Method and apparatus for reducing dust-containing gas

Abstract

The application discloses a dust-containing gas reduction method and equipment, and specific operation steps are as follows: raw material gas enters a fluidized bed under the adjusting action of a pressure reducing valve; at the same time, solid-phase material is weighed and stirred in a solid-phase feeding system and then enters the fluidized bed, and the fluidized gas-solid mixture enters an inorganic membrane cross-flow filter to be cross-flow filtered; tail gas after filtration enters a bag-type dust collector to be collected and then enters a post-processing section; and clean gas after filtration is collected from a clean gas outlet. The method successfully realizes dust-containing gas reduction by using the material characteristics of the inorganic membrane and combining the separation mechanism of the cross-flow filtration. The collected clean gas can be directly discharged or continuously produced by entering a downstream process; the concentrated gas is greatly reduced, the post-processing equipment configuration can be reduced, and the investment cost is reduced. The method is mainly used in the gas-solid two-phase separation process of industrial large gas volume and low solid content.

Description

Technical Field

[0001] This invention relates to the field of gas-solid two-phase coherent separation technology, specifically to a method and equipment for reducing the volume of dust-laden gas. Background Technology

[0002] Gas-solid two-phase dry separation technology is an important production unit in industries such as chemical engineering, new energy, and metallurgy. The choice of separation method and equipment directly affects the separation efficiency and industrial economics. Industrial gas-solid separation operations are often characterized by large volumes and low solid content, resulting in large processing equipment configurations and high investment costs. Therefore, it is necessary to reduce the gas phase volume, rationally recover and reuse clean gas, reduce the configuration of gas-solid separation equipment, and lower the overall investment cost of the equipment.

[0003] Currently, common gas-solid separation technologies mainly include centrifugal sedimentation, sieving, filtration, and electrostatic precipitators. Centrifugal sedimentation equipment primarily uses cyclone separators, which are simple in structure and easy to maintain, but are unsuitable for high-end industrial applications and cannot intercept particles with a diameter ≤5μm. Sieving equipment mainly uses traditional candle filters, which require high-end configurations and are costly under large-volume conditions. Moving bed filters have complex structures and low filtration efficiency. Electrostatic precipitators can remove fine powders, but have limited processing capacity. Membrane separation technology has been widely studied in recent years. Inorganic membranes possess advantages such as high permeate flux, excellent mechanical properties, higher filtration accuracy, and excellent chemical stability, and have been successfully applied in gas-solid separation fields such as the silicon industry and coal chemical industry.

[0004] In industrial processes, the most common filtration method is terminal filtration, which suffers from problems such as severe filter media contamination, high filtration resistance, and high backflushing frequency. It requires frequent reliance on backflushing systems to extend the service life of filter elements, and large-volume air handling equipment configurations result in high investment costs. Cross-flow filtration, on the other hand, uses tangential force to control the filter cake thickness. It not only has the advantages of terminal filtration but also enables gas phase volume reduction, reduces the need for post-treatment equipment, lowers construction investment costs, and solves problems such as severe filter media contamination and rapid increase in filtration pressure drop.

[0005] Chinese patent application publication number CN201410331406 introduces a filtration device for high-temperature gas purification, which combines an inorganic membrane with terminal filtration for gas-solid separation. This patent demonstrates the advantages of membrane materials, but the problem of high filtration resistance caused by terminal filtration is not solved, significantly reducing the service life of the membrane. Chinese patent application publication number CN201010105677 introduces a gas-solid separation system and separation method, which uses an inorganic membrane for gas-solid phase catalytic and non-catalytic reaction processes. Chinese patent application publication number CN201010105670 introduces a dry dust removal method for organochlorosilanes. This patent achieves a continuous gas-solid separation process by using a separation membrane without changing the process in the production of methylchlorosilane. Although the above two methods combine inorganic membranes and cross-flow filtration mechanisms, they do not achieve low-frequency backflushing or gas phase volume reduction. Summary of the Invention

[0006] The purpose of this invention is to provide a method for reducing the volume of dust-laden gas with a clear filtration mechanism, high separation efficiency, and simple process, as well as a gas-solid cross-flow device with a simple structure and low investment cost. This device utilizes the material properties of inorganic membranes combined with the separation mechanism of cross-flow filtration to successfully achieve the reduction of dust-laden gas volume, reduce the need for post-treatment equipment, lower investment and construction costs, and simultaneously solve problems such as severe filter media contamination and rapid increase in filtration pressure drop.

