Hydrogenation liquid filtering device of hydrogen peroxide produced by anthraquinone fluidized bed process

Abstract

The scheme discloses a hydrogenation liquid filter device for hydrogen peroxide produced by a fluidized bed process of an anthraquinone method, which comprises a fluidized bed reactor and a first filter connected downstream of the fluidized bed reactor, and a monitoring filter connected downstream of the first filter; the monitoring filter is provided with a filter element, differential pressure transmitters are connected to both sides of the filter element in the upstream and downstream, a liquid level meter is further arranged above the filter element, and the lower flange position of the liquid level meter is not lower than the upper flange position of the differential pressure transmitter. The beneficial effects of the scheme are as follows: 1. By arranging the monitoring filter, the catalyst leaked from the first filter due to damage of the filter element or loosening of the seal during long-time use can be effectively monitored and intercepted, and the safety and reliability of the fluidized bed process are improved; 2. By arranging the gas-liquid separator, the gas amount in the hydrogenation turbid liquid entering the first filter is reduced, the filtering efficiency and the operation stability of the first filter are improved, the consumption of hydrogen is reduced, and the production cost is reduced.

Description

Technical Field

[0001] This utility model relates to the field of peroxide production in inorganic chemistry, specifically a hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process. Background Technology

[0002] Hydrogen peroxide is widely used in chemical, papermaking, textile, and environmental protection industries. The only industrially large-scale production method for hydrogen peroxide is the anthraquinone process. This process uses alkyl anthraquinone as a working carrier, dissolving it in an organic solvent to form the working solution. Hydrogen peroxide is produced through three main steps: hydrogenation, oxidation, and extraction. Depending on the type of hydrogenation reactor, the anthraquinone process is divided into fixed-bed and fluidized-bed processes. The fixed-bed process uses millimeter-sized spherical catalysts; the working solution and hydrogen gas flow through a stationary catalyst bed and react to obtain the hydrogenated liquid. The fluidized-bed process uses submicron-sized powdered catalysts; the catalyst and working solution are fluidized under the influence of gas.

[0003] For fixed-bed processes, Chinese patent document CN203612954U, published on May 28, 2014, discloses a hydrogenation section system for producing hydrogen peroxide using the anthraquinone process. In this system, unreacted hydrogen and hydrogenated liquid exiting the reactor are separated by a gas-liquid separator. The gas then enters a tail gas condenser to remove solvent before being directly vented. This undoubtedly increases the consumption of relatively valuable hydrogen. Furthermore, the second bag filter used to filter the hydrogenated liquid is primarily for filtering catalyst powder and alumina powder. However, due to insufficient mechanical strength and filtration accuracy of bag filters, there is a possibility that solid powder may not be effectively intercepted during use, posing a safety hazard.

[0004] Compared to fixed-bed processes, fluidized-bed processes offer more uniform reactions and higher catalyst efficiency, resulting in higher production efficiency. Because fluidized-bed processes use submicron-sized powdered catalysts, the gas, liquid, and solid phases are in a fully mixed state. The hydrogenated liquid exiting the fluidized-bed reactor inevitably carries gas and catalyst particles, thus placing significantly higher demands on filtration compared to fixed-bed processes. Otherwise, the catalyst entering the oxidation process with the hydrogenated liquid can lead to uncontrolled decomposition of the hydrogen peroxide generated, potentially causing an explosion. Therefore, hydrogenated liquid filtration is a critical step in the anthraquinone fluidized-bed process for hydrogen peroxide production. Currently, a common safety procedure is to filter the hydrogenated turbid liquid exiting the fluidized-bed reactor through a primary filter followed by a precision filtration. As mentioned earlier, to maintain catalyst fluidization, the gas feed rate to the fluidized-bed reactor must be sufficiently large. This inevitably results in a high gas content in the liquid exiting the reactor, leading to the loss of expensive hydrogen and affecting the stable operation of the primary filter, reducing its efficiency. Therefore, the filtration system for fluidized-bed processes cannot simply be copied from that of fixed-bed processes.

