A device and method for treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor

Abstract

The present invention discloses a device and method for treating volatile organic compounds (VOCs) by coupling a catalytic oxidation process with a molecular sieve rotor. The device includes a molecular sieve rotor comprising an adsorption zone, a catalytic oxidation zone, and a cooling zone. The method employs adsorption purification and catalytic oxidation to efficiently degrade VOCs, while also allowing for the regeneration and recycling of the molecular sieve adsorbent. The device occupies a small footprint and enables continuous treatment of VOCs. The method is simple and easy to operate, achieving a VOC conversion rate of ≥47.53% and, under optimal conditions, ≥100%.

Description

Technical Field

[0001] The present invention belongs to the technical field of volatile organic compound treatment, and in particular relates to a device and method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. Background Art

[0002] Volatile organic compounds (VOCs) are the primary precursors to secondary pollutants such as PM2.5 and O3. Most VOCs are toxic and pose a significant threat to human health. High VOC concentrations can easily cause acute poisoning, ranging from mild symptoms such as headaches, dizziness, coughing, nausea, vomiting, or a state of intoxication to severe liver poisoning and even coma, which can be life-threatening.

[0003] CN110639330A discloses a system and method for treating gases containing volatile organic compounds and preparing carbon nanomaterials. The system includes a gas adsorption / desorption subsystem, a gas-liquid separation subsystem, and an exhaust gas carbonization subsystem. The method uses the system to treat gases containing volatile organic compounds and prepare carbon nanomaterials. The method involves adsorbing the volatile organic compound gas through the gas adsorption / desorption subsystem, and the gas exiting the gas adsorption / desorption subsystem meets emission standards. The organic matter desorbed by the gas adsorption / desorption subsystem is condensed through a gas-liquid separation subsystem to obtain a liquid that is collected, reused, or reprocessed. The exhaust gas exiting the gas-liquid separation subsystem enters the exhaust gas carbonization subsystem, where carbon nanomaterials are generated at high temperature. The exhaust gas is then combined with the exhaust gas from the gas adsorption / desorption subsystem and discharged in compliance with emission standards. However, adsorption treatment cannot fundamentally eliminate pollutants. Once saturated, the adsorbent needs to be regenerated or replaced, and adsorbent regeneration inevitably causes secondary pollution.

[0004] CN107469550A discloses a VOCs treatment method that integrates condensation and adsorption. This method involves passing oil and gas through a cold box for condensation and liquefaction. The liquefied organic matter enters a gas-liquid separator tank, where the non-condensable gas is sent to the adsorption system. The adsorbed and desorbed gas enters the gas-liquid separator tank. The low-temperature liquid organic matter in the separator tank is pressurized by a return pump and sent to the cooling pipe of the adsorption tank. The liquid organic matter that leaves the cooling pipe is then sent to a storage tank. However, the equipment used in this treatment method occupies a large area, and the liquid organic matter requires further processing.

[0005] CN110953599A provides a VOCs waste gas catalytic combustion system and method, which includes a first heat exchanger, a dust removal device, an ozone supply device, a mixing device, a second heat exchanger, a catalytic combustion device, and an exhaust gas absorption device. After the VOCs waste gas flows through the first heat exchanger and the dust removal device in sequence, it is mixed with ozone generated by the ozone supply device in the mixing device, then flows through the second heat exchanger, and then enters the catalytic combustion device for catalytic combustion. The exhaust gas after catalytic combustion flows through the second heat exchanger and finally flows into the exhaust gas absorption device. However, this method uses precious metals as catalysts, which is costly; it needs to be carried out in a high-temperature environment, which poses safety risks and is prone to catalyst deactivation; and the low concentration of organic waste gas requires external heat to maintain combustion.

[0006] Therefore, there is an urgent need to develop a method for treating volatile organic compounds that can achieve efficient degradation of volatile organic compounds, does not require subsequent secondary treatment, and has a simple process and is easy to operate. Summary of the Invention

[0007] In view of the problems existing in the prior art, the object of the present invention is to provide a device and method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The device for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor integrates adsorption, catalytic oxidation and adsorbent regeneration in the rotor, occupies a small area, and can achieve continuous treatment; the method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor can achieve efficient degradation of volatile organic compounds, does not require subsequent secondary treatment, and has a simple process and is easy to operate.