[0007] The technical solution provided by this invention is as follows:

[0008] A method for reducing the volume of dust-laden gas includes the following steps:

[0009] The pressure of the raw gas is reduced to 0.01-10.0 MPa;

[0010] After weighing and stirring the solid material, it is fluidized with the raw material gas to form a gas-solid mixture. The gas-solid mixture is then sent to an inorganic membrane cross-flow filter for cross-flow filtration to produce exhaust gas and clean gas.

[0011] The exhaust gas is discharged from the inorganic membrane cross-flow filter and then passed into a bag filter for treatment;

[0012] The clean gas is extracted from the inorganic membrane cross-flow filter, and the extraction ratio of the clean gas is greater than 20-70%.

[0013] The system detects whether the transmembrane pressure difference of the inorganic membrane cross-flow filter meets a first condition or whether the operating time of the inorganic membrane cross-flow filter meets a second condition. If the first or second condition is met, the inorganic membrane cross-flow filter is backflushed through the backflushing system to remove the filter cake generated inside the inorganic membrane cross-flow filter. If the first or second condition is not met, backflushing is not performed.

[0014] The inorganic membrane cross-flow filter includes a housing and a filter element, wherein the filter element is a tubular membrane filter element with a filtration accuracy of 0.1-30μm.

[0015] Furthermore, the raw material gas is compressed air, nitrogen, or hydrogen.

[0016] Furthermore, the solid material is silicon powder, coal powder, or a catalyst.

[0017] Furthermore, the solid material is conveyed by a pneumatic conveying feeding device, and the solid material and the raw gas are fluidized in a fluidized bed.

[0018] Furthermore, the first condition is that the transmembrane pressure difference of the inorganic membrane crossflow filter increases to 50 kPa;

[0019] The second condition is that the inorganic membrane cross-flow filter operates for 24 hours.

[0020] Furthermore, the pneumatic conveying and feeding equipment is controlled by a PLC controller.

[0021] The present invention also provides a dust-laden gas reduction device, which adopts the above-mentioned dust-laden gas reduction method and includes a solid-phase feeding system, an inorganic membrane cross-flow filter and a bag filter connected in sequence through pipelines;

[0022] The solid-phase feeding system includes a pneumatic conveying feeder and a fluidized bed. The fluidized bed is connected to the raw material gas conveying pipeline and the pneumatic conveying feeder. The fluidized bed is used to fluidize the raw material gas and solid materials to form a gas-solid mixture.

[0023] The inorganic membrane cross-flow filter is provided with a gas-solid mixture inlet, a clean gas outlet, an exhaust gas outlet, and a backflush port on its outer shell. The gas-solid mixture inlet is connected to the fluidized bed, the exhaust gas outlet is connected to the bag filter, and the backflush port is connected to an external backflush system.

[0024] Furthermore, the filter element includes a metal membrane with a filtration accuracy of 1 μm.

[0025] Furthermore, a pressure reducing valve and a first volumetric flow meter are installed on the raw gas conveying pipeline;

[0026] Differential pressure transmitters are respectively installed on the pipelines connecting the clean gas outlet and the exhaust gas outlet. A first regulating valve is also installed between the bag filter and the exhaust gas outlet. A second volumetric flow meter and a second regulating valve are installed on the pipeline connecting the clean gas outlet.

[0027] Compared with the prior art, the beneficial effects of the present invention are:

[0028] (1) Under low-frequency backflushing conditions, the present invention effectively achieves gas-solid separation by utilizing the performance advantages of inorganic membrane materials combined with cross-flow filtration mechanism.

