Purification system for treating volatile organic compounds

Abstract

The application discloses a purification system for treating volatile organic compounds, and belongs to the field of volatile organic compound treatment. The purification system for treating volatile organic compounds comprises a pretreatment filtering device for dust and oil removal of VOCs waste gas; an adsorption runner comprising a cylindrical zeolite molecular sieve module for adsorption concentration of the pretreated volatile organic compound waste gas; and a catalytic combustion reactor for combustion removal treatment of the adsorption concentrated volatile organic compound waste gas from the adsorption runner. The adsorption runner comprises a shell, a waste gas inlet and an outlet, a ceramic heat exchanger and a runner device are arranged in the shell and communicate with each other, the ceramic heat exchanger communicates with the waste gas inlet, the runner device communicates with the outlet, the runner device comprises a plurality of columns, and at least one layer of molecular sieve module for adsorbing volatile organic compounds in waste gas is arranged between adjacent columns in the plurality of columns.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of volatile organic compounds treatment, and particularly relates to a purification system for treating volatile organic compounds. BACKGROUND

[0002] With the rapid development of chemical industry and the increasing energy consumption, volatile organic compounds (VOCs) generated in petrochemical, electroplating, printing and dyeing industries as precursors and participants of PM2.5 and O3 have multiple environmental effects on the atmosphere, which seriously endanger human health. Industrial sources are the main sources of volatile organic compounds, and their significant features are high emission intensity, high concentration, multiple types of pollutants and long duration, which have a great impact on regional atmospheric environment. At present, the treatment of volatile organic compounds has become a key and difficult point in the prevention and control of air pollution in China.

[0003] The conventional treatment methods such as absorption, condensation and membrane separation have low removal efficiency of volatile organic compounds, which cannot meet the current emission control requirements. The existing zeolite molecular sieve adsorption roller has low concentration ratio, large floor area, and the zeolite is easy to be damaged and difficult to be replaced, and the operation and maintenance cost is high. Most of the catalytic combustion reactors on the market are unstable, have low purification efficiency and are easy to produce secondary pollution. SUMMARY

[0004] In order to solve at least one of the above problems and defects in the prior art, the present application provides a purification system for treating volatile organic compounds. The pretreatment, adsorption concentration and catalytic combustion are combined to form a new purification system for treating volatile organic compounds, which realizes the improvement of technical equipment and the optimization and perfection of process, and effectively solves the performance defects and secondary pollution problems of the prior art.

[0005] An object of the present application is to provide a purification system for treating volatile organic compounds.

[0006] According to one aspect of the present application, there is provided a purification system for treating volatile organic compounds, comprising:

[0007] a pretreatment filtering device for dust removal and oil removal of volatile organic compound waste gas;

[0008] an adsorption roller comprising a cylindrical zeolite molecular sieve module for adsorption concentration of the pretreated volatile organic compound waste gas,

[0009] a catalytic combustion reactor for combustion removal treatment of the adsorbed and concentrated volatile organic compound waste gas from the adsorption roller,

[0010] The adsorption runner comprises a shell, a waste gas inlet and an outlet, a ceramic heat exchanger and a runner device are arranged in the shell and communicate with each other, the ceramic heat exchanger communicates with the waste gas inlet, the runner device communicates with the outlet, the runner device comprises a plurality of columns, at least one layer of molecular sieve module for adsorbing volatile organic compounds in waste gas is arranged between adjacent columns in the plurality of columns.

[0011] Further, the runner device further comprises a driving device, a slewing bearing, a bottom disc and a top disc, the plurality of columns are fixed between the bottom disc and the top disc and are arranged in the circumferential direction of the bottom disc, the slewing bearing is drivingly connected with the bottom disc, and the driving device is connected with the slewing bearing.

[0012] Specifically, the ceramic heat exchanger and the runner device further communicate through a heat exchange pipeline, a first end of the heat exchange pipeline is connected with the ceramic heat exchanger, and a second end of the heat exchange pipeline is inserted into an inner cavity of the runner device, and the runner device comprises an adsorption zone and a desorption zone.

[0013] Specifically, a port outer edge of the second end of the heat exchange pipeline is provided with a sliding rail, the top disc and the bottom disc are in the shape of a circular ring, and a flange in sliding connection with the sliding rail is arranged at an inner surface of the top disc and the bottom disc.

[0014] A part of the heat exchange medium flowing through the at least one layer of molecular sieve module constitutes the desorption zone.

[0015] Further, the outlet comprises an adsorption zone outlet for discharging clean gas obtained after the volatile organic compounds are adsorbed and a desorption zone outlet for discharging gas after desorption,

[0016] The ceramic heat exchanger comprises a first outlet for discharging waste gas after heat exchange and a second outlet for discharging heat exchange medium after heat exchange with waste gas, the first outlet communicates with the adsorption zone, and the second outlet is connected with the heat exchange pipeline.

[0017] Specifically, one end of the adsorption zone outlet is arranged in the inner cavity of the runner device, and the other end extends outward along the longitudinal direction of the runner device to the outside of the shell,

[0018] One end of the desorption zone outlet is arranged in the desorption zone, and the other end extends along the longitudinal direction of the adsorption runner to the outside of the shell,

[0019] The adsorption zone accounts for three fourths of all the molecular sieve modules in the at least one layer of molecular sieve module, and the desorption zone accounts for one fourth of all the molecular sieve modules in the at least one layer of molecular sieve module.

[0020] Further, an axial flow fan for extracting the heat exchange medium in the ceramic heat exchanger to the desorption area and a heater for heating the heat exchange medium are arranged in the heat exchange pipeline, the axial flow fan is arranged close to the ceramic heat exchanger, and the heater is arranged close to the second gas outlet.

[0021] Specifically, the at least one layer of molecular sieve module includes an inner layer of molecular sieve module and an outer layer of molecular sieve module, and the inner layer of molecular sieve module and the outer layer of molecular sieve module are arranged along the radial direction of the base disc.

[0022] Specifically, a moving push rod device for replacing the at least one layer of molecular sieve module and a sensor for measuring the concentration of volatile organic compounds are further arranged in the inner cavity, and the sensor is in signal connection with the moving push rod device.

[0023] Preferably, the column is a rotating column, which drives the inner layer of molecular sieve module and the outer layer of molecular sieve module on one side to rotate.

[0024] Further, the pretreatment filtering device includes coarse efficiency filter cotton and medium efficiency filter cloth bag, the coarse efficiency filter cotton is arranged on a stainless steel mesh frame, and the medium efficiency filter cloth bag is arranged at the rear end of the coarse efficiency filter cotton.

[0025] Further, the catalytic reactor includes a preheating chamber and a catalytic combustion chamber, the preheating chamber is connected with the air inlet of the catalytic reactor, and after desorption, the volatile organic compound waste gas after adsorption and concentration enters the preheating chamber to exchange heat with the heat exchange medium in the heat conducting pipe.

[0026] The catalytic combustion chamber is provided with a catalyst reaction bed, and the waste gas after preheating is combusted on the catalyst reaction bed to generate high-temperature flue gas.