[0008] To achieve this object, the present invention adopts the following technical solutions:

[0009] In a first aspect, the present invention provides a device for treating volatile organic compounds by coupling catalytic oxidation with a molecular sieve rotor. The device comprises a molecular sieve rotor, and the molecular sieve rotor comprises an adsorption zone, a catalytic oxidation zone, and a cooling zone.

[0010] The adsorption zone, catalytic oxidation zone and cooling zone in the device for treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor provided by the present invention concentrate adsorption, catalytic oxidation and adsorbent regeneration in one molecular sieve rotor, occupying a small area. Through the continuous rotation of the rotor, the regeneration and recycling of the molecular sieve adsorbent is realized, and volatile organic compounds can be continuously treated.

[0011] Preferably, a first air inlet duct and a first air outlet duct are provided in the adsorption zone.

[0012] Preferably, a second air inlet duct, a third air inlet duct and a second air outlet duct are provided in the catalytic oxidation zone.

[0013] Preferably, the device further comprises an oxidant generating device connected to the second air inlet duct.

[0014] Preferably, the oxidant generating device comprises an ultraviolet component or a dielectric barrier discharge device.

[0015] Preferably, the device further comprises a heating device connected to the second air inlet duct.

[0016] Preferably, the device further comprises a cooling device arranged at a corresponding position of the cooling zone.

[0017] Preferably, the cooling device is arranged outside the cooling zone.

[0018] Preferably, the area of the adsorption zone accounts for 40-60% of the area of the molecular sieve rotor, for example, it can be 40%, 43%, 45%, 47%, 50%, 55% or 60%.

[0019] Preferably, the area of the catalytic oxidation zone accounts for 20-40% of the area of the molecular sieve wheel, for example, it can be 20%, 22%, 25%, 27%, 30%, 35% or 40%.

[0020] Preferably, the area of the cooling zone accounts for 20% of the area of the molecular sieve wheel.

[0021] In the present invention, the area of the adsorption zone is larger than that of the catalytic oxidation zone and the cooling zone, which has the advantages of reducing the rotation frequency of the wheel and lowering energy consumption.

[0022] Preferably, the device further comprises a housing, and a bracket is provided inside the housing.

[0023] Preferably, the molecular sieve rotor is arranged on the bracket.

[0024] Preferably, the device further comprises a power drive device connected to the molecular sieve rotor.

[0025] Preferably, the power drive device includes a motor and a chain drive component connected to the motor.

[0026] Preferably, the chain drive component is arranged on the outside of the molecular sieve rotor.

[0027] Preferably, the power drive device further includes a speed control device connected to the motor.

[0028] In a second aspect, the present invention provides a method for treating volatile organic compounds using a catalytic oxidation coupled molecular sieve rotor, wherein the method is performed using the catalytic oxidation coupled molecular sieve rotor device described in the first aspect.

[0029] The method for treating volatile organic compounds by coupling catalytic oxidation with a molecular sieve rotor provided by the present invention utilizes adsorption and catalytic oxidation to couple the treatment of volatile organic compounds. Compared with treating volatile organic compounds with a molecular sieve rotor alone, the oxidant can degrade the volatile organic compounds into carbon dioxide and water without the need for secondary treatment. Compared with treating volatile organic compounds with oxidation alone, the combined treatment with the coupled molecular sieve rotor can improve the removal efficiency of volatile organic compounds, and the adsorbent in the molecular sieve rotor can be regenerated and recycled, greatly reducing treatment costs.