[0005] Chinese patent document CN106629618A, published on May 10, 2017, discloses a method for installing a sintered metal powder filter element inside or outside a reactor to separate the catalyst from the hydrogenated liquid obtained from the reaction. However, because the hydrogenated liquid to be filtered is not separated into gas and liquid phases, entrained gas enters the filter element, reducing filtration efficiency and causing large fluctuations in the flow rate of the hydrogenated liquid exiting the filter, thus reducing operational stability. Chinese patent document CN107098318A, published on August 29, 2017, discloses a fluidized bed reaction system where the method of drawing the hydrogenated liquid from the bottom of the reactor not only involves a large amount of entrained gas and unstable operation, but also, because the catalyst concentration is highest at the bottom of the fluidized bed reactor, the catalyst content in the hydrogenated liquid entering the filter is also very high, undoubtedly increasing the filtration load.

[0006] More importantly, during long-term use, the primary filter element may be damaged, or the sealing gasket or sealing ring may be damaged, or the filter element may not be installed correctly, potentially leading to a large-scale catalyst leak. If the leaked catalyst enters the oxidation process containing hydrogen peroxide, it will cause uncontrolled decomposition of the hydrogen peroxide, potentially resulting in an explosion. Therefore, if a catalyst leak is detected in the primary filter, the unit must be shut down immediately. However, currently there is no timely and effective method to monitor for catalyst leaks, making it impossible to properly handle leaked catalyst. Summary of the Invention

[0007] Based on the above problems, this utility model provides a hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process, which can improve the filtration efficiency of the primary filter and the safety and reliability of the hydrogenated liquid filtration system.

[0008] To achieve the purpose of this invention, the present invention adopts the following technical solution: a hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process, comprising a fluidized bed reactor and a primary filter connected downstream therefrom. A monitoring filter is connected downstream of the primary filter; The monitoring filter is equipped with a filter element, and differential pressure transmitters are connected to the upstream and downstream sides of the filter element. A level gauge is also installed above the filter element, and the lower flange of the level gauge is not lower than the upper flange of the differential pressure transmitter.

[0009] Preferably, the monitoring filter is also equipped with a nitrogen / steam inlet pipe, a nitrogen / steam condensate outlet pipe, and a catalyst discharge port.

[0010] Preferably, the filter element is a stainless steel fiber sintered felt or a stainless steel metal sintered wire mesh.

[0011] Preferably, a gas-liquid separator is connected between the fluidized bed reactor and the primary filter.

[0012] Preferably, the pipe connecting the fluidized bed reactor to the gas-liquid separator opens at a height of 40% to 65% of the inner cavity height of the fluidized bed reactor.

[0013] Preferably, the gas-liquid separator is equipped with corrugated or sawtooth baffles, with a spacing of 20~50mm between the baffles.

[0014] Preferably, the ratio of gas-liquid separators to primary filters is 1:1 to 1:4.

[0015] Preferably, the primary filter is equipped with a slag discharge port for backflushing operation; the slag discharge port is connected to a height of 3% to 25% of the inner cavity height of the fluidized bed reactor.

[0016] Preferably, a secondary filter is connected downstream of the monitoring filter; the secondary filter has a higher filtration accuracy than the primary filter.

[0017] Preferably, a tertiary filter is connected downstream of the secondary filter; the filtration accuracy of the tertiary filter is higher than that of the secondary filter.

[0018] The beneficial effects of this plan are: 1. By setting up a monitoring filter, it is possible to effectively monitor and intercept catalyst leakage from the primary filter due to filter element damage or loose seal during long-term use, thereby improving the safety and reliability of the fluidized bed process. 2. The gas-liquid separator reduces the amount of gas in the hydrogenated turbid liquid entering the primary filter, improving the filtration efficiency and operational stability of the primary filter, and also reducing hydrogen consumption, which helps to reduce production costs. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the structure of this utility model; Figure 2 This is a schematic diagram of the monitoring filter.