[0029] (2) This invention can extract 20%-70% or more of clean gas volume, achieving gas phase reduction;

[0030] (3) The present invention has a stable transmembrane pressure difference, which enables a short process flow; the separation efficiency is >99.9%;

[0031] (4) The present invention can reduce the equipment configuration of the exhaust gas after-treatment section and reduce investment costs. Attached Figure Description

[0032] Figure 1 This is a schematic diagram of the dust-laden gas reduction process in an embodiment of the present invention;

[0033] In the diagram: a-raw material gas, b-solid material, c-tail gas, d-clean gas, e-gas-solid mixture; 100-solid feeding system, 200-inorganic membrane cross-flow filter, 300-bag filter; 1-pressure reducing valve, 2-first volumetric flow meter, 3-pressure gauge, 4-second volumetric flow meter, 5-first regulating valve, 6-differential pressure transmitter, 7-second regulating valve;

[0034] Figure 2 The curves showing the changes in clean gas flow rate and transmembrane pressure difference with filtration time under different gas flow rates in this embodiment of the invention;

[0035] Figure 3 This is a schematic diagram of the inorganic membrane cross-flow filter structure in an embodiment of the present invention;

[0036] In the diagram: 201-Gas-solid mixture inlet, 202-Shell, 203-Filter element, 205-Clean gas outlet, 206-Exhaust gas outlet, 207-Airflow zone, 208-Backflush port;

[0037] Figure 4 This is a schematic diagram of the solid-phase feeding system in an embodiment of the present invention;

[0038] In the diagram: 101 - pneumatic conveying and feeding equipment, 102 - fluidized bed. Detailed Implementation

[0039] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the embodiments described below are only some embodiments of this application, not all embodiments. The components of the embodiments of this application described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0040] Therefore, the detailed description of the embodiments of this application provided below with reference to the accompanying drawings is intended merely to illustrate selected embodiments of this application and is not intended to limit the scope of protection claimed by this application. All other embodiments obtained by those skilled in the art based on the embodiments of this application without inventive effort are within the scope of protection of this application.

[0041] It should be understood that in the description of embodiments of the present invention, the terms "first," "second," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Therefore, features defined with "first," "second," etc., may explicitly or implicitly include one or more of the stated features.

[0042] In the description of the embodiments of the present invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," "connect," and "link" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection, an electrical connection, or a connection that allows for mutual communication; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in the embodiments of the present invention according to the specific circumstances.

[0043] See Figure 1 This invention provides a method for reducing the volume of dust-laden gas, comprising the following steps:

[0044] Step S1: Reduce the pressure of the raw material gas a to control the pressure between 0.01-10.0 MPa.

[0045] In step S1, the raw material gas a is depressurized to a safe range of 0.01-10.0 MPa before being introduced into the pipeline to prevent excessive pressure from damaging the pipeline or causing a safety accident. This step typically uses a pressure reducing valve for depressurization.

[0046] Step S2: After weighing and stirring the solid material b, it is fluidized with the raw material gas a to form a gas-solid mixture e. The gas-solid mixture e is sent into the inorganic membrane cross-flow filter 200 for cross-flow filtration to produce tail gas c and clean gas d.

[0047] Step S3: The exhaust gas c is discharged from the inorganic membrane cross-flow filter 200 and then passed into the bag filter 300 for treatment.

[0048] Step S4: The clean gas d is extracted from the inorganic membrane cross-flow filter 200, and the extraction ratio of the clean gas d reaches 20%-70%.

[0049] Step S5: Detect whether the transmembrane pressure difference of the inorganic membrane cross-flow filter 200 meets the first condition or whether the operating time of the inorganic membrane cross-flow filter 200 meets the second condition. If the first condition or the second condition is met, the inorganic membrane cross-flow filter 200 is backflushed through the backflushing system to remove the filter cake generated in the inorganic membrane cross-flow filter 200; if the first condition or the second condition is not met, backflushing is not performed.

[0050] like Figure 3 As shown, the inorganic membrane cross-flow filter 200 includes a housing 202 and a filter element 203. The filter element 203 is a tubular membrane filter element with a filtration accuracy of 0.1-30μm and is made of metal or ceramic.

[0051] The inorganic membrane cross-flow filter 200 has a gas-solid mixture inlet 201 at the front end, a clean gas outlet 205 and an exhaust gas outlet 206 at the rear end, and filter elements 203 fixed by pressure plates at both ends. The area between the outer shell 202 and the filter elements 203 is the airflow area 207.

[0052] Optionally, the raw material gas a is an industrial gas such as compressed air, nitrogen, hydrogen, or synthesis gas.

[0053] Optionally, the solid material b is a powder solid such as silicon powder, coal powder, or catalyst.