[0030] Preferably, the method comprises the following steps:

[0031] (1) Volatile organic matter enters the adsorption zone, is adsorbed and purified by the adsorbent in the adsorption zone, and the gas after adsorption and purification is discharged;

[0032] (2) rotating the molecular sieve rotor to rotate the adsorbent in the adsorption zone of step (1) to the catalytic oxidation zone, where the volatile organic compounds enter the catalytic oxidation zone, are catalytically oxidized by the heated oxidant, and the generated gas is discharged;

[0033] (3) rotating the molecular sieve rotor to move the adsorbent after catalytic oxidation in step (2) to a cooling zone for cooling to obtain a regenerated adsorbent;

[0034] Repeat steps (1) to (3) to treat volatile organic compounds.

[0035] In the present invention, the volatile organic compounds pass through the adsorption zone, the catalytic oxidation zone and the cooling zone in sequence, which not only realizes the efficient degradation of the volatile organic compounds, but also realizes the regeneration and recycling of the molecular sieve adsorbent.

[0036] Preferably, the volatile organic compounds in step (1) enter the adsorption zone through the first air inlet duct.

[0037] Preferably, the gas purified by adsorption is discharged through a first gas outlet pipe.

[0038] Preferably, the adsorption zone, catalytic oxidation zone and cooling zone are all filled with molecular sieve adsorbents loaded with active substances.

[0039] Preferably, the preparation method of the active substance-loaded adsorbent comprises the following steps:

[0040] The active substance acetate was dissolved in deionized water, stirred until completely dissolved, BETA molecular sieves were added, and magnetic stirring was performed for 8 hours; after rotary evaporation at 80°C, it was dried in a 100°C oven for 12 hours, and finally calcined in a muffle furnace at 500°C for 3 hours.

[0041] Preferably, the active substance acetate includes any one or a combination of at least two of manganese acetate, cerium acetate or nickel acetate, wherein typical but non-limiting combinations are a combination of manganese acetate and cerium acetate, a combination of manganese acetate and nickel acetate, a combination of cerium acetate and nickel acetate, or a combination of manganese acetate, cerium acetate and nickel acetate.

[0042] Preferably, the active material comprises any one or a combination of at least two of manganese oxide, cerium oxide or nickel oxide, wherein typical but non-limiting combinations are a combination of manganese oxide and cerium oxide, a combination of manganese oxide and nickel oxide, a combination of cerium oxide and nickel oxide, or a combination of manganese oxide, cerium oxide and nickel oxide.

[0043] Preferably, the active material loading on the molecular sieve adsorbent is 0.3-20%, for example, 0.3%, 0.5%, 1%, 3%, 5%, 10%, 15%, 18% or 20%.

[0044] Preferably, the molecular sieve adsorbent comprises BETA molecular sieve.

[0045] The present invention adopts BETA molecular sieve with good hydrophobicity and high selectivity for adsorption, which can reduce the adsorption of water in volatile organic compounds by the molecular sieve and extend the service life of the adsorbent, and can selectively adsorb volatile organic compounds and improve the removal efficiency of volatile organic compounds.

[0046] Preferably, the volatile organic compounds in step (2) enter the catalytic oxidation zone through the third air inlet pipe.

[0047] Preferably, the oxidant in step (2) includes ozone.

[0048] In the present invention, ozone is used as an oxidant. Since ozone can significantly reduce the apparent activation energy of volatile organic compound oxidation more than oxygen, volatile organic compounds can be efficiently decomposed into carbon dioxide and water.

[0049] Preferably, the ozone is produced by treating oxygen with an ultraviolet component or a dielectric barrier discharge device.

[0050] Preferably, the ozone is heated by a heating device.

[0051] Preferably, the heating temperature is 60-170°C, for example, 60°C, 70°C, 80°C, 100°C, 120°C, 140°C, 150°C or 170°C.

[0052] The present invention requires that ozone heated to 60-170° C. be introduced into the catalytic oxidation zone because ozone catalytic oxidation efficiency is high within this temperature range and the removal effect on volatile organic compounds is good.

[0053] Preferably, the heated ozone enters the catalytic oxidation zone through the second air inlet pipe.

[0054] Preferably, the ozone concentration is 1000-10000 ppm, for example, 1000 ppm, 2000 ppm, 3000 ppm, 5000 ppm, 7000 ppm, 9000 ppm or 10000 ppm.