[0027] Specifically, part of the high-temperature flue gas is directly discharged into the atmosphere, and the other part of the high-temperature flue gas flows into the desorption area of the adsorption wheel as a heat exchange medium.

[0028] Specifically, the cylindrical zeolite molecular sieve module is a 13X molecular sieve module, and the 13X molecular sieve is prepared by the following method, which includes the following steps:

[0029] A fly ash raw material is provided, and the mass percentage of the fly ash ranges from 66% to 85%;

[0030] The fly ash raw material is mixed and ground with sodium hydroxide, a silicon source, an aluminum source, 13X molecular sieve seeds, and a hard template to obtain a mixture, the silicon-aluminum ratio in the mixture ranges from 3 to 11, the mass percentage of the 13X molecular sieve seeds ranges from 8% to 15%, and the mass percentage of the hard template ranges from 2% to 5%.

[0031] crystallizing the mixture at a temperature in the range of 80-98 DEG C for 15-24 hours to obtain a crystallized product, and cooling the crystallized product to obtain a primary product;

[0032] calcining the primary product at a temperature in the range of 500-600 DEG C for 4-8 hours to obtain a calcined product, and then sequentially cooling, washing and filtering the calcined product, and then drying at a temperature in the range of 50-70 DEG C for 10-15 hours to obtain the 13X molecular sieve.

[0033] Specifically, the mass percentage of the sodium hydroxide is 5-15%.

[0034] Preferably, the mass percentage of the silicon source and / or the aluminum source is 0-15%.

[0035] Further, the silicon source includes any one or combination of sodium silicate, silica gel or white carbon black.

[0036] Further, the aluminum source includes any one or combination of pseudo-boehmite, sodium metaaluminate or aluminum hydroxide.

[0037] Further, the hard film plate includes any one or combination of carbon black, carbon nanotube or porous carbon.

[0038] Specifically, the 13X molecular sieve is a microporous-mesoporous 13X molecular sieve structure.

[0039] Further, the particle size of the mixture is less than or equal to 74 microns, and the washing water is deionized water.

[0040] Further, the fly ash is a circulating fluidized bed fly ash.

[0041] The grinding is performed in air.

[0042] The step of providing the fly ash raw material includes: removing iron from the fly ash by magnetic separation, and then washing, filtering and drying to obtain.

[0043] The purification system for treating volatile organic compounds according to the present application has at least one of the following advantages:

[0044] (1) The adsorption wheel of the purification system provided by the present application has the characteristics of compact design, simple structure, small footprint, self-operation through waste heat recovery maintaining device, high energy utilization efficiency, etc.

[0045] (2) The adsorption wheel of the purification system provided by the present application has the advantages of modular assembly, easy replacement, convenient transportation, small specific heat capacity, less heat absorption, high concentration ratio, high adsorption efficiency, stable operation and low energy consumption.

[0046] (3) The design of the multi-layer molecular sieve module in the adsorption runner of the purification system improves the adsorption efficiency of volatile organic compounds;

[0047] (4) The design of the heat exchange pipeline in the adsorption runner of the purification system improves the efficiency of desorption of the molecular sieve module using recovered heat;

[0048] (5) The use of a moving push rod device in combination with a concentration sensor in the adsorption runner of the purification system can realize automatic replacement of the molecular sieve module, avoiding the danger of manual replacement of the molecular sieve module in high temperature;

[0049] (6) The 13X molecular sieve of the purification system does not need a calcination activation link for the preparation of molecular sieve from circulating fluidized bed fly ash;

[0050] (7) The 13X molecular sieve of the purification system is prepared without using a solution, has high molecular sieve yield, high utilization rate of the crystallization kettle, low synthesis pressure, and small environmental pollution;

[0051] (8) The 13X molecular sieve of the purification system has a micropore-mesopore structure, which greatly improves the mass transfer efficiency;

[0052] (9) The 13X molecular sieve of the purification system is simple to make, low in cost, and small in pollution, and has good popularization advantages.

[0053] (10) The preparation method of the 13X molecular sieve of the purification system and the 13X molecular sieve are prepared using bulk solid waste fly ash as raw material, which not only improves the value-added utilization rate of bulk solid waste and expands the comprehensive utilization way of solid waste, but also effectively reduces the preparation cost, achieving the effect of "turning waste into treasure". BRIEF DESCRIPTION OF DRAWINGS

[0054] These and / or other aspects and advantages of the present application will become apparent and readily understood from the following description, taken in connection with the accompanying drawings, in which:

[0055] Figure 1 is a structural schematic diagram of an adsorption runner according to an embodiment of the present application;

[0056] Figure 2 is Figure 1 a structural schematic diagram of the runner device shown in FIG. 1;

[0057] Figure 3 is a purification system for treating volatile organic compounds according to an embodiment of the present application.

[0058] Figure 4is a flow chart of a preparation method of 13X molecular sieve according to an embodiment of the present application;

[0059] Figure 5 is an XRD characterization result chart of 13X molecular sieve obtained in Example 1;

[0060] Figure 6 is Figure 5 is a low magnification (5000 times) scanning electron microscope chart of 13X molecular sieve shown in Figure 1;

[0061] Figure 7 is Figure 5 is a high magnification (80000 times) scanning electron microscope chart of 13X molecular sieve shown in Figure 2;

[0062] Figure 8 is a scanning electron microscope chart of 13X molecular sieve obtained in Example 2;

[0063] Figure 9 is a scanning electron microscope chart of 13X molecular sieve obtained in Example 3;

[0064] Figure 10 is a scanning electron microscope chart of 13X molecular sieve obtained in Example 4;

[0065] Figure 11 is a scanning electron microscope chart of 13X molecular sieve in Example 5 at 80000 times;

[0066] Figure 12 is Figure 11 is a scanning electron microscope chart of 13X molecular sieve at 20000 times.

[0067] Wherein, 100 is an adsorption wheel, 10 is a shell, 11 is a waste gas inlet, 12 is a first gas outlet, 13 is a second gas outlet, 14 is a ceramic heat exchanger, 15 is a heat exchange pipeline, 15' is a second heat exchange pipeline, 16 is an adsorption area gas outlet, 17 is a desorption area gas outlet, 18 is an axial flow fan, 19 is a heater, 20 is a wheel device, 21 is a stand, 22 is an inner layer molecular sieve module, 23 is an outer layer molecular sieve module, 24 is a top disc, 25 is a bottom disc, 26 is a slewing bearing, 200 is a pretreatment filtering device, 210 is a pretreatment gas inlet, 220 is a coarse efficiency filter cotton, 230 is a medium efficiency filter bag, 240 is a shell, 300 is a catalytic combustion reactor, 310 is a hot air gas outlet, 311 is a waste gas recovery outlet, 312 is a catalytic reactor gas inlet, 313 is a heat conducting pipe, 314 is a air supplement pipe, 315 is a frequency conversion fan, 316 is a preheating chamber, 317 is a catalyst reaction bed, 318 is an electric heating pipe. DETAILED DESCRIPTION

[0068] The technical solution of the present invention will be further described in detail below through embodiments and in conjunction with the accompanying drawings. In this specification, the same or similar reference numerals indicate the same or similar components. The following description of the embodiments of the present invention with reference to the accompanying drawings is intended to explain the overall inventive concept of the present invention and should not be construed as a limitation thereof.