[0054] Optionally, the solid material b is conveyed by a pneumatic conveying feeding device 101, and the solid material b and the raw material gas a are fluidized in a fluidized bed 102.

[0055] Optionally, the first condition is that the transmembrane pressure difference of the inorganic membrane crossflow filter 200 increases to 50 kPa.

[0056] The second condition is that the inorganic membrane cross-flow filter 200 operates for 24 hours.

[0057] Optionally, the pneumatic conveying and feeding device 101 is controlled by a PLC controller.

[0058] The present invention also provides a dust-laden gas reduction device, which includes a solid-phase feeding system 100, an inorganic membrane cross-flow filter 200 and a bag filter 300 connected in sequence by pipelines.

[0059] like Figure 4 As shown, the solid-phase feeding system 100 includes a pneumatic conveying feeder 101 and a fluidized bed 102. The fluidized bed 102 is connected to the raw material gas conveying pipeline and the pneumatic conveying feeder 101, respectively. The fluidized bed 102 is used to fluidize the raw material gas a and solid material b to form a gas-solid mixture e.

[0060] like Figure 3 As shown, the inorganic membrane cross-flow filter 200 has a gas-solid mixture inlet 201, a clean gas outlet 205, an exhaust gas outlet 206, and a backflush port 208 on its outer shell 202. The gas-solid mixture inlet 201 is connected to the fluidized bed 102, the exhaust gas outlet 206 is connected to the bag filter 300, and the backflush port 208 is connected to an external backflush system. An airflow region 207 exists between the outer shell 202 and the filter element 203.

[0061] Optionally, the filter element 203 is a single stainless steel filter cartridge and a metal membrane. The stainless steel filter cartridge has a pore size of 19 mm and a wall thickness of 2 mm. The metal membrane has a filtration accuracy of 1 μm and is made of 316L stainless steel.

[0062] Optionally, the raw material gas conveying pipeline is equipped with a pressure reducing valve 1 and a first volumetric flow meter 2.

[0063] Differential pressure transmitters 6 are respectively installed on the pipelines of the clean gas outlet 205 and the exhaust gas outlet 206. A first regulating valve 5 is also installed between the bag filter 300 and the exhaust gas outlet 206. A second volumetric flow meter 4 and a second regulating valve 7 are installed on the pipeline connected to the clean gas outlet 205.

[0064] The pneumatic conveying and feeding device 101 is connected to a PLC controller. The feeding speed, feeding time, and feeding amount are all controlled by the PLC controller.

[0065] Example 1

[0066] This embodiment provides a method for reducing the volume of dust-laden gas using the aforementioned equipment. The solid material b is silicon powder with a particle size of 5 μm, and the raw material gas a is compressed air with a working pressure of 0.35 MPa and a flow rate of 15 m³ / s. 3 / h, initial dust concentration 260g / m³ 3 The filter element has a filtration accuracy of 5μm and an operating time of 2 hours. The pneumatic conveying feeding equipment 101 has a processing capacity of 4kg / h. The PLC controller is a Siemens PLC. Before starting the device, the corresponding process parameters are set in advance using the PLC controller, and the corresponding data are collected during the experiment.

[0067] The specific steps for using this equipment to reduce the volume of dust-laden gas are as follows:

[0068] Compressed air is regulated to a safe operating range by pressure reducing valve 1 and then introduced into the pipeline. Silica powder is weighed and stirred in solid phase feeding system 100 and then enters inorganic membrane cross-flow filter 200 along with the compressed air for cross-flow filtration. Dust-laden exhaust gas c enters bag filter 300 from exhaust gas outlet 206 at the rear end of inorganic membrane cross-flow filter 200 along the tangential direction for solid phase particle recovery. The filtered clean gas d permeates from the membrane tube side along the normal direction under pressure and is extracted from clean gas outlet 205.

[0069] By adjusting process parameters such as airflow velocity, the relationship between transmembrane pressure difference and clean gas extraction rate in the short-process technology was obtained. Under different process parameters, with the increase of filtration time, the clean gas extraction rate gradually decreased and tended to stabilize, while the transmembrane pressure difference also tended to stabilize after rising to a certain value, and the clean gas extraction rate reached 20%-70%.