[0055] In the present invention, the concentration of ozone is controlled within the range of 1000 to 10000 ppm, which can achieve efficient purification of organic matter and avoid excess ozone residue.

[0056] Preferably, the gas after catalytic oxidation is discharged through a second gas outlet pipe.

[0057] In the present invention, the gas after catalytic oxidation still has a relatively high temperature and can be circulated back to the catalytic oxidation zone for waste heat reuse, thereby achieving the purpose of energy saving.

[0058] Preferably, the cooling zone is cooled by a heat exchange device.

[0059] Preferably, the cooling is to 20-30°C, for example, 20°C, 21°C, 23°C, 25°C, 27°C, 29°C or 30°C.

[0060] The present invention cools the molecular sieve heated by the hot ozone gas introduced into the catalytic oxidation zone, so that the molecular sieve adsorbent can be regenerated and can continue to adsorb after being rotated to the adsorption zone.

[0061] As a preferred technical solution of the present invention, the method comprises the following steps:

[0062] (1) Volatile organic matter enters the adsorption zone through the first air inlet pipe, and is adsorbed and purified by the BETA molecular sieve adsorbent with an active material loading of 0.3 to 20% in the adsorption zone, and the gas after adsorption and purification is discharged through the first air outlet pipe;

[0063] (2) rotating the molecular sieve wheel to rotate the adsorbent in the adsorption zone of step (1) to the catalytic oxidation zone, and the volatile organic matter enters the catalytic oxidation zone through the third air inlet pipe, and is treated by the ultraviolet component or the dielectric barrier discharge device to produce 1000-10000 ppm of ozone, which is heated to 60-170° C. by the heating device, and enters the catalytic oxidation zone through the second air inlet pipe to catalytically oxidize the volatile organic matter, and the generated gas is discharged through the second air outlet pipe;

[0064] (3) rotating the molecular sieve rotor to move the adsorbent after catalytic oxidation in step (2) to a cooling zone and cooling it to 20-30° C. via a heat exchange device to obtain a regenerated adsorbent;

[0065] Repeat steps (1) to (3) to treat volatile organic compounds.

[0066] The numerical range described in the present invention includes not only the point values listed above, but also any point values between the above numerical ranges that are not listed. Due to space limitations and for the sake of simplicity, the present invention no longer exhaustively lists the specific point values included in the range.

[0067] Compared with the prior art, the present invention has the following beneficial effects:

[0068] (1) The device for treating volatile organic compounds by coupling catalytic oxidation with a molecular sieve rotor provided by the present invention integrates adsorption, catalytic oxidation, and adsorbent regeneration into the rotor, occupies a small area, and can achieve continuous treatment of volatile organic compounds;

[0069] (2) The method of treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor provided by the present invention can achieve efficient degradation of volatile organic compounds without the need for secondary treatment. The process is simple and easy to operate. The volatile organic compound conversion rate is ≥47.53%. Under optimal conditions, the volatile organic compound conversion rate is ≥100%. BRIEF DESCRIPTION OF THE DRAWINGS

[0070] Figure 1 Schematic diagram of the device for treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor provided in Example 1 of the present invention.

[0071] In the figure: 1-molecular sieve rotor; 2-adsorption zone; 3-catalytic oxidation zone; 4-cooling zone; 5-first air inlet pipe; 6-third air inlet pipe; 7-first air outlet pipe; 8-second air inlet pipe; 9-second air outlet pipe. DETAILED DESCRIPTION

[0072] The present invention is further described in detail below. However, the following examples are merely simplified examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be subject to the claims.

[0073] 1. Implementation

[0074] Example 1

[0075] This embodiment provides a device for treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor. The schematic diagram of the device is shown in FIG. Figure 1 As shown, the device includes a molecular sieve rotor 1, which includes an adsorption zone 2, a catalytic oxidation zone 3, and a cooling zone 4. The area of the adsorption zone 2 accounts for 50% of the area of the molecular sieve rotor 1; the area of the catalytic oxidation zone 3 accounts for 30% of the area of the molecular sieve rotor 1; and the area of the cooling zone 4 accounts for 20% of the area of the molecular sieve rotor 1.

