temperature.

[0106] The heating rate during the calcination process was 3°C / min.

[0107] The active oxide components of Cr, Ce and Co in the catalyst prepared after calcination refer to the active oxide components containing Cr, Ce and Co respectively. 6 + / Cr 3+ 、Ce 4+ / Ce 3+ , and Co 3+ / Co 2+ Two valence states coexist in the oxide active component, and Cr 6+ 、Ce 3+ 、Co 3+ The element mass accounts for more than 40%, 35% and 40% respectively.

[0108] The present invention provides a method for using an electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons. As a specific embodiment of the present invention, the electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons comprises the following steps:

[0109] Step 1) See Figure 2 , the electrically driven catalyst prepared by the present invention is placed in a catalytic reactor, and then the catalytic reactor is installed after the laboratory simulation generator.

[0110] Step 2) Controlling the operating temperature of the electrically driven catalyst to be between 100°C and 250°C.

[0111] Step 3) Connecting a DC power supply with an output power of 0.79 to 102 W to both ends of the electrically driven catalyst to perform electrically driven catalytic purification on the chlorinated aromatics passing through the electrically driven catalyst.

[0112] As another specific embodiment of the present invention, the catalytic purification of chlorinated aromatics by an electrically driven catalyst comprises the following steps:

[0113] Step 1) See Figure 3 , the electrically driven catalyst prepared by the present invention is placed in a catalytic reactor, and then the catalytic reactor is installed before the industrial waste gas purification device.

[0114] Step 2) Controlling the operating temperature of the electrically driven catalyst to be between 100°C and 250°C.

[0115] Step 3) Connecting a DC power supply with an output power of 0.79 to 102 W to both ends of the electrically driven catalyst to perform electrically driven catalytic purification on the chlorinated aromatics passing through the electrically driven catalyst.

[0116] Among them, chlorinated aromatic hydrocarbons include chlorobenzene-type volatile organic compounds, chlorinated PAHs, and dioxin-type organic pollutants.

[0117] The present invention provides a method for using an electrically driven catalyst for catalytically purifying chlorinated aromatics, which has the advantages of easy operation and simple process. It does not require the consumption of reheated steam to increase the flue gas temperature, can directly replace existing catalytic purification process facilities, and can solve a large amount of energy consumption, reduce the actual operating costs of enterprises, and has important application value in solving the emission problem of difficult-to-degrade chlorinated aromatics such as dioxins and chlorobenzenes in industrial waste gas.

[0118] The following examples specifically illustrate an electrically driven catalyst for catalytically purifying chlorinated aromatics provided by the present invention, as well as its preparation method and use method.

[0119] In the embodiment of the present invention, the industrial waste gas refers to the waste gas discharged from the pharmaceutical, petrochemical, packaging and printing industries and the flue gas generated during the incineration of solid waste. The porous monolithic electric-driven catalyst for the efficient catalytic degradation of dioxins and chlorinated aromatic hydrocarbons represented by chlorobenzene provided in the embodiment of the present invention has a composition represented by CrO x -CeO x -CoO x / Sb@SnO x (N), the electrically driven catalyst consists of an active component (CrO x 、CeO x 、CoO x ) and conductive antimony-doped tin oxide nanomaterials (Sb@SnO x (N) conductive carrier material).

[0120] In Examples 1-15 of the present invention, Sb@SnO x (N) The conductive carrier materials are all prepared by hydrothermal method. The specific preparation method is as follows:

[0121] (1) Dissolve the measured amount of antimony trichloride and tin tetrachloride in methanol, stir vigorously for 180 min, add a certain amount of ammonia water, and ultrasonically treat at 50°C for 100 min to obtain solution A containing antimony and tin elements.

[0122] (2) The ultrasonic solution A was placed in a hydrothermal reactor and heated to 200°C at a rate of 3°C / min. After maintaining at 200°C for 360 min, it was naturally cooled to room temperature to obtain Sb@SnO x (N) Precursor solution B.

[0123] (3) Filter solution B to obtain a solid mixture, and rinse it with ultrapure water several times until the pH value of the supernatant is 7 to obtain Sb@SnO x (N) Precursor sample.

[0124] (4) The obtained Sb@SnO x (N) The precursor sample was dried at 80 °C for 300 min and calcined at 600 °C for 300 min to obtain Sb@SnO x (N) Conductive support material, the heating rate of the above drying and calcining is 3°C / min.