[0069] like Figures 1-3 As shown, a purification system for treating volatile organic compounds (VOCs) according to an embodiment of the present invention includes a cylindrical zeolite molecular sieve adsorption rotor (or simply adsorption rotor) 100, a pretreatment filter 200 located upstream of the adsorption rotor, and a catalytic combustion reactor 300 located downstream of the adsorption rotor 100. The purification system for treating volatile organic compounds specifically comprises... Figure 3 The detailed description shows that the purification system adopts a three-stage coupling process, which organically combines the pretreatment, adsorption concentration and catalytic combustion of volatile organic compounds. By improving and optimizing their structure and perfecting the process, the purification efficiency of volatile organic compounds is significantly improved. The purification system has the advantages of simple structure, modular assembly of zeolite molecular sieves, convenient operation, small footprint, low energy consumption, long service life and no secondary pollution.

[0070] The specific treatment process is roughly as follows: the waste gas containing volatile organic compounds first enters the pretreatment filter device 200 for dust and oil removal, and then passes through the cylindrical zeolite molecular sieve adsorption rotor 100 for adsorption and concentration. The clean gas purified by the cylindrical zeolite molecular sieve adsorption rotor is directly discharged into the atmosphere. The concentrated waste gas containing volatile organic compounds then enters the catalytic combustion reactor 300 for catalytic combustion treatment. The qualified gas after catalytic combustion is directly discharged into the atmosphere.

[0071] The following sections will detail the structure of the adsorption rotor 100, the pretreatment filter 200, and the catalytic combustion reactor 300, as well as the corresponding waste gas treatment processes.

[0072] like Figure 1As shown, the adsorption wheel 100 provided by the present application comprises a housing 10, a waste gas inlet 11, a first gas outlet 12, a second gas outlet 13, a ceramic heat exchanger 14 and a wheel device 20. The ceramic heat exchanger 14 and the wheel device 20 are arranged in the housing 10. The waste gas inlet 11 is arranged on the side of the housing 10 close to the ceramic heat exchanger 14 and communicates with the ceramic heat exchanger 14. The first gas outlet 12 and the second gas outlet 13 are two gas outlets of the ceramic heat exchanger, and the first gas outlet 12 communicates with the wheel device 20. In use, waste gas with a temperature as high as 80-200°C enters the ceramic heat exchanger 14 from the waste gas inlet 11 and exchanges heat therein. The waste gas after heat exchange has a temperature of 30-60°C and enters the wheel device 20 through the first gas outlet 12. Since the optimal adsorption temperature of the molecular sieve (to be described below) is between 20-60°C, the waste gas after heat exchange is just within the optimal adsorption temperature range of the molecular sieve, thereby improving the adsorption efficiency of the molecular sieve and also realizing waste heat recovery. Specifically, the housing 10 is a sealed housing, and the ceramic heat exchanger 14 is made of silicon carbide material.

[0073] In combination Figure 1 and Figure 2 As shown, in one example, the wheel device 20 comprises a plurality of columns 21, inner layer molecular sieve modules 22, outer layer molecular sieve modules 23, a top disc 24, a bottom disc 25, a slewing bearing 26 and a driving device (not shown). The plurality of columns 21 are arranged at intervals between the top disc 24 and the bottom disc 25, and the plurality of columns 21 are arranged along the circumferential direction of the bottom disc 25, so that the plurality of columns 21, the top disc 24 and the bottom disc 25 form a cylindrical wheel around each other. The driving device drives the slewing bearing 26 to rotate, thereby driving the cylindrical wheel arranged on the slewing bearing 26 to rotate. In one example, the rotation speed of the wheel device 20 is 2-4 revolutions per hour.

[0074] In one example, in order to improve the adsorption efficiency of the molecular sieve in the wheel device to volatile organic compounds (i.e. VOCs) in the waste gas, two layers of molecular sieve modules, i.e. the inner layer molecular sieve modules 22 and the outer layer molecular sieve modules 23, are filled between two columns 21 adjacent to each other. It should be understood by those skilled in the art that 1 layer, 3 layers or more layers of molecular sieve modules can also be filled. In another example, the inner layer molecular sieve modules 22 and the outer layer molecular sieve modules 23 can also be designed into an upper and lower two-layer mode as needed. Those skilled in the art can select the number of layers of molecular sieve modules according to actual needs.

[0075] In one example, the molecular sieve module can adopt any type of existing molecular sieve, and the shape of the molecular sieve module is determined according to the shape between two adjacent columns. The number of columns and the size of the rotary device can be set according to the air volume of the actual treated exhaust gas, for example, the rotary device can be divided into multiple partitions as needed, such as 18 partitions, 20 partitions, 24 partitions, etc. Those skilled in the art can also divide it into other numbers of partitions as needed. In one example, the number of molecular sieve modules filled is determined by the distance between the columns adjacent to each other.

[0076] In one example, the column 21 is designed as a rotary column. The driving device also drives the rotary column to rotate. The rotary column drives the inner layer molecular sieve module 22 and the outer layer molecular sieve module 23 on one side thereof to rotate, that is, the rotary column drives the inner layer molecular sieve module and the outer layer molecular sieve module on the same side in the clockwise direction of the rotation of the rotary device or in the counterclockwise direction of the rotation of the rotary device to rotate simultaneously. It can also be said that the inner layer molecular sieve module 22 and the outer layer molecular sieve module 23 on the left side of the rotary column rotate simultaneously or the inner layer molecular sieve module 22 and the outer layer molecular sieve module 23 on the right side of the rotary column rotate simultaneously. Those skilled in the art can design the rotary column to drive the inner layer molecular sieve module and the outer layer molecular sieve module on both sides to rotate simultaneously as needed, at which time two inner layer molecular sieve modules and two outer layer molecular sieve modules need to be filled between adjacent columns. Those skilled in the art can make a selection as needed.

[0077] In one example, the rotary column can be designed as a multi-layer rotary column. The design of each layer of the rotary column, as well as the structure and principle of the design of the corresponding inner and outer layer molecular sieve modules, are exactly the same as the design of the column 21 and the structure and principle of the design of the corresponding inner layer molecular sieve module 22 and outer layer molecular sieve module 23, and will not be repeated here.

[0078] In one example, the rotary column can be designed in the adsorption zone and / or the desorption zone. The distance between two adjacent layers of rotary columns is at least the distance between adjacent rotary columns, for example, it can also be 2 times the distance between adjacent rotary columns. Those skilled in the art can make corresponding design and adjustment according to the actual design of the inner layer molecular sieve module and the outer layer molecular sieve module and the column. This example is only an illustrative example, and those skilled in the art should not understand it as a limitation of the present application.