[0076] The device further includes a heating device connected to the second air inlet pipe 8, an ozone generator connected to the second air inlet pipe 8, and a cooling device arranged at a corresponding position outside the cooling zone 4; the ozone generator includes a dielectric barrier discharge device.

[0077] The adsorption zone 2 is provided with a first air inlet pipe 5 and a first air outlet pipe 7 ; the catalytic oxidation zone 3 is provided with a second air inlet pipe 8 , a third air inlet pipe 6 and a second air outlet pipe 9 .

[0078] The device further comprises a housing with a support provided therein, and the molecular sieve rotor 1 is arranged on the support; the device further comprises a motor connected to the molecular sieve rotor 1 and a chain drive component and a speed control device connected to the motor.

[0079] In Examples 2 to 7, the ratio of the adsorption zone area to the molecular sieve rotor area was changed to 40%, 43%, 45%, 47%, 55%, and 60%, the cooling zone area to the molecular sieve rotor area was 20%, and the catalytic oxidation zone area to the remaining area. The exhaust gas concentration was 200 mg / m 3 , total air volume is 100000Nm 3 / h, the adsorption capacity of Beta molecular sieve is 1.10mmol / g (toluene), and the load capacity of the rotor is 1000kg. The maximum adsorption capacity of the entire rotor is 101200g (toluene). The results of the maximum adsorption capacity and adsorption saturation time of the molecular sieve rotor are shown in Table 1.

[0080] Table 1

[0081] Area ratio of adsorption zone (%) Maximum adsorption capacity (g) Adsorption saturation time (h) Example 1 50 50600 2.5 Example 2 40 40480 2.0 Example 3 43 43516 2.2 Example 4 45 45540 2.3 Example 5 47 47564 2.4 Example 6 55 55660 2.8 Example 7 60 60720 3.0

[0082] As shown in Table 1, as the adsorption zone area continues to increase, the maximum adsorption capacity also increases, and the time to adsorption saturation also increases accordingly, which helps save VOC treatment costs. However, adsorption treatment cannot fundamentally eliminate pollutants and must be coupled with catalytic oxidation technology to achieve efficient degradation and removal of VOCs.

[0083] Comparative Example 1

[0084] This comparative example provides a device for treating volatile organic compounds using a molecular sieve wheel. The device replaces the catalytic oxidation zone in Example 1 with a heating zone, connects the heating device to the third air inlet pipe, and deletes the second air inlet pipe connected to the catalytic oxidation zone and the ozone generator connected to the second air inlet pipe.

[0085] 2. Application Examples

[0086] Application Example 1

[0087] This application example provides a method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The method is performed using the device for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided in Example 1, and includes the following steps:

[0088] (1) 100 ppm toluene gas enters the adsorption zone through the first air inlet pipe at a flow rate of 200 mL / min, and is adsorbed and purified by a BETA molecular sieve adsorbent with an average pore size of 0.61 nm and a manganese dioxide loading of 1% in the adsorption zone. The adsorbed and purified gas is discharged through the first air outlet pipe;

[0089] (2) After 240 minutes, the molecular sieve wheel is rotated to rotate the adsorbent in the adsorption zone of step (1) to the catalytic oxidation zone. The volatile organic compounds enter the catalytic oxidation zone through the third air inlet pipe, and are irradiated by an ultraviolet lamp with a wavelength of 185 nm to generate 800 ppm of ozone. The ozone is heated to 170° C. by an electric heating device and enters the catalytic oxidation zone through the second air inlet pipe at a flow rate of 200 mL / min to catalytically oxidize the volatile organic compounds. The generated gas is discharged through the second air outlet pipe;

[0090] (3) After 240 minutes, the molecular sieve rotor is rotated to move the adsorbent after catalytic oxidation in step (2) to a cooling zone and cooled to 30° C. via a heat exchange device to obtain a regenerated adsorbent;

[0091] Repeat steps (1) to (3) to treat the toluene gas.

