CN111121070B - Treatment method for normal-temperature catalytic ignition of VOCs (volatile organic chemicals) self-sustaining combustion - Google Patents

Treatment method for normal-temperature catalytic ignition of VOCs (volatile organic chemicals) self-sustaining combustion Download PDF

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CN111121070B
CN111121070B CN201811277747.6A CN201811277747A CN111121070B CN 111121070 B CN111121070 B CN 111121070B CN 201811277747 A CN201811277747 A CN 201811277747A CN 111121070 B CN111121070 B CN 111121070B
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CN111121070A (en
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杨沙沙
王国清
王育
张利军
刘小波
彭晖
刘俊杰
马天石
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

The invention relates to a treatment method for catalyzing and igniting VOCs to burn VOCs in a self-sustaining manner at normal temperature, belonging to the technical field of VOCs-containing waste gas treatment. The processing methodThe method comprises the following steps: in the catalytic ignition stage, at normal temperature and normal pressure, when the temperature of a catalyst bed layer in a reactor filled with the doped precious metal composite oxide catalyst is 30-45 ℃, VOCs waste gas and H are mixed2Introducing into a reactor, introducing air to make VOCs waste gas catalytically initiate combustion, entering a catalytic self-sustaining combustion stage, and stopping introducing H2And the feed flow of the VOCs waste gas is adjusted, the volume flow of the introduced air is adjusted, the reaction is developed into the self-sustaining combustion reaction of the VOCs waste gas, and the VOCs waste gas is thoroughly oxidized into carbon dioxide and water and then is discharged through the outlet of the reactor. Compared with the traditional VOCs catalytic combustion ignition technology, the method does not need external auxiliary heating, does not need to newly add an ignition device, can be realized at normal temperature, has simple process and is beneficial to environmental protection.

Description

Treatment method for normal-temperature catalytic ignition of VOCs (volatile organic chemicals) self-sustaining combustion
Technical Field
The invention relates to the technical field of treatment of waste gas containing VOCs, in particular to a treatment method for catalyzing and igniting VOCs to burn by self-sustaining at normal temperature.
Background
Common VOCs purification technologies include condensation, adsorption, absorption, catalysis, biological methods, and the like, which are widely applied. The catalytic method is to heat VOCs to the ignition temperature (200-450 ℃) to realize the catalytic and non-catalytic combustion reaction of the VOCs to generate carbon dioxide and water.
Patent CN106979526A provides a method for rapidly igniting low-temperature plasma in which VOCs are catalyzed and self-sustained to burn at normal temperature and pressure. A catalyst is placed in a discharge area in a plasma reactor, gas discharge is carried out after voltage is applied to generate low-temperature plasma, degradation reaction of VOCs is rapidly developed into self-sustaining combustion under the synergistic action of the low-temperature plasma and the catalyst through waste gas to be treated containing VOCs with certain concentration in the reactor, and the VOCs are thoroughly oxidized into carbon dioxide and discharged. Compared with the traditional catalytic combustion ignition technology, the method does not need auxiliary heating energy, can be carried out at normal temperature and normal pressure, and has the advantages of simple process, rapid ignition and low energy consumption. Similar methods are also proposed in patents CN104689713A and CN 105478136A. But needs low-temperature plasma reactor equipment, and is suitable for purifying industrial source organic waste gas with large air quantity and low concentration by cooperating with the plasma technology.
The petrochemical small and middle test devices produce VOCs waste gas containing a certain amount of low unsaturated hydrocarbons, the total amount is small and dispersed, the economic benefit is not easy to recycle, and meanwhile, the discharge treatment of the waste gas often fails to draw sufficient attention. So far, a catalytic combustion technology which is regarded as relatively high economic value aiming at the VOCs waste gas is still lacking at home and abroad.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a treatment method for catalyzing and igniting VOCs to burn by self at normal temperature. The treatment method for VOCs catalytic self-sustaining combustion at normal temperature (not less than 30 ℃) and normal pressure is particularly suitable for treating VOCs waste gas containing a certain amount of low unsaturated hydrocarbon. The method can ignite the VOCs waste gas and burn the waste gas in a self-sustaining manner without external auxiliary heating energy, has simple process and is beneficial to environmental protection.