[0079] In one example, the rotating column can be designed to rotate at the same speed as the rotating wheel device 20, for example, 2-4 rotations per hour. It can also be designed to rotate at a different speed than the rotating wheel device 20, for example, 12 rotations per hour, 1 rotation per hour. Those skilled in the art can make corresponding designs according to the air volume, the saturation of the molecular sieve module adsorbing volatile organic compounds, and the like. For example, as the amount of volatile organic compounds adsorbed in the molecular sieve module gradually increases, the signal of the concentration of volatile organic compounds in the molecular sieve module can be transmitted to the control module (not shown), and the control module can transmit the signal of the reduced speed to the driving device, thereby gradually reducing the speed of the rotating column. Those skilled in the art can make corresponding adjustments according to actual needs.

[0080] In one example, the top disc 24 and the bottom disc 25 are designed in the shape of a ring. The heat exchange pipe 15 is further provided between the ceramic heat exchanger 14 and the rotating wheel device 20. The first end of the heat exchange pipe 15 is connected to the second air outlet 13, and the second end is inserted into the inner cavity of the rotating wheel device 20. The outer edge of the port of the second end of the heat exchange pipe 15 is provided with a sliding rail (not shown), and the inner surface of the top disc 24 and the bottom disc 25 is respectively provided with a flange (not shown) that is slidably connected to the sliding rail along the circumferential direction of the top disc 24 and the bottom disc 25, i.e., the sliding rail on the upper side of the outer edge of the port of the second end of the heat exchange pipe 15 is slidably connected to the flange of the top disc 24, and similarly, the sliding rail on the lower side of the outer edge of the port of the second end of the heat exchange pipe 15 is slidably connected to the flange of the bottom disc 25. In this way, when the rotating wheel device 20 rotates at high speed, the heat exchange pipe 15 will not rotate simultaneously with the rotating wheel device 20, thereby realizing that the position of the heat exchange pipe 15 in the rotating wheel device 20 is fixed.

[0081] Those skilled in the art can know that, according to the actual application of the rotating wheel device, the sliding rail can also be designed on the inner surface and / or outer surface of the top disc 24, and / or the sliding rail can also be designed on the inner surface and / or outer surface of the bottom disc 25. Correspondingly, the flange can be designed on the heat exchange pipe 15. Those skilled in the art can make corresponding selection according to needs, as long as the heat exchange pipe 15 can be slidably connected to the top disc 24 and the bottom disc 25.

[0082] In one example, the heat exchange pipe 15 is provided with an axial flow fan 18, a heater 19 (for example, an electric heating sleeve), and a temperature sensor (not shown). The axial flow fan 18 is arranged close to the ceramic heat exchanger 14, and the heater 19 is arranged close to the second air outlet 13.

[0083] The axial flow fan 18 draws the heat-exchanged heat-exchange medium from the ceramic heat exchanger 14, at which time the temperature sensor senses the temperature of the heat-exchanged medium in the heat-exchange pipeline 15. When the temperature sensor senses that the temperature of the heat-exchanged medium is low, for example, lower than 200°C, the temperature sensor transmits a signal to the electric heating jacket, at which time the electric heating jacket is activated and starts to heat the heat-exchanged medium in the heat-exchange pipeline 15. When the temperature is as high as 200°C to 300°C, the temperature sensor transmits a signal to the electric heating jacket, at which time the electric heating jacket stops heating. The heat-exchanged medium in the heat-exchange pipeline 15 is then delivered to the desorption zone, thereby realizing the self-running process of the rotary adsorption-desorption. Those skilled in the art can understand that the heater can also be designed as other heating devices or components, as long as it can realize the heating of the heat-exchanged medium.

[0084] In one example, the heat-exchanged medium in the second end of the heat-exchange pipeline 15, together with the portion of the inner layer molecular sieve module 22 corresponding to the second end of the heat-exchange pipeline 15 and the portion of the outer layer molecular sieve module 23, constitutes the desorption zone, and the rest is the adsorption zone. In use, the rotary device 20 rotates, at which time the molecular sieve module corresponding to the second end of the heat-exchange pipeline is located in the desorption zone, at which time the molecular sieve module performs the desorption process. With the rotation of the rotary device 20, the plurality of molecular sieve modules in turn leave the desorption zone and enter the adsorption zone, and each molecular sieve module performs the cyclic adsorption process on the waste gas. In one example, the wind speed in the adsorption zone and the desorption zone is lower than 4 meters / second.

[0085] In one example, the adsorption rotary device is also designed with an adsorption zone gas outlet 16 and a desorption zone gas outlet 17. The adsorption zone gas outlet 17 extends upward from the inner cavity of the rotary device 20 in the longitudinal direction thereof to the outside of the shell 10. The desorption zone gas outlet 17 discharges the desorbed gas in the desorption zone from the adsorption rotary device 100, and extends in the longitudinal direction of the adsorption rotary device 100 to the outside of the shell 10. In use, when the volatile organic compound waste gas enters the adsorption zone, the molecular sieve module adsorbs and concentrates the volatile organic compound components in the waste gas, and the obtained clean gas is discharged from the adsorption zone gas outlet 16 at the center position of the rotary device 20, and is desorbed by the heat-exchanged medium when the molecular sieve module rotates to the desorption zone, thereby achieving the concentration effect. The heat-exchanged medium in the desorption zone is then discharged from the desorption zone gas outlet 17 to the subsequent catalytic fluidized bed or catalyst reaction bed for concentrated treatment.

[0086] In one example, the adsorption zone accounts for three quarters of all the molecular sieve modules in the at least one layer of molecular sieve modules, and the desorption zone accounts for one quarter of all the molecular sieve modules in the at least one layer of molecular sieve modules. Those skilled in the art can understand that the size of the adsorption zone and the desorption zone can be adjusted accordingly according to actual needs, for example, the adsorption zone accounts for two thirds, and the desorption zone accounts for one third, etc. In one example, a heat preservation plate (not shown) for heat preservation is arranged in the desorption zone. For example, it can be arranged on the inner wall of the port at the other end of the heat exchange pipeline.

[0087] In one example, a moving push rod device (not shown) and a concentration sensor (not shown) are arranged in the inner cavity of the rotating device. The probe of the concentration sensor is arranged towards the molecular sieve module in the adsorption zone. After being used for a period of time according to the actual operating conditions, the concentration sensor senses that the volatile organic compound concentration in the clean gas in the inner cavity is higher than 10 mg / m 3 When the molecular sieve module has reached the state of adsorption saturation, the concentration sensor transmits a signal to the moving push rod device (i.e. signal connection), and the moving push rod device pushes the inner layer molecular sieve module to the outer side position and places the new molecular sieve module conveyed into the inner cavity to the inner side position, so as to achieve automatic replacement of the molecular sieve module.