[0092] Application Example 2

[0093] This application example provides a method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The method is performed using the apparatus for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided in Example 1. The method is the same as that in Application Example 1, except that the molecular sieve loaded with manganese dioxide is replaced with a molecular sieve loaded with nickel oxide.

[0094] Application Example 3

[0095] This application example provides a method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The method is performed using the apparatus for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided in Example 1. The method is the same as that in Application Example 1, except that the molecular sieve loaded with manganese dioxide is replaced with a molecular sieve loaded with cerium oxide.

[0096] Application Example 4

[0097] This application example provides a method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The method is performed using the device for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided in Example 1. The method is the same as that in Application Example 1 except that toluene gas is replaced by propane.

[0098] Application Example 5

[0099] This comparative example provides a method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The method is carried out using the device for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided in Example 1. Except for heating the ozone entering the catalytic oxidation zone to 30°C, the rest of the method is the same as that in Application Example 1.

[0100] Application Example 6

[0101] This comparative example provides a method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor. The method is carried out using the device for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided in Example 1. Except for heating the ozone entering the catalytic oxidation zone to 210°C, the rest of the method is the same as that in Application Example 1.

[0102] Comparative Application Example 1

[0103] This comparative example provides a method for treating volatile organic compounds with a molecular sieve rotor. The method is performed using the device for treating volatile organic compounds with a molecular sieve rotor provided in comparative example 1, and the rest is the same as in application example 1.

[0104] The method for treating volatile organic compounds using a molecular sieve rotor provided in this comparative example only desorbs toluene and does not degrade it, so a secondary treatment is required later.

[0105] 3. Test and Results

[0106] The concentrations of volatile organic compounds (VOCs) and the catalytic oxidation degradation products, carbon dioxide and carbon monoxide, were measured at different temperatures at the outlet of the second gas outlet pipe in Examples 1 to 6. The concentration of the VOCs was measured by gas chromatography, and the concentrations of carbon dioxide and carbon monoxide were measured by infrared spectroscopy. The VOC conversion rate was calculated based on the change in VOC concentration before and after the reaction. The CO2 yield was calculated by comparing the generated CO2 concentration to the equivalent value, and the CO yield was calculated by comparing the generated CO2 concentration to the equivalent value.

[0107] Table 2 shows the results of Application Example 1.

[0108] Table 2

[0109] Temperature (℃) Toluene conversion rate (%) <![CDATA[CO2 production rate (%)]]> CO production rate (%) 63 83.7 48.1 20.0 84 87.9 52.4 22.7 126 80.4 48.9 22.1 168 70.4 45.3 18.9

[0110] Table 3 shows the results of Application Example 2.

[0111] Table 3

[0112]

[0113]

[0114] Table 4 shows the results of Application Example 3.

[0115] Table 4

[0116] Temperature (℃) Toluene conversion rate (%) <![CDATA[CO2 production rate (%)]]> CO production rate (%) 62 80.5 22.0 11.7 84 83.6 40.5 18.8 127 89.7 59.0 21.7 169 75.2 50.3 18.1

[0117] Table 5 shows the results of Application Example 4.

[0118] Table 5

[0119] Temperature (℃) Propane conversion rate (%) <![CDATA[CO2 production rate (%)]]> CO production rate (%) 62 97.64 95.6 14.5 84 100.00 83.6 13.5 126 96.81 78.9 13.5 168 47.53 52.1 3.4

[0120] Table 6 shows the results of Application Example 5.

[0121] Table 6

[0122] Temperature (℃) Toluene conversion rate (%) <![CDATA[CO2 production rate (%)]]> CO production rate (%) 30 62.5 14.9 5.8

[0123] Table 7 shows the results of Application Example 6.