[0020] The components include: fluidized bed reactor 1, gas-liquid separator 2, primary filter 3, primary filter hydrogenated liquid inlet pipe switch valve 3-1, primary filter hydrogenated liquid outlet pipe switch valve 3-2, primary filter backwash liquid inlet switch valve 3-3, primary filter slag discharge pipe switch valve 3-4, primary filter element 3-5, monitoring filter 4, hydrogenated liquid inlet pipe 4-1, hydrogenated liquid outlet pipe 4-2, nitrogen / steam inlet pipe 4-3, nitrogen / steam condensate outlet pipe 4-4, filter element 4-5, differential pressure transmitter 4-6, level gauge 4-7, catalyst discharge port 4-8, hydrogenated liquid storage tank 5, hydrogenated liquid pump 6, secondary filter 7, secondary filter element 7-1, tertiary filter 8, and tertiary filter element 8-1. Detailed Implementation

[0021] The present invention will now be further described with reference to the accompanying drawings and specific embodiments.

[0022] Example 1 Example 1 is a hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process. See details below. Figure 1 As shown, with the left side as the upstream direction and the right side as the downstream direction, the hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process includes a fluidized bed reactor 1 located at the upstream end. The fluidized bed reactor 1 is equipped with a hydrogenated turbid liquid outlet, which is connected to a primary filter 3 downstream through a pipeline. A monitoring filter 4 is connected downstream of the primary filter 3.

[0023] The primary filter 3 is vertical, and the quantity can be selected from 4 to 20 units, arranged around the fluidized bed reactor 1. The primary filter element 3-5 is a stainless steel metal powder sintered filter element with a filtration accuracy of 3-20 microns. In addition to the conventional filtration function, the primary filter 3 is also equipped with a backwashing mechanism for backwashing operations. Specifically, a primary filter hydrogenated turbidity inlet valve 3-1 is installed on the pipeline between the fluidized bed reactor 1 and the primary filter 3, while a primary filter hydrogenated liquid outlet valve 3-2 is installed on the pipeline between the primary filter 3 and the monitoring filter 4. A backwashing pipeline is connected in parallel to the pipeline between the primary filter 3 and the monitoring filter 4, and a primary filter backwash liquid inlet valve 3-3 is installed on the backwashing pipeline. A slag discharge pipeline is connected between the primary filter 3 and the fluidized bed reactor 1, and a primary filter slag discharge valve 3-4 is installed on the slag discharge pipeline. The inlet valve 3-1 and outlet valve 3-2 of the primary filter's hydrogenated liquid are in one group, while the backwash liquid inlet valve 3-3 and slag discharge valve 3-4 are in another group. By controlling the opening and closing of these two groups of valves through a program, the system can automatically switch between filtration and backwashing modes. During filtration, the inlet valve 3-1 and outlet valve 3-2 of the primary filter's hydrogenated liquid are open, while the backwash liquid inlet valve 3-3 and slag discharge valve 3-4 are closed. During backwashing, the inlet valve 3-1 and outlet valve 3-2 of the primary filter's hydrogenated liquid are closed, while the backwash liquid inlet valve 3-3 and slag discharge valve 3-4 are open. The backwash fluid is a hydrogenated liquid, which is pumped from the hydrogenated liquid storage tank 5 (mentioned later) to the primary filter 3 by a backwash pump. During backwashing, the hydrogenated liquid backwashes the catalyst trapped by the primary filter elements 3-5 back into the fluidized bed reactor 1 through the slag discharge port. The slag discharge port of the primary filter 3 is connected to a height of 3% to 25% of the inner cavity of the fluidized bed reactor 1 via a pipeline. When the number of primary filters 3 is small, the filtration capacity and backwash flow rate of a single unit are large, resulting in unstable operation. When the number of units is too large, the investment and operating costs increase. If the filtration accuracy of the primary filter elements 3-5 is too low, it cannot effectively intercept the catalyst; if the filtration accuracy is too high, the filtration flux is insufficient, requiring an increase in the number of filter elements, which increases investment.