[0125] In the step (1), the vigorous stirring means that the stirring speed is greater than 400 r / min; the amount of each material is accurately controlled to ensure that Sb@SnO x (N) The molar ratio of Sb and Sn in the conductive carrier material meets the molar ratio and mass ratio requirements of the raw materials. The following Examples 1-15 are all operated in the same manner and will not be repeated here.

[0126] The electrically driven catalysts of Examples 1-15 of the present invention were all prepared by extrusion molding, and the specific preparation methods are as follows:

[0127] The following temperature program was used for the preparation, drying, and calcination of the porous monolithic catalyst rough blank: the precursors of the oxide active components of Cr, Ce, and Co were fully stirred in ultrapure water at 50°C for 180 min, and then stirred for another 120 min. The mixed solution was then mixed with Sb@SnO x (N) After the carrier material is thoroughly mixed and stirred, it is vacuum pre-extruded to obtain a plastic slurry, which is further extruded to obtain a porous monolithic catalyst blank; the temperature conditions for the porous monolithic catalyst blank during the drying process are: maintaining at 60°C for 80 minutes, heating to 85°C at a rate of 3°C / min; maintaining at 85°C for 80 minutes, heating to 105°C at a rate of 2°C / min; maintaining at 105°C for 60 minutes, and then naturally cooling to room temperature; the temperature conditions for the porous monolithic catalyst blank during the calcination process are: heating from room temperature to 80°C at a rate of 2°C / min; maintaining at 80°C for 60 minutes, heating to 400°C at a rate of 3°C / min; maintaining at 400°C for 180 minutes, and then naturally cooling to room temperature. The following examples are all operated in the same manner and are not repeated here.

[0128] Example 1

[0129] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, and a porous monolithic catalyst rough billet is obtained by integral extrusion molding, and then dried and calcined to finally obtain catalyst 1. In catalyst 1, the converted support material Sb@SnO x The molar percentage of Sb in (N) is 1 mol%, and the molar ratio of Cr:Sn in the catalytic system is 0.05.

[0130] Example 2

[0131] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, and a porous monolithic catalyst rough billet is obtained by integral extrusion molding, and then dried and calcined to finally obtain catalyst 2. In catalyst 2, the converted support material Sb@SnO x The molar percentage of Sb in (N) is 5 mol%, and the molar ratio of Cr:Sn in the catalytic system is 0.05.

[0132] Example 3

[0133] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, and a porous monolithic catalyst rough billet is obtained by integral extrusion molding, and then dried and calcined to finally obtain catalyst 3. In catalyst 3, the converted support material Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, and the molar ratio of Cr:Sn in the catalytic system is 0.05.

[0134] Example 4

[0135] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, and a porous monolithic catalyst rough billet is obtained by integral extrusion molding, and then dried and calcined to finally obtain catalyst 4. In catalyst 4, the converted support material Sb@SnO x The molar percentage of Sb in (N) is 15 mol%, and the molar ratio of Cr:Sn in the catalytic system is 0.05.

[0136] Example 5

[0137] Weigh Sb@SnO according to the set molar ratio x (N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, catalyst 5 is finally obtained. In catalyst 5, the Sb@SnO in the carrier material after conversion is xThe molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.005, the molar ratio of Ce:Sn is 0.005, and the molar ratio of Co:Sn is 0.005.

[0138] Example 6

[0139] Weigh Sb@SnO according to the set molar ratio x (N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, catalyst 6 is finally obtained. In catalyst 6, the converted carrier material Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.08, the molar ratio of Ce:Sn is 0.005, and the molar ratio of Co:Sn is 0.005.

[0140] Example 7

[0141] Weigh Sb@SnO according to the set molar ratio x (N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, catalyst 7 is finally obtained. In catalyst 7, the Sb@SnO in the carrier material after conversion is x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.005, the molar ratio of Ce:Sn is 0.05, and the molar ratio of Co:Sn is 0.005.

[0142] Example 8

[0143] Weigh Sb@SnO according to the set molar ratio x (N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, catalyst 8 is finally obtained. In catalyst 8, the converted carrier material Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.005, the molar ratio of Ce:Sn is 0.005, and the molar ratio of Co:Sn is 0.05.

[0144] Example 9

[0145] Weigh Sb@SnO according to the set molar ratio x(N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, catalyst 9 is finally obtained. In catalyst 9, the converted carrier material Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.08, the molar ratio of Ce:Sn is 0.05, and the molar ratio of Co:Sn is 0.05.

[0146] Example 10

[0147] Weigh Sb@SnO according to the set molar ratio x (N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, a catalyst 10 is finally obtained. In the catalyst 10, the Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.045, the molar ratio of Ce:Sn is 0.01, and the molar ratio of Co:Sn is 0.015.