[0124] Table 7

[0125] Temperature (℃) Toluene conversion rate (%) <![CDATA[CO2 production rate (%)]]> CO production rate (%) 63 83.7 48.1 20.0 84 87.9 52.4 22.7 126 80.4 48.9 22.1 168 70.4 45.3 18.9 209 54.8 40.4 13.9

[0126] From the comprehensive application examples 1 to 4, it can be seen that the method of treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided by the present invention can achieve efficient removal of volatile organic compounds, with a toluene conversion rate of ≥70.4%. Under optimal conditions, the toluene conversion rate is ≥95.8%, and the propane conversion rate is ≥47.53%. Under optimal conditions, the propane conversion rate is ≥100%. Moreover, when the method is used to treat volatile organic compounds, the conversion rate first increases and then decreases with the increase of the treatment temperature. Among them, when using a molecular sieve loaded with manganese dioxide to treat toluene in application example 1, at a relatively low temperature of 84°C, the toluene conversion rate reaches a maximum of 87.9%, the CO2 yield is 52.4%, and the CO yield is 22.7%. When using a molecular sieve loaded with manganese dioxide to treat propane in application example 4, at a relatively low temperature of 84°C, the propane conversion rate is as high as 100%, without the need for secondary treatment.

[0127] From Application Example 1 and Application Examples 5 to 6, it can be seen that in Application Example 1, the ozone entering the catalytic oxidation zone is heated to 170°C, but the toluene conversion rate reaches a maximum of 87.9% at 84°C, the CO2 yield is 52.4%, and the CO yield is 22.7%. In Application Example 5, the ozone entering the catalytic oxidation zone is heated to 30°C, the toluene conversion rate is only 62.5%, the CO2 yield is only 14.9%, and the CO yield is only 5.8%. In Application Example 6, the ozone entering the catalytic oxidation zone is heated to 210°C, but the toluene conversion rate is only 54.8% at 209°C, still reaching a maximum at 84°C. The temperature increase does not improve the conversion rate, but instead causes energy waste. This shows that the present invention further controls the heating of the oxidant entering the catalytic oxidation zone to a temperature within the range of 60 to 170°C, which not only achieves efficient catalytic degradation and conversion of volatile organic compounds, but also reduces energy consumption and saves costs.

[0128] In summary, the method for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor provided by the present invention can achieve efficient degradation of volatile organic compounds without the need for secondary treatment, and has low treatment energy consumption, thereby saving costs.

[0129] The applicant declares that the above is only a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Those skilled in the art should understand that any changes or substitutions that can be easily thought of by those skilled in the art within the technical scope disclosed by the present invention fall within the scope of protection and disclosure of the present invention.

Claims

1. A device for treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor, characterized in that: The device includes a molecular sieve rotor, which includes an adsorption zone, a catalytic oxidation zone and a cooling zone; The adsorption zone is provided with a first air inlet pipe and a first air outlet pipe; The catalytic oxidation zone is provided with a second air inlet pipe, a third air inlet pipe and a second air outlet pipe; The device also includes an oxidant generating device connected to the second air inlet pipe; The device also includes a heating device connected to the second air inlet duct; The device also includes a cooling device arranged at a corresponding position of the cooling zone; The catalytic oxidation zone utilizes a heated oxidant to catalytically oxidize volatile organic compounds, and the oxidant includes ozone, which is heated to 60-170° C. by a heating device; The adsorption zone, catalytic oxidation zone and cooling zone are all filled with molecular sieve adsorbent loaded with active substances.

2. The device according to claim 1, characterized in that The oxidant generating device includes an ultraviolet component or a dielectric barrier discharge device.

3. The device according to claim 1, characterized in that The cooling device is arranged outside the cooling zone.

4. The device according to claim 1, characterized in that The area of the adsorption zone accounts for 40-60% of the area of the molecular sieve rotor.

5. The device according to claim 1, characterized in that The area of the catalytic oxidation zone accounts for 20-40% of the area of the molecular sieve rotor.

6. The device according to claim 1, characterized in that The area of the cooling zone accounts for 20% of the area of the molecular sieve wheel.

7. The device according to claim 1, characterized in that The device further comprises a shell, wherein a bracket is provided inside the shell.

8. The device according to claim 7, characterized in that The molecular sieve rotor is arranged on the bracket.

9. The device according to claim 1, characterized in that The device also includes a power drive device connected to the molecular sieve rotor.

10. The device according to claim 9, characterized in that The power drive device includes a motor and a chain drive component connected to the motor.