The treatment method for normal-temperature catalytic ignition of VOCs self-sustaining combustion can comprise the following steps:
in the catalytic ignition stage, at normal temperature (more than or equal to 30 ℃, preferably 30-50 ℃, more preferably 30-45 ℃) and normal pressure (10-1000000 kpa, preferably 100-10000 kpa), when the temperature of a catalyst bed layer in a reactor filled with the doped noble metal composite oxide catalyst is 30-45 ℃, VOCs waste gas and H are mixed2Introducing into a reactor to remove VOCs waste gas and H2The space velocity of the catalyst is 100-10000 h-1Then introducing air to catalyze and ignite the VOCs waste gas, and rapidly heating the temperature of a catalyst bed layer to 100-500 ℃; entering a catalytic self-sustaining combustion stage, and stopping introducing H2And adjusting the feeding flow of the VOCs waste gas, adjusting the volume flow of the introduced air to be 5-30 times (preferably 10-20 times) of the volume flow of the VOCs, adjusting the volume airspeed of the doped noble metal composite oxide catalyst, developing the reaction into a self-sustaining combustion reaction of the VOCs waste gas, and completely oxidizing the VOCs waste gas into carbon dioxide and water and then discharging the carbon dioxide and water through an outlet of the reactor.
Wherein the content of the first and second substances,
in the VOCs waste gas, the content of C1-C4 unsaturated hydrocarbon is at least 5-100 vol%, preferably 10-60 vol% of the total volume of the VOCs waste gas.
In the catalytic pilot phase, H2The amount of the unsaturated hydrocarbon is 0 to 5 times, preferably 0.1 to 2 times, the volume of the unsaturated hydrocarbon containing C1 to C4 in the VOCs waste gas. When VOCs waste gas contains H2When H is not added, it is considered that2。
In the catalytic ignition stage, the space velocity of the doped noble metal composite oxide catalyst is 100-10000 h-1Preferably 500 to 10000h-1More preferably 500 to 5000 hours-1。
And in the catalytic ignition stage, the volume flow of the introduced air is 1-15 times of the volume flow of the VOCs.
In the catalytic self-sustaining combustion stage, the volume space velocity of the doped noble metal composite oxide catalyst is controlled to be 1000-100000 h by adjusting the feed flow of the VOCs waste gas-1More preferably 3000-10000 h-1。
According to the invention, in order to be able to better control the combustion reaction, the method may comprise a cooling step; the cooling step may be to control the temperature of the gas (the main components of which are carbon dioxide and water) after the combustion reaction to be below 1000 ℃, preferably 500 to 800 ℃ by using cooling water. The cooling water may be provided in a manner conventional in the art, for example, a circulation pipe for the cooling water may be provided around or inside the apparatus for performing the combustion reaction, thereby facilitating the cooling water to carry heat. In particular, the reactor can also be provided with a flow pipeline; the flow conduit may be arranged inside the reactor or at the periphery of the reactor; the cooling water circulates in the circulating pipeline, so that the cooling water can carry heat conveniently.
The doped precious metal composite oxide catalyst can comprise a precious metal active component, an oxygen storage material cerium zirconium solid solution and a carrier; the carrier contains Al2O3A carrier;
wherein, the content of the noble metal active component is 0.03 to 5 parts by weight, preferably 0.05 to 3 parts by weight, more preferably 0.05 to 1.5 parts by weight, the content of the oxygen storage material cerium zirconium solid solution is 5 to 40 parts by weight, preferably 10 to 30 parts by weight, and the balance is the carrier, based on 100 parts by weight of the total weight of the catalyst.
Wherein the noble metal active component is selected from Pd and/or Pt.
The oxygen storage material cerium-zirconium solid solution is a cerium pickaxe solid solution which is formed by performing a high-temperature solid-phase reaction at 500-1200 ℃ (preferably 700-900 ℃) and has a cerium-zirconium molar ratio (Ce/Zr) of 0.5-3.
The carrier comprises large-surface Al2O3A carrier; the Al is2O3The specific surface of the carrier can be 100-300 m2/g。
The preparation method of the cerium-zirconium solid solution comprises the following steps:
weighing cerium salt and zirconium salt according to the molar ratio of cerium to zirconium, dissolving the cerium salt and the zirconium salt in an aqueous solution to prepare a mixed solution with the total solute concentration of 0.1-5 mol/L (preferably 0.2-2 mol/L), diluting 25 wt% of ammonia water to 0.1-10 wt% (preferably 1-5 wt%) of the mixed solution as a precipitator, placing the mixed solution in a three-neck flask, slowly dripping the mixed solution of cerium salt and zirconium salt under the condition of vigorous stirring until the pH value of the solution is 9-11, continuing stirring after dripping, standing overnight, washing with deionized water, filtering, drying a filter cake, then programming to 500-1200 ℃ under flowing air, preferably 700-900 ℃, roasting, and preparing the catalyst aid cerium-zirconium solid solution.