[0148] Example 11

[0149] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, cerium (IV) nitrate, cobalt nitrate, and the like are extruded to obtain a rough billet of a porous monolithic catalyst, which is dried and calcined to obtain catalyst 11. In catalyst 11, the converted support material contains Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.045, the molar ratio of Ce:Sn is 0.01, and the molar ratio of Co:Sn is 0.015.

[0150] Example 12

[0151] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, cerium oxide, cobalt nitrate, by integral extrusion molding to obtain a porous monolithic catalyst rough billet, after drying and calcination process, finally obtain catalyst 12. In catalyst 12, the converted support material Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.045, the molar ratio of Ce:Sn is 0.01, and the molar ratio of Co:Sn is 0.015.

[0152] Example 13

[0153] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium nitrate, cerium ammonium nitrate, cobalt nitrate, the porous monolithic catalyst rough billet is obtained by integral extrusion molding, and after drying and calcination, the catalyst 13 is finally obtained. In the catalyst 13, the Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.045, the molar ratio of Ce:Sn is 0.01, and the molar ratio of Co:Sn is 0.015.

[0154] Example 14

[0155] Weigh Sb@SnO according to the set molar ratio x (N) support material, chromium oxide, cerium (III) nitrate hexahydrate, and cobalt nitrate are used to obtain a rough billet of a porous monolithic catalyst by an integral extrusion molding method. After drying and calcination, catalyst 14 is finally obtained. In catalyst 14, the Sb@SnO in the support material after conversion is x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.045, the molar ratio of Ce:Sn is 0.01, and the molar ratio of Co:Sn is 0.015.

[0156] Example 15

[0157] Weigh Sb@SnO according to the set molar ratio x (N) carrier material, chromium nitrate, cerium (III) nitrate hexahydrate, and cobalt oxide are extruded to obtain a rough billet of a porous monolithic catalyst, which is dried and calcined to finally obtain catalyst 15. In catalyst 15, the converted carrier material Sb@SnO x The molar percentage of Sb in (N) is 10 mol%, the molar ratio of Cr:Sn in the catalytic system is 0.045, the molar ratio of Ce:Sn is 0.01, and the molar ratio of Co:Sn is 0.015.

[0158] In order to verify the catalytic effect of the catalysts prepared in Examples 1-15 of the present invention, Figure 1 or Figure 2 As shown, the catalyst prepared in the embodiment of the present invention is used for purification of laboratory simulated atmosphere or industrial waste gas.

[0159] The specific purification treatment method is as follows: the electric-driven catalyst prepared in the embodiment of the present invention is filled in a catalytic reactor, and the catalytic reactor can provide direct current to the catalyst through a power supply to generate Joule heating effect to heat the catalyst body, or provide the catalyst body with a corresponding reaction temperature through an external heat source such as steam or flue gas. The catalytic reactor is installed after the laboratory simulation generator or before the industrial waste gas purification device; during the simulated gas or waste gas purification process, the operating temperature of the catalyst is 100-250°C, the output power of the DC power supply is 0.79-4.13 W, and the experimental volume space velocity ratio is 10000 h -1 , in order to achieve efficient catalytic oxidation of dioxins and chlorobenzene-type chlorinated aromatic hydrocarbons.

[0160] Specifically, Examples 3, 10, and 11 were used to verify the catalytic effect on chloroaromatic hydrocarbons. The experimental simulated gas was introduced into the catalytic reactor via a laboratory simulation generator, while the industrial waste gas was directly introduced into the catalytic reactor. The industrial waste gas was pharmaceutical waste gas and packaging and printing industry waste gas. The average initial concentration of dioxins in the experimental simulated gas or industrial waste gas was 0.35 ng I-TEQ / Nm 3 The average initial concentration of chlorobenzene was 205 ppm; the average initial concentration of dioxins in pharmaceutical industrial waste gas was 0.23 ng I-TEQ / Nm 3 The average initial concentration of chlorobenzene was 186 ppm; the average initial concentration of dioxins in waste gas from the packaging and printing industry was 0.19 ng I-TEQ / Nm 3 , the average initial concentration of chlorobenzene was 157 ppm.

[0161] The removal rates of dioxins and chlorobenzene in experimental simulated gas, pharmaceutical industry waste gas and packaging and printing industry waste gas by the electrically driven catalysts prepared in Examples 3, 10 and 11 of the present invention at different temperatures and different heating powers to maintain reaction operation are shown in Table 1.