[0024] For the specific structure of monitoring filter 4, please refer to Figure 2As shown. In this example, the monitoring filter 4 is a vertical structure, and there is one unit. A filter element 4-5 is located in the middle of the monitoring filter 4. The filter element 4-5 is made of stainless steel fiber sintered felt or stainless steel metal sintered wire mesh; in this example, the former, stainless steel fiber sintered felt, is selected, with a filtration accuracy of 35~60 micrometers. Differential pressure transmitters 4-6 are connected to the upstream and downstream sides of the filter element 4-5. In this example, the differential pressure transmitter 4-6 has a range of 0~100 kPa and an accuracy of 0.1~4.0 class. A level gauge 4-7 is installed above the differential pressure transmitter 4-6. In this example, the lower flange of the level gauge 4-7 is 100 mm higher than the upper flange of the differential pressure transmitter 4-6. A nitrogen / steam inlet pipe 4-3 is installed above the monitoring filter 4, and a nitrogen / steam condensate outlet pipe 4-4 is installed below it. A hydrogenated turbid liquid inlet pipe 4-1 is located at the upper left. The hydrogenated liquid outlet pipe 4-2 shares a liquid outlet pipe with the nitrogen / steam condensate outlet pipe 4-4 below, and is diverted in the middle by a three-way valve. A catalyst discharge port 4-8 is located in the middle of the monitoring filter 4.

[0025] The nitrogen / steam inlet pipe 4-3 on the monitoring filter 4 is used to replace air and pressurize the catalyst when nitrogen is connected, and to purge the catalyst leaking from the primary filter 3 when steam is connected, in order to remove the hydrogenated liquid entrained in the catalyst. The catalyst discharge port 4-8 facilitates the recovery and disposal of leaked catalyst.

[0026] The purpose of setting up monitoring filter 4 is to quickly and accurately detect any abnormality caused by a large amount of catalyst escaping from primary filter 3. Its filtration accuracy needs to be determined based on factors such as the filtration accuracy of primary filter 3 and the size of the catalyst particles used in fluidized bed reactor 1. During normal production, primary filter 3 can effectively intercept relatively intact catalyst particles and fine powder generated by catalyst wear over long-term use. However, a small amount of extremely fine powder may still penetrate the filter element of primary filter 3 and enter downstream processes. Therefore, the accuracy of monitoring filter 4 cannot be too high; otherwise, the pressure differential will increase due to the interception of these fine catalyst particles, failing to achieve the purpose of quickly detecting catalyst leakage. However, its accuracy cannot be too low either; it must effectively intercept the relatively intact catalyst particles leaking from primary filter 3. In addition, a moderate filtration accuracy can maintain a large liquid flow rate, which helps reduce the size of the monitoring filter, facilitates operation, and saves investment.

[0027] Differential pressure transmitters 4-6 are installed on both sides of the filter element 4-5 of the monitoring filter 4 to monitor the differential pressure changes in real time. Selecting appropriate range and accuracy for the differential pressure transmitters 4-6 helps improve monitoring accuracy and prevents catalyst leaks from going undetected. If the differential pressure of the monitoring filter 4 rises rapidly, it indicates a catalyst leak, requiring a shutdown. For this reason, a backup filter is not needed. This method not only accurately monitors catalyst leaks in the primary filter 3 but also effectively intercepts leaked catalyst, significantly improving the safety and reliability of hydrogen peroxide production in the anthraquinone fluidized bed process.

[0028] A level gauge 4-7 is installed above the differential pressure transmitter 4-6. The lower flange of the level gauge 4-7 is 100mm higher than the upper flange of the differential pressure transmitter. The reading of the level gauge 4-7 is controlled at about 15% of the full scale of the level gauge to ensure that the liquid completely submerges the upper flange of the differential pressure transmitter 4-6. This ensures that the differential pressure data does not fluctuate under normal conditions and improves the reliability of monitoring.