The cerium salt can be selected from cerium nitrate, cerium sulfate and cerium acetate;
the zirconium salt may be selected from zirconyl nitrate, zirconium oxychloride, or zirconium tetrachloride.
The preparation method of the doped noble metal composite oxide catalyst can specifically select a common wet forming method.
The wet forming method may specifically include the following steps:
the oxygen storage material cerium zirconium solid solution, the auxiliary agent and Al2O3And kneading the carrier and a forming assistant, extruding and forming, drying at 80-120 ℃ for 3-10 h, roasting at 250-600 ℃ for 3-5 h to obtain a catalyst carrier, soaking the required noble metal active component in equal volume, drying at 80-120 ℃ for 3-10 h, and roasting at 250-600 ℃ for 3-5 h to obtain the catalyst carrier.
The forming auxiliary agent can be selected from a binder, an extrusion aid and the like; the molding can be in the shapes of strips, raschig rings, honeycombs and the like. The molding aid can be used in an amount of Al2O3The carrier is 0.5-3% of the weight and can be adjusted according to actual conditions.
The auxiliary agent is selected from sol; the sol may be at least one selected from titanium sol, silica sol, water glass and silane. The dosage of the auxiliary agent is Al2O31-5% of the weight of the carrier.
The doped noble metal composite oxide catalyst can catalyze and ignite VOCs material flow containing a certain amount of low unsaturated hydrocarbon and hydrogen at the temperature of more than or equal to 30 ℃, has good hydrothermal stability and high temperature stability, and still has good catalytic combustion activity after accelerated aging at 1000 ℃.
The substantial difference between the present invention and the prior art is: the invention provides a treatment method for VOCs catalytic self-sustaining combustion at normal temperature (not less than 30 ℃) and normal pressure, which is particularly suitable for treating VOCs waste gas containing a certain amount of low unsaturated hydrocarbon. The method can ignite the VOCs waste gas and burn the waste gas in a self-sustaining manner without external auxiliary heating energy, has simple process and is beneficial to environmental protection.
The invention has the beneficial effects that: the method can ignite the VOCs waste gas containing a certain amount of low unsaturated hydrocarbon without external auxiliary heating energy and realize self-sustaining combustion, does not need to add an ignition device, can be realized at normal temperature, has simple process and is beneficial to environmental protection.
Detailed Description
The present invention will be further described with reference to the following examples. However, the present invention is not limited to these examples. The preparation method of the doped precious metal composite oxide catalyst comprises the following steps:
weighing 43g of cerium nitrate and 27g of zirconyl nitrate to prepare 0.25mol/L aqueous solution, diluting 85g of 25 wt% ammonia water to 5 wt% to be used as a precipitant, placing the precipitant in a three-neck flask, slowly dropping a mixed solution of the cerium nitrate and the zirconyl nitrate until the pH value of the solution is 9-11, continuing stirring for 0.5h after dropping, standing and aging overnight, washing with deionized water, filtering, drying a filter cake at 100 ℃ for 5h, and then performing programmed heating to 900 ℃ for 5h under flowing air to obtain the catalyst aid CZ 1. CZ1 with a specific surface area of 250m2Alumina (Ziboshuren alumina technologies Co., Ltd., model 80150) (in which the weight ratio of CZ1 to alumina is 3:7), a silica sol assistant (Jiangyin softfly chemical industries Co., Ltd., JH-40) (in which the dosage is 3% of the weight of alumina), a binder (in which the dosage is 1.5% of the weight of alumina), an extrusion assistant (in which the dosage is 1% of the weight of alumina), kneading, extruding, molding, drying at 100 ℃ for 3h, and calcining at 450 ℃ for 2h to obtain a catalyst carrier CZ1-Al2O3. Adding CZ1-Al catalyst carrier2O3Impregnating palladium nitrate by an isometric impregnation method to ensure that the Pd content of the catalyst is 0.1 percent, drying after impregnation, and roasting at 450 ℃ for 2 hours to obtain a finished catalyst A (in percentage by weight, the Pd content is 0.1 percent, and the cerium-zirconium solid solution CZ1 accounts for 30 percent)
Example 1
This example illustrates the present invention of a method for treating waste gas containing a quantity of low unsaturated hydrocarbons by catalytic ignition at ambient temperature.