[0088] Referring to Figure 3 , the pretreatment filtering device 200 includes a pretreatment air inlet 210, a coarse filter cotton 220 and a medium filter bag 230. The coarse filter cotton 220 is arranged on a stainless steel mesh frame (not shown), and the medium filter bag 230 is arranged at the rear end of the coarse filter cotton 220. Both the coarse filter cotton 220 and the medium filter bag 230 are arranged in a shell 240. It can be understood that whether the medium filter bag 230 is arranged in series to further remove oil and dust can be determined according to the dust content of the volatile organic compound waste gas and the dust removal requirement. The coarse filter cotton 220 is used to filter out impurities with a particle size greater than 10 microns, and the medium filter bag is used to filter out impurities with a particle size of 0-10 microns.

[0089] Specifically, for example, high concentration of volatile organic waste gas enters the pretreatment filter device 200 through the pretreatment inlet 210, and sequentially passes through the coarse filter cotton 220 and the medium filter cloth bag 230 to be treated for dust removal and oil removal, forming the volatile organic waste gas after pretreatment filtration. At this time, the waste gas with a temperature as high as 80-200℃ enters the ceramic heat exchanger 14 from the waste gas inlet 11 and exchanges heat here. The temperature of the waste gas after heat exchange is reduced to 30-60℃, and the waste gas enters the rotary device 20 through the first gas outlet 12. When the volatile organic waste gas enters the adsorption zone, the molecular sieve modules 22 and 23 adsorb and concentrate the volatile organic components in the waste gas, and the clean gas obtained is discharged from the adsorption zone gas outlet 16 at the center of the rotary device 20. When the molecular sieve module rotates to the desorption zone, the desorption is carried out by the heat exchange medium (heat exchange gas or waste gas, the heat exchange gas in the ceramic heat exchanger 14 can be clean air or waste gas treated by the purification system of the present application) from the ceramic heat exchanger 14 and / or the catalyst reaction bed 317, so as to achieve the effect of desorption and concentration. After that, the heat exchange medium in the desorption zone is discharged from the desorption zone gas outlet 17 to the subsequent catalytic reactor for catalytic combustion treatment.

[0090] The catalytic reactor 300 comprises a hot air outlet 310, a waste gas recovery outlet 311, a catalytic reactor inlet (or concentrated waste gas inlet) 312, a heat conducting pipe 313, a supplementary air pipe 314, a variable frequency fan 315, a catalyst reaction bed 317, and an electric heating pipe 318.

[0091] The desorption zone gas outlet 17 is connected to the catalytic reactor inlet 312 of the catalytic reactor, and the catalytic reactor inlet 312 is in communication with the preheating chamber 316 comprising the heat conducting pipe 313. The volatile organic waste gas after adsorption and concentration (i.e. the heat exchange medium from the desorption zone) enters the preheating chamber 316, and then exchanges heat with the high-temperature flue gas (from the catalyst reaction bed 317, which will be described in detail below) in the heat conducting pipe 313 to be preheated. The preheated waste gas is combusted on the catalyst reaction bed 317 to generate high-temperature flue gas, which then passes through the heat conducting pipe 313. Under the action of the variable frequency fan 315 in the chimney, a part of the high-temperature flue gas that meets the standard is directly discharged through the hot air outlet 310, and another part of the high-temperature flue gas is introduced into the desorption zone of the adsorption rotary device 100 through the second heat exchange pipe 15’. As shown in Figure 3 The space in the preheating chamber 316 is divided into three areas by two partition walls, and the waste gas entering from the catalytic reactor inlet 312 finally enters the catalyst reaction bed 317 through a winding path. The winding path is arranged to achieve sufficient preheating, and the specific arrangement is not limited to Figure 3The catalytic combustion exhaust gas (i.e. high temperature flue gas) is returned to the leftmost compartment of the preheating chamber 316 through the heat conducting pipe 313, and the upper end of the compartment is connected to the catalytic reactor inlet 312.

[0092] In one example, a portion of the high temperature flue gas is directly discharged into the chimney and finally discharged into the atmosphere, and another portion of the high temperature flue gas is used as a heat exchange medium and flows into the desorption zone of the adsorption wheel 100 through the recovered exhaust gas outlet 311. It can be understood that because the ceramic heat exchanger 14 is arranged in the adsorption wheel 100, the heat exchange medium in the ceramic heat exchanger 14 can achieve the desorption of volatile organic compounds in the desorption zone, so it can be selected whether to also use a portion of the high temperature flue gas as a heat exchange medium for desorbing volatile organic compounds. Of course, both the gas from the ceramic heat exchanger 14 and the catalytic reaction bed 317 can be used as a heat exchange medium or heat exchange gas at the same time.

[0093] In the catalytic reactor 300, the electric heating pipe 318 is used to heat the catalytic reaction bed 317 to achieve catalytic combustion. The variable frequency fan 315 is used to discharge the catalytic combustion exhaust gas that meets the standard into the atmosphere through the hot air outlet 310. One end of the air supplement pipe 314 is arranged outside the chimney, the other end penetrates the chimney along the radial direction of the chimney, and is communicated with the preheating chamber 316. The air supplement pipe 314 is used to supplement the atmosphere to the exhaust gas to be discharged into the hot air outlet 310 and the recovered exhaust gas outlet 311 to reduce their temperature to the desired value. The recovered exhaust gas outlet 311 is arranged on the chimney and located on the upper side of the air supplement port.

[0094] In another embodiment of the present application, the cylindrical zeolite molecular sieve module is a module made of 13X molecular sieve, which can be made of white mud produced in the process of extracting aluminum from fly ash by acid method, or can be prepared by the following method. The above-mentioned method is used to prepare the 13X molecular sieve into a modular design, which has low preparation cost, realizes energy saving and environmental protection effect, develops a new way for high value-added utilization of fly ash, is easy to replace, convenient to transport, has small specific heat capacity, small heat absorption, high concentration ratio, high purification efficiency, stable operation, low energy consumption, no secondary pollution, etc.

[0095] The specific steps of the acid method for extracting aluminum are as follows:

[0096] Any one or mixture of fly ash, coal gangue and diatomite solid waste is crushed, sieved and dried to obtain raw materials. The raw materials are leached with hydrochloric acid to obtain aluminum-rich liquid and aluminum extraction residue. The aluminum extraction residue is dissolved with sodium hydroxide to obtain silicon-rich liquid and residual material. Then, the silicon-rich liquid and the aluminum-rich liquid are crystallized and molded by microwave heating to obtain a type of 13X molecular sieve product, which has the advantages of high production efficiency, low energy consumption, low cost, no secondary pollution, etc.

[0097] First, solid waste rich in silicon and aluminum such as fly ash, coal gangue or diatomite is obtained, and the SiO2 and Al2O3 contents in the fly ash, coal gangue or diatomite are determined.

[0098] According to the mass ratio of SiO2 to Al2O3 being (2-8):1, an appropriate amount of any one or a mixture of more than one of the solid waste of fly ash, coal gangue or diatomite is taken as raw material, dried at 70-90°C for 10-14 hours, and then crushed and sieved through a 200-mesh sieve to obtain undersize material, i.e. coarse material, with a particle size of less than or equal to 74 mm.