[0162] Table 1

[0163]

[0164] In order to compare the catalytic effects of the electrically driven catalyst prepared in the embodiment of the present invention with those of the catalyst prepared in the prior art, a catalyst was prepared according to the following comparative example.

[0165] Comparative Example 1

[0166] The CrO prepared in Example 10 was used. x -CeO x -CoO x / Sb@SnO x(N) A porous monolithic electrically driven catalyst is loaded into a catalytic reactor in the same manner as in Example 10 of the present invention, and the same reaction temperature (100, 150, 200, and 250° C.) is maintained by external heating of the catalytic reactor, and simulated gas or industrial waste gas of the same composition is introduced.

[0167] Comparative Example 2

[0168] The CrO prepared in Example 11 was used x -CeO x -CoO x / Sb@SnO x (N) A porous monolithic electrically driven catalyst is loaded into a catalytic reactor in the same manner as in Example 11 of the present invention, and the same reaction temperature (150° C.) is maintained by external heating of the catalytic reactor, and simulated gas or industrial waste gas of the same composition is introduced.

[0169] Comparative Example 3

[0170] Commercial catalyst 1 was loaded into a catalytic reactor using the same method as in Example 10 of the present invention. External heating of the catalytic reactor was used to maintain the same reaction temperature (150°C). Simulated gas or industrial waste gas with the same composition was introduced. Commercial catalyst 1 primarily consisted of V2O5 (0.9 wt%), Pt (0.8 wt%), and Al2O3 (98.3 wt%).

[0171] Comparative Example 4

[0172] Commercial catalyst 2 was loaded into a catalytic reactor using the same method as in Example 10 of the present invention. External heating of the catalytic reactor was used to maintain the same reaction temperature (150°C). Simulated gas or industrial waste gas with the same composition was introduced. Commercial catalyst 2 primarily consisted of Pt (0.8 wt%), Pd (0.44 wt%), Al2O3 (96.5 wt%), and CeO2 (2.3 wt%).

[0173] The removal rates of dioxins and chlorobenzene in experimental simulated gas, pharmaceutical industry waste gas and packaging and printing industry waste gas by the electrically driven catalysts prepared in Comparative Examples 3, 10 and 11 of the present invention at different temperatures and different heating powers to maintain reaction operation are shown in Table 2.

[0174] Table 2

[0175]

[0176] A comparison of the data in Tables 1 and 2 shows that the porous monolithic electrically driven catalyst prepared using embodiments of the present invention, when heated by the Joule heating effect generated by the direct current provided by a DC power supply, can achieve more efficient catalytic oxidation of chlorinated aromatic organic pollutants such as dioxins and chlorobenzene at lower energy consumption and lower temperatures. This overcomes the shortcomings of existing catalytic reaction devices, such as high operating energy consumption and low reaction activity, caused by the use of external reactor heating. Furthermore, the electrically driven catalyst preparation method provided by the present invention is simple to operate and has low operating costs, and has great application value in the future fields of industrial waste gas purification and ambient air purification.

[0177] Finally, it should be noted that the above specific implementation methods are only used to illustrate the technical solutions of the present invention and are not limiting. Although the present invention has been described in detail with reference to examples, those skilled in the art should understand that the technical solutions of the present invention can be modified or replaced by equivalents without departing from the spirit and scope of the technical solutions of the present invention, which should all be included in the scope of the claims of the present invention.

Claims

1. An electrically driven catalyst for catalytically purifying chlorinated aromatics, characterized in that: The electrically driven catalyst comprises a mixture of a Sb@SnOx(N) conductive support material and active components of Cr, Ce, and Co oxides; The molar percentage of Sb in the Sb@SnOx(N) conductive carrier material is 5 to 13 mol %, and the resistivity is 0.8 to 1.3 Ω / cm; The Cr oxide active component includes Cr 6+ / Cr 3+ Two valence states of oxide active components, Cr 6+ The proportion of elements in two valence states is higher than 40%; The Ce oxide active component includes Ce 4+ / Ce 3+ Two valence states of oxide active components, Ce 3+ The proportion of two valence elements is higher than 35%; The Co oxide active component includes Co 3+ / Co 2+ Two valence states of oxide active components, Co 3+ The proportion of elements in two valence states is higher than 40%; In the electrically driven catalyst, the molar ratio of Cr:Sn is 0.005-0.08, the molar ratio of Ce:Sn is 0.005-0.05, and the molar ratio of Co:Sn is 0.005-0.05; The Sb@SnOx(N) conductive carrier material is a conductive antimony-doped tin oxide nano-oxide material.