[0029] Example 1 is the most basic implementation of this solution. Subsequent examples are all optimized and improved based on this example.

[0030] Example 2 Example 2 adds a gas-liquid separator 2, a secondary filter 7, and a tertiary filter 8 to Example 1.

[0031] A gas-liquid separator 2 is located between the fluidized bed reactor 1 and the primary filter 3. The gas-liquid separator 2 can be a vertical or horizontal separation tank or a partially enlarged pipe. The hydrogenated turbid liquid outlet of the fluidized bed reactor 1 is located at 40%–65% of its internal height, through which the hydrogenated turbid liquid enters the gas-liquid separator 2. A gas outlet is located at the top of the gas-liquid separator 2 and is connected to the gas phase space above the fluidized bed reactor 1 via a pipe; a liquid outlet is located at the bottom of the gas-liquid separator 2 and is connected to the hydrogenated turbid liquid inlet of the downstream primary filter 3 via a pipe. Because hydrogen gas reacts immediately with anthraquinone and is consumed upon entering the fluidized bed reactor 1, the gas content in the upper liquid of the fluidized bed reactor 1 is lower than that at the bottom. Leading the hydrogenated turbid liquid out from approximately 40%–65% of the height of the fluidized bed reactor 1 not only reduces the amount of gas entrained in the hydrogenated turbid liquid but also utilizes the reaction pressure and liquid height pressure difference of the fluidized bed reactor 1 as a driving force to filter the hydrogenated turbid liquid entering the primary filter 3. The gas-liquid separator 2 is equipped with corrugated or sawtooth baffles, with a spacing of 30-50 mm between the baffles. Compared to a gas-liquid separator 2 without baffles, the baffles enhance the separation of gas and hydrogenated liquid, effectively reducing the gas content of the hydrogenated liquid before entering the primary filter 3. Furthermore, the separated hydrogen can be reused after returning to the fluidized bed reactor, thus reducing hydrogen consumption. The spacing between the baffles must ensure the smooth passage of the catalyst-containing hydrogenated liquid while simultaneously enhancing the separation of gas from the liquid. If the spacing is too small, the resistance to the passage of the catalyst-containing hydrogenated liquid is high, potentially preventing smooth discharge; if the spacing is too large, the effective separation of gas from the liquid cannot be achieved.

[0032] The gas-liquid separator 2 can be paired one-to-one with the primary filter 3, or multiple primary filters 3 can extract hydrogenated turbid liquid from a single gas-liquid separator 2 for filtration. It is recommended that the ratio of the number of gas-liquid separators 2 to the number of primary filters 3 be 1:1 to 1:4.

[0033] The hydrogenated liquid discharged from fluidized bed reactor 1 undergoes gas-liquid separation via gas-liquid separator 2, and then passes through primary filter 3 to remove catalyst particles before entering monitoring filter 4. The hydrogenated liquid exiting monitoring filter 4 enters hydrogenated liquid storage tank 5. Hydrogenated liquid storage tank 5 is used for temporary storage of the hydrogenated liquid. Since sufficient pressure is required for subsequent filtration and delivery of the hydrogenated liquid to the oxidation reactor, a hydrogenated liquid outlet is located at the bottom of hydrogenated liquid storage tank 5 and connected to hydrogenated liquid pump 6 via a pipeline for downstream pumping. The hydrogenated liquid temporarily stored in hydrogenated liquid storage tank 5 can also be used for backflushing primary filter 3.