The finished catalyst A was loaded into the reactor at a catalyst loading of 0.02L, accounting for 80% by volume of the fixed bed reactor. When the temperature of a catalyst bed layer in a reactor filled with a doped precious metal composite oxide catalyst is 33 ℃, introducing VOCs (volatile organic compounds) waste gas with the volume flow of 12L/h (the components are shown in table 1) and 1.5L/h of hydrogen into the reactor together, then introducing 20L/h of air to catalyze and ignite the VOCs waste gas, and rapidly heating the temperature of the catalyst bed layer to 450 ℃; and entering a catalytic self-sustaining combustion stage, stopping introducing hydrogen, regulating the volume flow of the VOCs waste gas to 6L/h, introducing air with the volume flow of 75L/h, rapidly increasing the temperature of a catalyst bed layer to about 650 ℃, and developing and continuously burning the VOCs waste gas in a self-sustaining mode.
The operation is carried out for 100h, wherein the content of each component in the tail gas after combustion discharged by the combustion reaction unit is shown in the table 3.
TABLE 1 VOCs exhaust gas composition in percent by volume (% by volume)
Figure BDA0001847383070000051
Figure BDA0001847383070000061
Comparative example 1
Unlike the method described in example 1, the comparative example employed a method in which 6L/h of VOCs waste gas containing a certain amount of low unsaturated hydrocarbons (components shown in table 1) and 75L/h of air were introduced into a reactor containing 0.02L of a commercially available catalytic combustion catalyst (YSs-1A/B type VOCs catalytic combustion catalyst, goodband technologies ltd., zhejiang) and heated to bring the VOCs waste gas to a light-off temperature of about 300 ℃, followed by light-off and catalytic and non-catalytic combustion to oxidize the VOCs waste gas into carbon dioxide and water, which were discharged through the outlet of the reactor.
The content of each component in the tail gas after combustion discharged by the combustion reaction unit after 100 hours of operation is shown in Table 3.
Example 2
This example illustrates a method of treating VOCs exhaust gas containing a quantity of low unsaturated hydrocarbons and hydrogen catalyzed at ambient temperature according to the present invention.
The finished catalyst A was loaded into the reactor at a catalyst loading of 0.02L, accounting for 80% by volume of the fixed bed reactor. When the temperature of a catalyst bed layer in a reactor filled with a doped precious metal composite oxide catalyst is 33 ℃, introducing VOCs waste gas (the components are shown in Table 2) with the volume flow of 12L/h into the reactor, then introducing 20L/h of air to catalyze and ignite the VOCs waste gas, and rapidly heating the temperature of the catalyst bed layer to 450 ℃; and entering a catalytic self-sustaining combustion stage, then regulating the volume flow of the VOCs waste gas to 6L/h, introducing air with the volume flow of 75L/h, rapidly increasing the temperature of a catalyst bed layer to about 650 ℃, and developing and continuously burning the VOCs waste gas in a self-sustaining mode.
The operation is carried out for 100h, wherein the content of each component in the tail gas after combustion discharged by the combustion reaction unit is shown in the table 3.
TABLE 2 VOCs exhaust gas composition in percent by volume (% by volume)
Hydrogen gas 16.99 Propadiene and propyne 0.4
Carbon monoxide 0.04 Isobutane 0.06
Methane 29.96 N-butane 0.11
Ethane (E) 6.17 N-butene 0.35
Ethylene 33.28 Isobutene 0.65
Acetylene 0.51 Trans-2-butene 0.11
Propane 0.5 Cis-2-butene 0.08
Propylene (PA) 9.51 1, 3-butadiene 1.28
Comparative example 2
Unlike the method described in example 2, the comparative example employed a method in which 6L/h of VOCs waste gas (composition shown in table 2) containing a certain amount of low unsaturated hydrocarbons and hydrogen and 75L/h of air were introduced into a reactor containing 0.02L of a commercially available catalytic combustion catalyst (YSs-1A/B VOCs catalytic combustion catalyst, goodband technologies ltd., zhejiang, excellent carbon environmental protection, ltd.), heated to bring the VOCs waste gas to an ignition temperature of about 190 ℃, ignited, and catalytically and non-catalytically combusted to oxidize the VOCs waste gas into carbon dioxide and water to be discharged through the outlet of the reactor.
The content of each component in the tail gas after combustion discharged by the combustion reaction unit after 100 hours of operation is shown in Table 3.