[0070] To further illustrate the excellent volume reduction effect and high clean gas production rate of this embodiment, the variation curves of transmembrane pressure difference and clean gas production rate in the short-process were obtained by adjusting the airflow velocity (e.g., Figure 2 (As shown in the figure). It can be seen from the figure that, at different gas velocities, with increasing filtration time, the clean gas output gradually decreases and tends to stabilize, and the transmembrane pressure difference also tends to stabilize after rising to a certain value. Furthermore, the clean gas output stabilizes between 20% and 70%. The curves show different trends under different process parameters. Figure 2 Similarly, this indicates that the method can achieve the reduction of dust-laden gas volume.

[0071] When the system has been running for 24 hours or the transmembrane pressure difference increases to 50 kPa, the backflushing setpoint is reached, with a backflushing time of 2 seconds and a backflushing pressure of 0.5 MPa. The transmembrane pressure difference can be obtained from the pressure gauge 3 installed on the inorganic membrane crossflow filter 200.

[0072] This embodiment effectively achieved the extraction of clean gas (extraction ratio of 20%-70%) by adjusting the above process parameters, successfully reducing the gas phase volume. It is worth noting that this embodiment achieved low-frequency backflushing compared to the 0.5h or 1h online backflushing frequency of industrial candle filters. To ensure the filtration performance of the filter element, a backflushing was performed after all experiments were completed.

[0073] The complete cross-flow system of this invention comprises a solid-phase feeding system 100, an inorganic membrane cross-flow filter 200, a bag filter 300, and various instrument valves. The raw material gas a is conveyed via a stainless steel pipeline. A fluidized bed 102 is installed at the rear end of the pneumatic conveying feeder 101 to facilitate fluidization. It is connected to the inorganic membrane cross-flow filter 200 via a stainless steel pipeline. The inorganic membrane cross-flow filter 200 is made of stainless steel, with a gas-solid mixture inlet 201 at the front end, a clean gas outlet 205 on the side end (with a reserved backflushing port 208), and a tail gas outlet 206 at the rear end. The dust-laden gas is connected to the bag filter 300 via a stainless steel pipeline, and the bag filter 300 is connected to the post-processing section via a stainless steel pipeline.

[0074] The solid material b in the pneumatic conveying feeding device 101 is silicon powder. After the raw material gas a is conveyed by the solid feeding system 100, the silicon powder is fluidized in the fluidized bed 102 and enters the inorganic membrane cross-flow filter 200 along the tangential direction of the pipeline for cross-flow filtration. The cross-flow gas volume is 15m³. 3 / h, dust concentration on the feed side is approximately 260g / m³ 3 The gas-solid mixture e is passed into the bag filter 300 under the action of the raw material gas a. The dust concentration of the gas passing through the inorganic membrane cross-flow filter 200 and the bag filter 300 is 350 g / m³. 3 The transmembrane pressure difference gradually increased from 0 to 2.79 kPa and then stabilized. The extracted clean gas volume (d) increased from 6.1 m³ / s. 3 / h gradually decreased to 4.98m 3 / h tends to stabilize.

[0075] During the filtration process, solid material b is intercepted by filter element 203, clean gas d permeates through the membrane surface and is discharged from clean gas outlet 205, and exhaust gas c enters the bag filter 300 after passing through inorganic membrane cross-flow filter 200. When the system has been running for 24 hours or the transmembrane pressure difference increases to 50 kPa, the backflushing system is activated to backflush filter element 203 through backflushing port 208, causing the filter cake to fall off and allowing the exhaust gas c that has passed through inorganic membrane cross-flow filter 200 to enter the bag filter 300. During backflushing, the first regulating valve 5 is closed. Throughout the process, the second regulating valve 7 remains open.

[0076] The clean gas d flowing out of the inorganic membrane cross-flow filter 200 is taken out from the clean gas outlet 205. The solid material intercepted by the inorganic membrane cross-flow filter 200 and the bag filter 300 enters the post-processing section. The configuration of filter elements in subsequent equipment can be reduced by 30%, and the corresponding container investment cost is also reduced.

[0077] The above description is merely the preferred embodiment of this application, but the scope of protection of this application is not limited thereto. Any variations or substitutions within the technical scope disclosed in this application should be included within the scope of protection of this application. Therefore, the scope of protection of this application should be determined by the scope of the claims.