[0034] Downstream of the hydrogenated liquid storage tank 5, a secondary filter 7 and a tertiary filter 8 can be installed sequentially as needed. The secondary filter 7 and tertiary filter 8 operate only in filtration mode, used to completely trap the fine catalyst powder that has penetrated the primary filter 3. The secondary filter 7 is either vertical or horizontal, with at least two units. The filter element 7-1 is a composite filter element consisting of a polyester skeleton + glass fiber membrane or a polyester skeleton + polypropylene membrane, with a filtration accuracy of 1-5 micrometers. The tertiary filter 8 is also either vertical or horizontal, with at least two units. The filter element 8-1 is a composite filter element consisting of a polyester skeleton + glass fiber membrane or a polyester skeleton + polytetrafluoroethylene membrane, with a filtration accuracy of 0.5-1 micrometer. It can be seen that the filtration accuracy increases sequentially from the primary filter element 3-5, the secondary filter element 7-1, and the tertiary filter element 8-1. The secondary filter 7 is used to intercept the extremely fine catalyst powder that has penetrated the primary filter 3, further filtration and purification of the hydrogenated liquid. The tertiary filter 8 is used to intercept extremely fine catalyst powder that penetrates the secondary filter 7. It is the last line of defense in the hydrogenated liquid filtration system, ensuring the cleanliness of the hydrogenated liquid entering the oxidation reactor, thereby improving the safety and reliability of the oxidation reaction. In addition to the number normally used, at least one secondary filter 7 and one tertiary filter 8 are kept on standby. This allows for quick switching to the standby filter when filter element replacement is needed, enabling filter element replacement without stopping the system.

[0035] Same as Example 1.

[0036] Taking a 300,000-ton / year hydrogen peroxide plant with a 35% concentration as an example, the working fluid (140g / L ethylanthraquinone, heavy aromatics: tetrabutylurea: trioctyl phosphate = 76:16:8), catalyst (2% Pd / Al2O3, particle size distribution range 60~180 micrometers), and hydrogen are subjected to a hydrogenation reaction in a fluidized bed reactor 1. The resulting hydrogenated turbid liquid is drawn out from 55% of the height of the fluidized bed reactor 1 and enters a vertical, locally enlarged pipeline gas-liquid separator 2. The gas content of the hydrogenated turbid liquid entering the gas-liquid separator 2 is 26%. Stainless steel corrugated baffles are installed in the gas-liquid separator 2, with a spacing of 30mm between the baffles. The gas separated in the gas-liquid separator 2 returns to the gas phase space above the fluidized bed reactor 1 through pipelines. There are 12 gas-liquid separators 2. The gas content of the hydrogenated turbid liquid exiting the gas-liquid separator 2 is 8%, and it enters a primary filter 3 after exiting from the bottom of the gas-liquid separator 2.

[0037] After the hydrogenated turbid liquid enters the primary filter 3, the catalyst is retained by the sintered metal powder filter element 9. There are 12 primary filters 3, and the filter elements 3-5 are sintered metal powder filter elements made of 316L stainless steel with a filtration accuracy of 10 microns. During filtration, the inlet valve 3-1 and outlet valve 3-2 of the primary filter hydrogenated turbid liquid are open, while the backwash liquid inlet valve 3-3 and slag discharge valve 3-4 are closed. During backwashing, the inlet valve 3-1 and outlet valve 3-2 of the primary filter hydrogenated turbid liquid are closed, while the backwash liquid inlet valve 3-3 and slag discharge valve 3-4 are open. Simultaneously, the backwash pump sends the hydrogenated liquid temporarily stored in the hydrogenated liquid storage tank 5 into the primary filter 3, and backwashes the catalyst retained on the surface of the filter elements 3-5 back into the fluidized bed reactor 1. The slag discharge port is located at 10% of the height of the fluidized bed reactor 1. Through program control, the primary filter 3 can switch between filtration and backwashing modes.