Table 3 percent gas volume content (%)
Methane Ethane (E) Ethylene (CO) process Propylene (PA)
Example 1 0.12 0.01 0 0
Comparative example 1 0.14 0.01 0 0
Example 2 0.11 0.01 0 0
Comparative example 2 0.13 0.01 0 0
When volume calculation is carried out on tail gas content, N is not included2、O2And H2O。
As can be seen from the comparison of the data in Table 3, the method of the present invention, and the noble metal doped composite oxide catalyst, has the same effect of treating VOCs waste gas containing a certain amount of low unsaturated hydrocarbon as the conventional catalytic combustion, and the method of the present invention does not need external heating energy, and is more simple, energy-saving and environment-friendly.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications all fall within the protection scope of the present invention.
It should be noted that the technical features described in the above embodiments can be combined in any suitable manner without contradiction, and various possible combinations of the features are not described in order to avoid unnecessary repetition.

Claims (18)

1. A treatment method for normal-temperature catalytic ignition of VOCs self-sustaining combustion is characterized by comprising the following steps:
in the catalytic ignition stage, at normal temperature and normal pressure, when the temperature of a catalyst bed layer in a reactor filled with the doped precious metal composite oxide catalyst is 30-45 ℃, VOCs waste gas and H are mixed2Introducing into a reactor to remove VOCs waste gas and H2The space velocity of the catalyst is 100-10000 h-1Then introducing air to catalyze and ignite the VOCs waste gas, and rapidly heating the temperature of a catalyst bed layer to 100-500 ℃; entering a catalytic self-sustaining combustion stageSegment, then stopping the introduction of H2Adjusting the feeding flow rate of the VOCs waste gas, adjusting the volume flow rate of the introduced air to be 5-30 times of the volume flow rate of the VOCs, wherein the reaction is developed into a self-sustaining combustion reaction of the VOCs waste gas, and the VOCs waste gas is thoroughly oxidized into carbon dioxide and water and then is discharged through an outlet of the reactor;
in the VOCs waste gas, the content of C1-C4 unsaturated hydrocarbon is 5-100% of the total volume of the VOCs waste gas;
the doped precious metal composite oxide catalyst comprises a precious metal active component, an oxygen storage material cerium-zirconium solid solution and a carrier; the noble metal active component is Pd and/or Pt.
2. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 1, wherein:
in the VOCs waste gas, the content of C1-C4 unsaturated hydrocarbon is 10-60% of the total volume of the VOCs waste gas;
said H2The dosage of the unsaturated hydrocarbon is 0-5 times of the volume of the unsaturated hydrocarbon between C1 and C4 in the VOCs waste gas.
3. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 2, characterized in that:
said H2The dosage of the unsaturated hydrocarbon is 0.1-2 times of the volume of the unsaturated hydrocarbon between C1 and C4 in the VOCs waste gas.
4. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 1, wherein:
in the catalytic ignition stage, the volume flow of the air is 1-15 times of the volume flow of the VOCs;
in the catalytic ignition stage, the airspeed of the doped noble metal composite oxide catalyst is controlled to be 100-10000 h-1。
5. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 4, wherein:
in the catalytic ignition stage, the air speed of the doped noble metal composite oxide catalyst is controlled to be 500-5000 h-1。
6. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 1, wherein:
in the catalytic self-sustaining combustion stage, the volume flow of the introduced air is 10-20 times of the volume flow of VOCs;
in the catalytic self-sustaining combustion stage, the volume space velocity of the doped noble metal composite oxide catalyst is controlled to be 1000-100000 h by adjusting the feed flow of the VOCs waste gas-1。
7. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 6, wherein:
in the catalytic self-sustaining combustion stage, the volume airspeed of the doped noble metal composite oxide catalyst is controlled to be 3000-10000 h by adjusting the feed flow of the VOCs waste gas-1。
8. The treatment method for normal-temperature catalytic ignition of self-sustaining combustion of VOCs according to claim 1, wherein:
the reactor is provided with a flow pipeline; the flow pipeline is arranged inside the reactor or at the periphery of the reactor; cooling water flows through the circulating pipeline;
the method comprises a cooling step;
and the cooling step is to control the temperature of the gas after the combustion reaction to be below 1000 ℃ by adopting cooling water.
9. The method of claim 8, wherein the step of igniting the VOCs by normal temperature catalysis comprises the steps of:
and in the cooling step, cooling water is adopted to control the temperature of the gas after the combustion reaction to be 500-800 ℃.