11. The device according to claim 10, characterized in that The chain driving component is arranged on the outside of the molecular sieve rotor.

12. The device according to claim 9, characterized in that The power drive device also includes a speed control device connected to the motor.

13. A method for treating volatile organic compounds by catalytic oxidation coupled with a molecular sieve rotor, characterized in that: The method is carried out using the device for treating volatile organic compounds by using a catalytic oxidation coupled molecular sieve rotor as described in any one of claims 1 to 12.

14. The method according to claim 13, characterized in that The method comprises the following steps: (1) Volatile organic matter enters the adsorption zone, is adsorbed and purified by the adsorbent in the adsorption zone, and the gas after adsorption and purification is discharged; (2) rotating the molecular sieve rotor to rotate the adsorbent in the adsorption zone of step (1) to the catalytic oxidation zone, where the volatile organic compounds enter the catalytic oxidation zone, are catalytically oxidized by the heated oxidant, and the generated gas is discharged; (3) rotating the molecular sieve rotor to move the adsorbent after catalytic oxidation in step (2) to a cooling zone for cooling to obtain a regenerated adsorbent; Repeat steps (1) to (3) to treat volatile organic compounds.

15. The method according to claim 14, characterized in that The volatile organic compounds in step (1) enter the adsorption zone through the first air inlet duct.

16. The method according to claim 14, characterized in that The gas purified by adsorption is discharged through the first gas outlet pipe.

17. The method according to claim 14, characterized in that The adsorption zone, catalytic oxidation zone and cooling zone are all filled with molecular sieve adsorbent loaded with active substances.

18. The method according to claim 17, characterized in that The active material includes any one of manganese oxide, cerium oxide or nickel oxide, or a combination of at least two of them.

19. The method according to claim 17, wherein The active material loading amount on the molecular sieve adsorbent is 0.3-20%.

20. The method according to claim 17, wherein The molecular sieve adsorbent includes BETA molecular sieve.

21. The method according to claim 14, wherein The volatile organic compounds in step (2) enter the catalytic oxidation zone through the third air inlet pipe.

22. The method according to claim 14, wherein The oxidant in step (2) includes ozone.

23. The method according to claim 22, characterized in that The ozone is produced by treating oxygen with an ultraviolet component or a dielectric barrier discharge device.

24. The method according to claim 22, characterized in that The ozone is heated by a heating device.

25. The method according to claim 24, characterized in that The heating temperature is 60-170°C.

26. The method according to claim 24, characterized in that The heated ozone enters the catalytic oxidation zone through the second air inlet pipe.

27. The method according to claim 26, characterized in that The ozone concentration is 1000-10000 ppm.

28. The method according to claim 26, characterized in that The gas after catalytic oxidation is discharged through the second gas outlet pipe.

29. The method according to claim 14, wherein The cooling zone is cooled by heat exchange equipment.

30. The method according to claim 29, wherein The cooling temperature is 20-30°C.

31. The method according to any one of claims 13 to 30, characterized in that The method comprises the following steps: (1) Volatile organic matter enters the adsorption zone through the first air inlet pipe, and is adsorbed and purified by the BETA molecular sieve adsorbent with an active material loading of 0.3 to 20% in the adsorption zone, and the gas after adsorption and purification is discharged through the first air outlet pipe; (2) rotating the molecular sieve wheel to rotate the adsorbent in the adsorption zone of step (1) to the catalytic oxidation zone, and the volatile organic matter enters the catalytic oxidation zone through the third air inlet pipe, and is treated by the ultraviolet component or the dielectric barrier discharge device to produce 1000-10000 ppm of ozone, which is heated to 60-170° C. by the heating device, and enters the catalytic oxidation zone through the second air inlet pipe to catalytically oxidize the volatile organic matter, and the generated gas is discharged through the second air outlet pipe; (3) rotating the molecular sieve rotor to move the adsorbent after catalytic oxidation in step (2) to a cooling zone and cooling it to 20-30° C. via a heat exchange device to obtain a regenerated adsorbent; Repeat steps (1) to (3) to treat volatile organic compounds.

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