[0099] The coarse material is added to an acid leaching tank, and an appropriate amount of hydrochloric acid is added according to the mass ratio of coarse material to inorganic acid being 1:(2-4) to perform acid leaching on the coarse material for 2-4 hours to obtain an acid leaching product, which is filtered to obtain an aluminum-rich liquid and an aluminum extraction residue.

[0100] The aluminum extraction residue is added to an alkali melting tank, and an appropriate amount of water and sodium hydroxide is added according to the mass ratio of aluminum extraction residue to water to sodium hydroxide being 1:(5-10):(0.2-0.8) to perform alkali melting on the aluminum extraction residue to obtain an alkali melting product, which is filtered to obtain a silicon-rich liquid and a remaining residue.

[0101] The silicon-rich liquid and the aluminum-rich liquid are mixed uniformly according to the mass ratio being (10-60):1, and are crystallized and formed by microwave heating, with the crystallization and formation temperature being selected to be 80-95°C and the crystallization and formation time being 10-14 hours, to obtain a 13X molecular sieve product.

[0102] The mass ratio of raw material SiO2 to Al2O3 is regulated to ensure high purity and crystallinity of the 13X molecular sieve product, the microwave magnetization effect increases the specific surface area of the molecular sieve, and the pore distribution is regular and uniform. This provides a new approach for high-value utilization of fly ash, coal gangue and diatomite solid waste, improves resource utilization efficiency, and achieves energy saving and emission reduction effect.

[0103] In addition, the 13X molecular sieve can also be made by grinding fly ash directly in air using sodium hydroxide, seed crystals, etc. without using a solution.

[0104] Specifically, as shown in Figure 4 the preparation method of the 13X molecular sieve includes the following steps:

[0105] (1) The circulating fluidized bed fly ash is removed of impurities by magnetic separation, washed, filtered and dried to obtain fly ash raw material;

[0106] (2) The fly ash raw material is mixed with sodium hydroxide, a silicon source, an aluminum source, 13X molecular sieve seed crystals and a hard template, and then ground to obtain a mixture;

[0107] (3) The mixture is crystallized in the range of 80 to 98°C for 15 to 24 hours to obtain a crystallized product. After cooling the crystallized product, the initial product of 13X molecular sieve is obtained.

[0108] (4) The initial product is calcined at a temperature range of 500-600℃ for 4-8 hours to obtain the calcined product. After the calcined product is cooled, it is washed and filtered. Then it is dried at a temperature range of 50-70℃ for 10-15 hours to obtain 13X molecular sieve.

[0109] like Figure 5 As shown, the 13X molecular sieve preparation method provided by the present invention has high crystallinity during the preparation process, and the obtained product has high purity and can be clearly seen as a typical 13X type structure.

[0110] In one example, step (1) involves the preparation of fly ash raw materials. The mass percentage of fly ash raw materials in the circulating fluidized bed fly ash used ranges from 66% to 85%, and the fly ash raw materials are circulating fluidized bed fly ash. Deionized water is used for washing to remove unburned carbon and soluble salts from the fly ash. After filtration, the fly ash is dried in an oven at 90°C to 120°C for 5 to 8 hours, preferably at 110°C for 6 hours.

[0111] In one example, step (2) is the preparation of a mixture, the particle size of which should be less than or equal to 74 μm. In the resulting mixture, the mass percentage of sodium hydroxide is 5% to 15%. The silicon-to-aluminum ratio is in the range of 3 to 11, the mass percentage of 13X molecular sieve seed crystals is 8% to 15%, the mass percentage of hard template is 2% to 5%, and the mixed fly ash raw material, sodium hydroxide, silicon source, aluminum source, 13X molecular sieve seed crystals and hard template are ground in air with a mortar for 10 to 15 minutes without any solution.

[0112] In one example, the silicon source includes any one or a combination of sodium silicate, silica gel, or precipitated silica. That is, the silicon source can be any one of sodium silicate, silica gel, and precipitated silica; it can also be a combination of sodium silicate and silica gel, a combination of silica gel and precipitated silica, a combination of sodium silicate and precipitated silica, or a combination of sodium silicate, silica gel, and precipitated silica. The requirement is that the mass percentage of the silicon source is within the range of 0-15%. Those skilled in the art can make appropriate selections according to actual needs.

[0113] In one example, the aluminum source includes any one or combination of pseudoboehmite, sodium aluminate or aluminum hydroxide. In other words, the aluminum source can be any one of pseudoboehmite, sodium aluminate and aluminum hydroxide; or a combination of pseudoboehmite and sodium aluminate, pseudoboehmite and aluminum hydroxide, sodium aluminate and aluminum hydroxide, or a combination of pseudoboehmite, sodium aluminate and aluminum hydroxide. As long as the silicon-aluminum ratio in the mixture is ensured to be in the range of 3-11 after the addition of the compound or composition, the corresponding selection can be made by those skilled in the art as needed.

[0114] In one example, the hard template includes any one or combination of carbon black, carbon nanotube and porous carbon. In other words, the hard template can be any one of carbon black, carbon nanotube and porous carbon; or a combination of carbon black and carbon nanotube, carbon black and porous carbon, carbon nanotube and porous carbon, or a combination of carbon black, carbon nanotube and porous carbon. The corresponding selection can be made by those skilled in the art as needed. As long as the 13X molecular sieve has meso-micropore, the selection can be made.

[0115] In one example, step (4) is the preparation of the 13X molecular sieve. The calcined product of the 13X molecular sieve is washed with deionized water and filtered, so that the hard template is removed. Then, the product is dried in an oven, and the drying temperature is preferably 60°C, and the drying time is preferably 12 hours, so that the 13X molecular sieve with meso-micropore structure is obtained.

[0116] The preparation method of the 13X molecular sieve and the 13X molecular sieve obtained by the preparation method will be described in the following examples.

[0117] Example 1

[0118] In this example, a certain amount of circulating fluidized bed fly ash with a certain silicon-aluminum ratio is first subjected to magnetic separation to remove iron. Then, deionized water is added to wash and remove floating substances in the fly ash, and the fly ash is filtered to remove soluble salts. Then, the fly ash raw material is obtained by drying the fly ash in an oven at 110°C for 6 hours. Then, the fly ash raw material, sodium hydroxide, sodium aluminate, aluminum hydroxide, seed crystal and hard template are mixed in a ratio of 70%, 10%, 7%, 2%, 8% and 3% respectively, and then grinded uniformly and placed in a reaction kettle. The crystallization product is obtained by crystallizing the mixture in an oven at 95°C for 16 hours. Then, the initial product is obtained by cooling the crystallization product. The initial product is calcined in a muffle furnace at 550°C for 6 hours. Finally, the hard template is removed by washing the product with deionized water several times and filtering. The final product, the 13X molecular sieve with meso-micropore structure, is obtained by drying the product in an oven at 60°C for 12 hours.

[0119] As Figures 5-7As shown, it can be seen that the 13X molecular sieve has a typical 13X structure, and both the purity and the crystallinity are high.