[0038] The hydrogenated liquid, after being filtered by the primary filter 3, enters the monitoring filter 4, a vertical type, with one unit. The filter element 4-5 is a sintered stainless steel wire mesh with a filtration accuracy of 40 microns. Differential pressure transmitters 4-6 are installed on both sides of the filter element 4-5 of the monitoring filter 4 to monitor the differential pressure changes in real time. The differential pressure transmitter 4-6 has a range of 0~40 kPa and an accuracy of 0.2 class. A level gauge 4-7 is installed above the filter element 4-5. The lower flange of the level gauge 4-7 is 100 mm higher than the upper flange of the differential pressure transmitter 4-6. The reading of the level gauge 4-7 is controlled at approximately 15% of its full range to ensure that the liquid completely submerges the upper flange of the differential pressure transmitter 4-6, ensuring monitoring reliability. A nitrogen / steam inlet pipe 4-3 is installed on the monitoring filter 4. When nitrogen is connected, it is used to replace air and pressurize the material. When steam is connected, it is used to purge the catalyst that has leaked from the primary filter 3. The catalyst discharge port 4-8 facilitates the recovery and disposal of leaked catalyst.

[0039] The hydrogenated liquid exiting the monitoring filter 4 enters the hydrogenated liquid storage tank 5, and is then pumped by the hydrogenated liquid pump 6 to the secondary filter 7. The secondary filter 7 is a horizontal type, with three units (two in operation and one as a backup). The filter element 7-1 is a polyester skeleton + glass fiber composite filter element, with a filtration accuracy of 3 microns. The tertiary filter 8 is also a horizontal type, with three units (two in operation and one as a backup). The filter element 8-1 is a polyester skeleton + polytetrafluoroethylene composite filter element, with a filtration accuracy of 1 micron. The filtered hydrogenated liquid is then sent to the oxidation reactor for oxidation reaction.

[0040] The above solution not only improves the filtration efficiency and operational stability of the primary filter and reduces hydrogen consumption, but also enhances the safety and reliability of the hydrogenated liquid filtration system.

Claims

1. A hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process, comprising a fluidized bed reactor (1) and a primary filter (3) connected downstream thereof, characterized in that, The primary filter (3) is connected downstream to a monitoring filter (4); The monitoring filter (4) is equipped with a filter element (4-5). The upstream and downstream sides of the filter element (4-5) are connected to a differential pressure transmitter (4-6). A level gauge (4-7) is also provided above the filter element (4-5). The lower flange of the level gauge (4-7) is not lower than the upper flange of the differential pressure transmitter (4-6).

2. The hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process according to claim 1, characterized in that, The monitoring filter (4) is also equipped with a nitrogen / steam inlet pipe (4-3), a nitrogen / steam condensate outlet pipe (4-4), and a catalyst discharge port (4-8).

3. A hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process according to claim 1 or 2, characterized in that, The filter element (4-5) is a stainless steel fiber sintered felt or a stainless steel metal sintered wire mesh.

4. A hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process according to claim 1 or 2, characterized in that, A gas-liquid separator (2) is connected between the fluidized bed reactor (1) and the primary filter (3).

5. The hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process according to claim 4, characterized in that, The pipe connecting the fluidized bed reactor (1) to the gas-liquid separator (2) opens at a height of 40% to 65% of the inner cavity height of the fluidized bed reactor (1).

6. The hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process according to claim 4, characterized in that, The gas-liquid separator (2) is equipped with a wave-shaped or sawtooth baffle plate, and the distance between the baffle plates is 20~50mm.

7. The hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process according to claim 4, characterized in that, The ratio of the number of gas-liquid separators (2) to the number of primary filters (3) is 1:1 to 1:

4.

8. The hydrogenated liquid filtration device for producing hydrogen peroxide using the anthraquinone fluidized bed process according to claim 4, characterized in that, The primary filter (3) is equipped with a slag discharge port for backflushing operation mode; the slag discharge port is connected to the height of 3% to 25% of the inner cavity of the fluidized bed reactor (1).

9. A hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process according to claim 4, characterized in that, A secondary filter (7) is connected downstream of the monitoring filter (4); the filtration accuracy of the secondary filter (7) is higher than that of the primary filter (3).

10. A hydrogenated liquid filtration device for producing hydrogen peroxide using an anthraquinone fluidized bed process according to claim 8, characterized in that, A tertiary filter (8) is connected downstream of the secondary filter (7); the filtration accuracy of the tertiary filter (8) is higher than that of the secondary filter (7).

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