2. The electrically driven catalyst for catalytic purification of chlorinated aromatics according to claim 1, characterized in that: The structure of the electrically driven catalyst is a porous monolithic structure.

3. The electrically driven catalyst for catalytically purifying chlorinated aromatics according to claim 2, characterized in that: The cross-sectional shape of the electrically driven catalyst perpendicular to the reaction gas flow is circular, square or other shapes that can fill the cross-sectional area of ​​the catalytic reactor.

4. A method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics according to any one of claims 1 to 3, characterized in that: The steps include: Take Sb@SnOx(N) conductive support material and oxide active component precursors of Cr, Ce, and Co; Dispersing active component precursors of oxides of Cr, Ce, and Co in ultrapure water to obtain dispersions, respectively, and then mixing the dispersions to obtain a mixed solution; The mixed liquid is mixed with the Sb@SnOx(N) conductive carrier material, and pre-extruded by vacuum to obtain a plastic mud material; The plastic clay is filled into a mold and extruded to obtain a catalyst rough blank; The catalyst rough body is dried and calcined in sequence to obtain an electrically driven catalyst.

5. The method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics according to claim 4, characterized in that: The Sb@SnOx(N) conductive support material is prepared by the following steps: (1) Antimony trichloride and tin tetrachloride are dissolved in methanol, ammonia water is added after dissolution, and ultrasonic treatment is performed at 40-60°C for 90-110 minutes to obtain a solution containing antimony and tin elements; (2) placing a solution containing antimony and tin elements into a hydrothermal reactor, heating the temperature to 180-220°C at a rate of 2.5-3.5°C / min, maintaining the temperature at 180-220°C for 350-380 min, and then naturally cooling the temperature to room temperature to obtain a solution containing a Sb@SnOx(N) precursor; (3) Filtering the solution containing the Sb@SnOx(N) precursor to obtain a solid mixture, and washing the solid mixture with ultrapure water until the pH value of the supernatant reaches 7 to obtain the Sb@SnOx(N) precursor; (4) The Sb@SnOx(N) precursor was dried at 70-90°C for 250-350 min, and then calcined at 500-700°C for 250-350 min to obtain the Sb@SnOx(N) conductive support material.

6. The method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics according to claim 4, characterized in that: The Cr oxide active component precursor is at least one of chromium nitrate and chromium trioxide, the Ce oxide active component precursor is two or more of cerium (III) nitrate hexahydrate, cerium (IV) nitrate, cerium oxide or ammonium cerium nitrate, and the Co oxide active component precursor is at least one of cobalt nitrate and cobalt oxide.

7. The method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics according to claim 4, characterized in that: When the oxide active component precursors of Cr, Ce and Co are dispersed in ultrapure water respectively, the ultrapure water temperature is 40-60° C. and the stirring and dispersing time is 150-200 minutes; when the dispersions are mixed, the mixture is stirred for 100-150 minutes to obtain a mixed solution.

8. The method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics according to claim 4, characterized in that: The drying of the catalyst rough billet comprises: Maintain at 55-65°C for 75-85 minutes, then increase the temperature to 80-90°C at a rate of 2.5-3.5°C / min; After maintaining at 80-90°C for 75-85 min, heat to 100-110°C at a rate of 1.5-2.5°C / min; After maintaining at 100-110°C for 55-65 min, cool naturally to room temperature.

9. The method for preparing an electrically driven catalyst for catalytically purifying chlorinated aromatics according to claim 4, characterized in that: The calcination of the catalyst rough body comprises: Raise the temperature from room temperature to 75-85°C at a rate of 1.5-2.5°C / min; After maintaining at 75-85°C for 55-65 min, heat to 350-450°C at a rate of 2.5-3.5°C / min; After maintaining at 350-450°C for 170-190 min, it is naturally cooled to room temperature.

10. A method for using the electrically driven catalyst for catalytically purifying chloroaromatic hydrocarbons according to any one of claims 1 to 3, characterized in that: The catalytic purification of chlorinated aromatics by the electrically driven catalyst comprises the following steps: The electrically driven catalyst is placed in a catalytic reactor, which is then installed after a laboratory simulation generator or before an industrial waste gas purification device; Controlling the operating temperature of the electrically driven catalyst to 100-250°C; A DC power supply with an output power of 0.79 to 102 W is connected to both ends of the electric-driven catalyst to perform electric-driven catalytic purification on chlorinated aromatics passing through the electric-driven catalyst.

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