10. The treatment method for the self-sustained combustion of VOCs by normal-temperature catalysis and ignition according to any one of claims 1 to 9, characterized in that:
the carrier contains Al2O3A carrier;
wherein, the total weight of the catalyst is 100 parts by weight, the content of the noble metal active component is 0.03-5 parts by weight, the content of the oxygen storage material cerium zirconium solid solution is 5-40 parts by weight, and the balance is a carrier.
11. The process of claim 10, wherein the step of igniting the VOCs by normal temperature catalysis comprises the steps of:
the catalyst comprises, by weight, 100 parts of the total weight of the catalyst, 0.05-3 parts of a noble metal active component, 10-30 parts of an oxygen storage material cerium zirconium solid solution, and the balance of a carrier.
12. The process of claim 10, wherein the step of igniting the VOCs by normal temperature catalysis comprises the steps of:
the Al is2O3The specific surface of the carrier is 100-300 m2/g；
The oxygen storage material cerium-zirconium solid solution is formed by performing a solid phase reaction at a high temperature of 500-1200 ℃ with a cerium-zirconium molar ratio (Ce/Zr) of 0.5-3.
13. The process of claim 12, wherein the step of igniting the VOCs by normal temperature catalysis comprises the steps of: the oxygen storage material cerium zirconium solid solution is prepared by the following steps:
weighing cerium salt and zirconium salt according to the molar ratio of cerium to zirconium, and dissolving the cerium salt and the zirconium salt in water to prepare a mixed solution with the total solute concentration of 0.1-5 mol/L; dropping the mixed solution into a precipitator under vigorous stirring until the pH value of the reaction solution is 9-11, continuing stirring after dropping, standing, washing, filtering, drying a filter cake, and then performing temperature programming to 500-1200 ℃ under flowing air for roasting to prepare the cerium-zirconium solid solution;
the precipitator is selected from 0.1-10 wt% ammonia water;
the cerium salt is selected from cerium nitrate, cerium sulfate and cerium acetate;
the zirconium salt is selected from zirconyl nitrate, zirconium oxychloride, or zirconium tetrachloride.
14. The process of claim 13, wherein the step of catalyzing the ignition of the self-sustaining combustion of VOCs comprises:
weighing cerium salt and zirconium salt according to the molar ratio of cerium to zirconium, and dissolving the cerium salt and the zirconium salt in water to prepare a mixed solution with the total solute concentration of 0.2-2 mol/L.
15. The process of claim 13, wherein the step of catalyzing the ignition of the self-sustaining combustion of VOCs comprises:
and (3) carrying out roasting by temperature programming to 700-900 ℃ under flowing air.
16. The process of claim 13, wherein the step of catalyzing the ignition of the self-sustaining combustion of VOCs comprises:
the precipitator is selected from ammonia water with the concentration of 1-5 wt%.
17. The processing method for normal-temperature catalytic ignition of self-sustained combustion of VOCs according to claim 10, wherein the doped precious metal composite oxide catalyst is prepared by a wet forming method;
the wet forming method comprises the following steps:
mixing oxygen storage material cerium zirconium solid solution, auxiliary agent and Al2O3And kneading and extruding the carrier and a forming assistant for forming, drying at 80-120 ℃, roasting at 250-600 ℃ to prepare the catalyst carrier, impregnating the catalyst carrier with the required noble metal active component, drying at 80-120 ℃, and roasting at 250-600 ℃.
18. The process of claim 17, wherein the step of catalyzing and igniting the self-sustaining combustion of VOCs comprises:
the auxiliary agent is selected from sol; the sol is selected from titanium sol, silica sol and water glassAt least one of silane; the dosage of the auxiliary agent is Al2O31-5% of the weight of the carrier.
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JP2002370014A (en) * 2001-06-13 2002-12-24 Babcock Hitachi Kk Exhaust gas treatment system
CN104138756A (en) * 2014-08-02 2014-11-12 孙超 Supported catalyzer for low-temperature catalytic combustion of VOCs and method for preparing supported catalyzer for low-temperature catalytic combustion of VOCs
CN107970921A (en) * 2016-10-21 2018-05-01 中国石油化工股份有限公司 A kind of catalyst with catalysis organic exhaust gas combustion function and its preparation method and application and the method for catalysis organic exhaust gas burning
CN106732521B (en) * 2016-12-02 2020-01-10 复旦大学 Preparation method of high-performance cerium-zirconium solid solution material
CN108325526B (en) * 2018-03-06 2020-07-31 西南化工研究设计院有限公司 Broad-spectrum VOCs catalytic combustion monolithic catalyst and preparation method and application thereof

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