[0120] Example 2

[0121] In this example, first, a proper amount of circulating fluidized bed fly ash containing a certain silicon-aluminum ratio is subjected to magnetic separation to remove iron, then washed with deionized water to remove floating matter, and filtered to remove soluble salts, and then dried in an oven at 110°C for 6 hours to obtain the fly ash raw material. Then, the fly ash raw material, sodium hydroxide, sodium silicate, aluminum hydroxide and hard template are mixed in a proportion of 78%, 10%, 7%, 2% and 3% by mass percentage respectively, and then ground uniformly and placed in a reaction kettle, and then crystallized in an oven at 95°C for 16 hours, and then the crystallization product is cooled to obtain the primary product. The primary product is calcined in a muffle furnace at 550°C for 6 hours. Finally, the product is washed several times with deionized water, filtered, and dried in an oven at 60°C for 12 hours to obtain the final product, the hierarchical pore 13X molecular sieve.

[0122] Compared with Example 1, no seed crystal is added in this Example 2. Therefore, due to the lack of seed crystal directing agent, the product obtained is not pure phase, and the crystallinity is not high. Figure 8 As shown in the scanning electron microscope image of

[0123] Example 3

[0124] In this example, first, a proper amount of circulating fluidized bed fly ash containing a certain silicon-aluminum ratio is subjected to magnetic separation to remove iron, washed with deionized water to remove floating matter, and filtered to remove soluble salts, and then dried in an oven at 110°C for 6 hours to obtain the fly ash raw material. Then, the fly ash raw material, sodium hydroxide, seed crystal and hard template are mixed in a proportion of 77%, 12%, 8% and 3% by mass percentage respectively, and then ground uniformly and placed in a reaction kettle, and then crystallized in an oven at 95°C for 16 hours, and then the crystallization product is cooled to obtain the primary product. The primary product is calcined in a muffle furnace at 550°C for 6 hours. Finally, the product is washed several times with deionized water, filtered, and dried in an oven at 60°C for 12 hours to obtain the final product, the hierarchical pore 13X molecular sieve.

[0125] Compared with Example 1, in this Example 3, no additional silicon / aluminum source is added, and due to the limitation of the silicon-aluminum ratio in the fly ash (i.e., the silicon-aluminum ratio in the fly ash is not within the range of 3-11), as shown in the scanning electron microscope image of Figure 9 As shown in the scanning electron microscope image of

[0126] Example 4

[0127] In this embodiment, firstly, a certain amount of circulating fluidized bed fly ash containing a certain silicon aluminum ratio is subjected to magnetic separation to remove iron, washed with deionized water to remove floating matter, filtered to remove soluble salt, dried in an oven at 110°C for 6 hours, and the fly ash raw material is obtained. Then, the fly ash raw material, sodium silicate, aluminum hydroxide, seed crystal and hard template are mixed in a proportion of 74% by mass, 10%, 5%, 8% and 3% respectively, and then ground uniformly and placed in a reaction kettle. The product is calcined in a muffle furnace at 550°C for 6 hours. Finally, the product is washed several times with deionized water, filtered, and dried in an oven at 60°C for 12 hours, and the final product of hierarchical pore 13X molecular sieve is obtained.

[0128] Compared with Example 1, in this embodiment, no alkali is added, as shown in the scanning electron micrographs of Figure 10 , the obtained product is basically not shaped, that is, there is no molecular sieve structure.

[0129] Example 5

[0130] In this embodiment, firstly, a certain amount of circulating fluidized bed fly ash containing a certain silicon aluminum ratio is subjected to magnetic separation to remove iron, washed with deionized water to remove floating matter, filtered to remove soluble salt, dried in an oven at 110°C for 6 hours, and the fly ash raw material is obtained. Then, the fly ash raw material, sodium silicate, aluminum hydroxide, seed crystal and hard template are mixed in a proportion of 74% by mass, 10%, 5%, 8% and 3% respectively, and then ground uniformly and placed in a reaction kettle. The product is calcined in a muffle furnace at 550°C for 6 hours. Finally, the product is washed several times with deionized water, filtered, and dried in an oven at 60°C for 12 hours, and the final product of hierarchical pore 13X molecular sieve is obtained.

[0131] Compared with Example 1, in this embodiment, a lower silicon aluminum ratio is set (as can be seen from the experimental data, the silicon aluminum ratio is not within the range of 3-11), as shown in the scanning electron micrographs of Figure 11 and Figure 12 , the obtained product is other type of crystal (i.e. 13X molecular sieve is not prepared), and there is a heterogeneous phase.

[0132] The purification system for treating volatile organic compounds according to the present application has at least one of the following advantages:

[0133] (1) The adsorption wheel of the purification system provided by the present application has the characteristics of compact design, simple structure, small footprint, self-operation through waste heat recovery maintenance device, high energy utilization efficiency, etc.

[0134] (2) The adsorption material zeolite in the adsorption wheel of the purification system has the advantages of modular assembly, easy replacement, convenient transportation, small specific heat capacity, less heat absorption, high concentration ratio, high adsorption efficiency, stable operation, low energy consumption, etc.

[0135] (3) The design of the multi-layer zeolite module in the adsorption wheel of the purification system improves the adsorption efficiency of volatile organic compounds;

[0136] (4) The design of the heat exchange pipeline in the adsorption wheel of the purification system improves the desorption efficiency of the zeolite module using recovered heat;

[0137] (5) The use of the moving push rod device and the concentration sensor in the adsorption wheel of the purification system can realize automatic replacement of the zeolite module, avoiding the danger of manual replacement of the zeolite module in high temperature;

[0138] (6) The 13X zeolite of the purification system is prepared from circulating fluidized bed fly ash, without the need for calcination and activation;

[0139] (7) The 13X zeolite of the purification system is prepared without using a solution, with high zeolite yield, high utilization rate of the crystallization kettle, low synthesis pressure, and small environmental pollution;

[0140] (8) The 13X zeolite of the purification system has a microporous-mesoporous structure, greatly improving the mass transfer efficiency;

[0141] (9) The 13X zeolite of the purification system is simple to make, low in cost, and small in pollution, with good promotion advantages.

[0142] (10) The preparation method of the 13X zeolite of the purification system and the 13X zeolite are prepared using bulk solid waste fly ash as raw material, which not only improves the value-added utilization rate of bulk solid waste and expands the comprehensive utilization way of solid waste, but also effectively reduces the preparation cost, achieving the effect of "turning waste into treasure".

[0143] Although some embodiments of the present general inventive concept have been shown and described, it will be apparent to those having ordinary skill in the art that changes can be made in these embodiments without departing from the principles and spirit of the present general inventive concept, the scope of which is defined in the claims and their equivalents.