Claims

1. A method for reducing the volume of dust-laden gas, characterized in that, Includes the following steps: The pressure of the raw gas is reduced to 0.01-10.0 MPa; After weighing and stirring the solid material, it is fluidized with the raw material gas to form a gas-solid mixture. The gas-solid mixture is then sent to an inorganic membrane cross-flow filter for cross-flow filtration to produce exhaust gas and clean gas. The exhaust gas is discharged from the inorganic membrane cross-flow filter and then passed into a bag filter for treatment; The clean gas is extracted from the inorganic membrane cross-flow filter, and the extraction ratio of the clean gas is greater than 20%-70%. The system detects whether the transmembrane pressure difference of the inorganic membrane cross-flow filter meets a first condition or whether the operating time of the inorganic membrane cross-flow filter meets a second condition. If either the first or second condition is met, the inorganic membrane cross-flow filter is backflushed through the backflushing system to remove the filter cake generated inside the inorganic membrane cross-flow filter. If either the first or second condition is not met, backflushing is not performed. The backflushing time is 2 seconds, and the backflushing pressure is 0.5 MPa. The inorganic membrane cross-flow filter includes a housing and a filter element, wherein the filter element is a tubular membrane filter element with a filtration accuracy of 0.1-30μm; The first condition is that the transmembrane pressure difference of the inorganic membrane crossflow filter increases to 50 kPa; The second condition is that the inorganic membrane cross-flow filter operates for 24 hours.

2. The method for reducing the volume of dust-laden gas according to claim 1, characterized in that: The raw material gas is compressed air, nitrogen, or hydrogen.

3. The method for reducing the volume of dust-laden gas according to claim 1, characterized in that: The solid material is silicon powder, coal powder, or a catalyst.

4. The method for reducing the volume of dust-laden gas according to any one of claims 1-3, characterized in that: The solid material is conveyed by a pneumatic conveying feeding device, and the solid material and the raw gas are fluidized in a fluidized bed.

5. The method for reducing the volume of dust-laden gas according to claim 4, characterized in that: The pneumatic conveying and feeding equipment is controlled by a PLC controller.

6. A dust-laden gas reduction device, employing the dust-laden gas reduction method as described in any one of claims 1-5, characterized in that: It includes a solid-phase feeding system, an inorganic membrane cross-flow filter, and a bag filter, which are connected in sequence by pipelines. The solid-phase feeding system includes a pneumatic conveying feeder and a fluidized bed. The fluidized bed is connected to the raw material gas conveying pipeline and the pneumatic conveying feeder. The fluidized bed is used to fluidize the raw material gas and solid materials to form a gas-solid mixture. The inorganic membrane cross-flow filter is provided with a gas-solid mixture inlet, a clean gas outlet, an exhaust gas outlet, and a backflush port on its outer shell. The gas-solid mixture inlet is connected to the fluidized bed, the exhaust gas outlet is connected to the bag filter, and the backflush port is connected to an external backflush system. The system detects whether the transmembrane pressure difference of the inorganic membrane cross-flow filter meets a first condition or whether the operating time of the inorganic membrane cross-flow filter meets a second condition. If either the first or second condition is met, the inorganic membrane cross-flow filter is backflushed through the backflushing system to remove the filter cake generated inside the inorganic membrane cross-flow filter. If either the first or second condition is not met, backflushing is not performed. The backflushing time is 2 seconds, and the backflushing pressure is 0.5 MPa. The inorganic membrane cross-flow filter includes a housing and a filter element, wherein the filter element is a tubular membrane filter element with a filtration accuracy of 0.1-30μm; The first condition is that the transmembrane pressure difference of the inorganic membrane crossflow filter increases to 50 kPa; The second condition is that the inorganic membrane cross-flow filter operates for 24 hours.

7. The dust-laden gas reduction device according to claim 6, characterized in that: The filter element includes a metal membrane with a filtration accuracy of 1 μm.

8. The dust-laden gas reduction device according to claim 6, characterized in that: The raw gas conveying pipeline is equipped with a pressure reducing valve and a first volume flow meter; Differential pressure transmitters are respectively installed on the pipelines connecting the clean gas outlet and the exhaust gas outlet. A first regulating valve is also installed between the bag filter and the exhaust gas outlet. A second volumetric flow meter and a second regulating valve are installed on the pipeline connecting the clean gas outlet.

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