Claims

1. A purification system for treating volatile organic compounds, comprising: A pretreatment filtration device is used to remove dust and oil from volatile organic compound waste gas; An adsorption rotor, comprising a cylindrical zeolite molecular sieve module for adsorbing and concentrating pre-treated filtered volatile organic compound waste gas, wherein the cylindrical zeolite molecular sieve module is a module composed of 13X molecular sieves; and A catalytic combustion reactor is used to combust and remove volatile organic compounds from the adsorption rotor after adsorption concentration. The 13X molecular sieve is prepared by the following method, which includes the following steps: Fly ash is subjected to magnetic separation to remove iron, followed by washing, filtering and drying to obtain fly ash raw material, wherein the mass percentage of fly ash ranges from 66% to 85%, and the fly ash is circulating fluidized bed fly ash; The fly ash raw material is mixed with sodium hydroxide, silicon source, aluminum source, 13X molecular sieve seed crystals, and hard template, and then ground in air to obtain a mixture. The silicon-to-aluminum ratio in the mixture ranges from 3 to 11, the mass percentage of the 13X molecular sieve seed crystals is 8% to 15%, and the mass percentage of the hard template is 2% to 5%. The mixture is crystallized at 80-98°C for 15-24 hours to obtain a crystallized product, and the crystallized product is cooled to obtain a primary product. The initial product is calcined at a temperature range of 500~600℃ for 4~8 hours to obtain the calcined product. The calcined product is then cooled, washed and filtered in sequence, and then dried at a temperature range of 50~70℃ for 10~15 hours to obtain the 13X molecular sieve. The adsorption rotor includes a shell, a waste gas inlet, and a waste gas outlet. A ceramic heat exchanger and a rotor device are disposed in the shell and are connected to each other. The ceramic heat exchanger is connected to the waste gas inlet, and the rotor device is connected to the waste gas outlet. The rotor device includes multiple columns, and at least one layer of the cylindrical zeolite molecular sieve module for adsorbing volatile organic compounds in waste gas is disposed between adjacent columns.

2. The purification system for treating volatile organic compounds according to claim 1, characterized in that, The rotating wheel device also includes a drive device, a rotary bearing, a bottom disc, and a top disc. The plurality of columns are fixed between the bottom disc and the top disc and are spaced apart along the circumference of the bottom disc. The rotary bearing is driven to the bottom disc, and the drive device is connected to the rotary bearing.

3. The purification system for treating volatile organic compounds according to claim 2, characterized in that, The ceramic heat exchanger and the rotating wheel device are also connected by a heat exchange pipe. The first end of the heat exchange pipe is connected to the ceramic heat exchanger, and the second end of the heat exchange pipe is inserted into the inner cavity of the rotating wheel device. The rotating wheel device includes an adsorption zone and a desorption zone.

4. The purification system for treating volatile organic compounds according to claim 3, characterized in that, A slide rail is provided at the outer edge of the second end of the heat exchange pipe. The top and bottom discs are annular in shape, and flanges that slide and connect with the slide rail are provided on the inner surfaces of the top and bottom discs. A portion of at least one layer of the cylindrical zeolite molecular sieve module through which the heat exchange medium flows constitutes the desorption zone.

5. The purification system for treating volatile organic compounds according to claim 4, characterized in that, The outlet includes an adsorption zone outlet for discharging the clean gas obtained after adsorbing the volatile organic compounds and a desorption zone outlet for discharging the desorbed gas. The ceramic heat exchanger includes a first outlet for discharging waste gas after heat exchange and a second outlet for discharging the heat exchange medium after heat exchange with the waste gas. The first outlet is connected to the adsorption zone, and the second outlet is connected to the heat exchange pipe.

6. The purification system for treating volatile organic compounds according to claim 5, characterized in that, One end of the air outlet of the adsorption zone is located in the inner cavity of the rotating wheel device, and the other end extends outward along the longitudinal direction of the rotating wheel device to the outside of the housing. One end of the gas outlet of the desorption zone is located in the desorption zone, and the other end extends along the longitudinal direction of the adsorption wheel to the outside of the housing. The adsorption zone occupies three-quarters of all the cylindrical zeolite molecular sieve modules in at least one layer of the cylindrical zeolite molecular sieve module, and the desorption zone occupies one-quarter of all the cylindrical zeolite molecular sieve modules in at least one layer of the cylindrical zeolite molecular sieve module.

7. The purification system for treating volatile organic compounds according to claim 5, characterized in that, An axial flow fan for drawing the heat exchange medium from the ceramic heat exchanger to the desorption zone and a heater for heating the heat exchange medium are provided in the heat exchange pipe. The axial flow fan is located near the ceramic heat exchanger and the heater is located near the second air outlet.

8. The purification system for treating volatile organic compounds according to any one of claims 3-7, characterized in that, At least one layer of the cylindrical zeolite molecular sieve module includes an inner molecular sieve module and an outer molecular sieve module, which are arranged along the radial direction of the bottom disk.

9. The purification system for treating volatile organic compounds according to claim 8, characterized in that, The inner cavity is also equipped with a movable push rod device for replacing at least one layer of the cylindrical zeolite molecular sieve module and a sensor for measuring the concentration of the volatile organic compounds. The sensor is signal-connected to the movable push rod device.

10. The purification system for treating volatile organic compounds according to claim 8, characterized in that, The column is a rotating column, which drives the inner molecular sieve module and the outer molecular sieve module on one side to rotate.

11. The purification system for treating volatile organic compounds according to claim 1, characterized in that, The pretreatment filtration device includes coarse filter cotton and medium-efficiency filter bag. The coarse filter cotton is placed on a stainless steel mesh frame, and the medium-efficiency filter bag is placed at the rear end of the coarse filter cotton.

12. The purification system for treating volatile organic compounds according to claim 1, characterized in that, The catalytic combustion reactor includes a preheating chamber and a catalytic combustion chamber. The preheating chamber is connected to the air inlet of the catalytic combustion reactor. After desorption, the volatile organic waste gas, which has been concentrated by adsorption, enters the preheating chamber and exchanges heat through the heat exchange medium in the heat-conducting pipe. The catalytic combustion chamber is equipped with a catalyst reaction bed, where the preheated exhaust gas is burned to produce high-temperature flue gas.

13. The purification system for treating volatile organic compounds according to claim 12, characterized in that, A portion of the high-temperature flue gas is directly discharged into the atmosphere, while another portion flows into the desorption zone of the adsorption rotor as a heat exchange medium.

14. The purification system for treating volatile organic compounds according to claim 1, characterized in that, The sodium hydroxide is 5% to 15% by mass.

15. The purification system for treating volatile organic compounds according to claim 14, characterized in that, The mass percentage of the silicon source and / or the aluminum source is 0% to 15%.

16. The purification system for treating volatile organic compounds according to claim 15, characterized in that, The silicon source includes any one or a combination of sodium silicate, silica gel, or silica.

17. The purification system for treating volatile organic compounds according to claim 16, characterized in that, The aluminum source includes any one or a combination of boehmite, sodium aluminate, or aluminum hydroxide.

18. The purification system for treating volatile organic compounds according to claim 17, characterized in that, The hard template includes any one or a combination of carbon black, carbon nanotubes, or porous carbon.

19. The purification system for treating volatile organic compounds according to any one of claims 14-18, characterized in that, The 13X molecular sieve is a microporous-mesoporous 13X molecular sieve.

20. The purification system for treating volatile organic compounds according to claim 19, characterized in that, The particle size of the mixture is less than or equal to 74 μm, and the washing water is deionized water.

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