Device for improving pressure difference between dense and dilute phases of fluidized bed and application thereof

Abstract

The application discloses a device for improving pressure difference of dense and dilute phase sections of a fluidized bed and application, the top of the fluidized bed is provided with an outlet, and the bottom is provided with an inlet, characterized in that the top of the inside of the fluidized bed is provided with more than one cyclone separator; the outlet of the inside cyclone separator is provided with a leg pipeline, the leg pipeline is provided with more than one purging insertion pipe orifice, and the bottom of the leg pipeline is further provided with a terminal wing valve mechanism; wherein the purging insertion pipe orifice is communicated with a purging insertion pipe, the purging insertion pipe penetrates through the side wall of the fluidized bed and is connected with a flange outside the fluidized bed; wherein outside the fluidized bed, the purging insertion pipe is further provided with a valve and a flow limiting orifice plate to control the gas flow of the purging insertion pipe.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of polycrystalline silicon, in particular to a device for improving the pressure difference between the dense phase and the dilute phase of a fluidized bed and application thereof. BACKGROUND

[0002] In the improved Siemens process for producing polycrystalline silicon, a fluidized bed reactor is used as the reaction equipment for silicon powder, silicon tetrachloride and hydrogen. If the gas-solid fluidized bed is compared to the liquid layer in boiling, the particle group in the fluidized state is equivalent to the liquid itself in boiling, and the gas bubbles rising through the bed are equivalent to the steam bubbles in the boiling liquid, so there is a special two-phase system in this fluidized bed. The particle group in the fluidized state is continuous and is called the continuous phase, and the gas bubbles are dispersed and are called the dispersed phase, also called the dilute phase. In the fluidized bed reactor for chlorohydration, the fine powder of the catalyst and the fine powder of silicon powder with small particle size in the dilute phase section will be elutriated to the upper part of the fluidized bed and suspended for a long time without returning to the dense phase bed of the fluidized bed, which will affect the stable operation of the device. The pressure difference is used to distinguish and judge the dense phase and the dilute phase in the bed, so the area of the dense phase and the dilute phase can be judged by the pressure difference.

[0003] At present, a cyclone separator is commonly used to separate the dust in the dilute phase section from the gas flow, and then the material is returned to the fluidized bed through a wing valve to continue to participate in the reaction, so as to improve the pressure difference between the dilute phase section and the dense phase section. However, the existing cyclone separator has the following disadvantages in terms of return material amount and operability: 1. Large return material amount: After the fine powder in the dilute phase section is separated by the cyclone separator for a long time and returned to the fluidized bed, the unreacted particles will be enriched in the fluidized bed. 2. Poor operability: The structure of the separator in the fluidized bed has been fixed and cannot be changed, so the operability is poor. 3. Material leg is easy to be blocked: Due to the jamming of the wing valve, the silicon powder deposited in the material leg is blocked in the pipeline. Therefore, a new device needs to be developed to solve the above problems. SUMMARY

[0004] The technical problem to be solved by the present application is to provide a device for improving the pressure difference between the dense phase and the dilute phase of a fluidized bed.

[0005] The present application also aims to provide the application of the above device.

[0006] The technical problem to be solved by the present application is to provide a device for improving the pressure difference between the dense phase and the dilute phase of a fluidized bed.

[0007] In order to solve the first technical problem, the application discloses a device for improving the pressure difference between the dense phase and the dilute phase of a fluidized bed, wherein the top of the fluidized bed 1 is provided with an outlet 16, and the bottom is provided with an inlet 15, and the top of the inside of the fluidized bed is provided with one or more internal cyclone separators, and the internal cyclone separators are connected with a valve, a flow limiting orifice plate, a differential pressure gauge, a pipeline and a check valve to form a system for controlling the gas flow.

[0008] The system for controlling the gas flow is specifically that the outlet of the internal cyclone separator 2 is provided with a leg pipeline 21, the leg pipeline 21 is provided with one or more purge insertion tube orifices, and the bottom of the leg pipeline 21 is further provided with a terminal wing valve mechanism 25.

[0009] The purge insertion tube orifice is in communication with a purge insertion tube, the purge insertion tube penetrates through the side wall of the fluidized bed 1, and is connected with a flange 4 outside the fluidized bed 1 in the form of an insertion tube, and the purge insertion tube is a φ15 pressure guide pipeline for introducing hydrogen.

[0010] The purge insertion tube is further provided with a valve and a flow limiting orifice plate outside the fluidized bed 1 to control the gas flow of the purge insertion tube.

[0011] When the number of the purge insertion tube orifices is two or more, the purge insertion tube corresponding to each purge insertion tube orifice in the system for controlling the gas flow is provided with an orifice, and each orifice is connected with a ball valve and a remote differential pressure gauge.

[0012] Preferably, the leg pipeline is provided with three purge insertion tube orifices, i.e., a first purge insertion tube orifice 22, a second purge insertion tube orifice 23 and a third purge insertion tube orifice 24 are arranged at the upper part, the middle part and the lower part of the leg pipeline 21, respectively.

[0013] The purge insertion tube is connected with an air inlet pipeline 34, the air inlet pipeline 34 is provided with a ball valve, a shut-off valve 10, a flow meter 11 and a check valve 12 to control the gas flow of the air inlet pipeline 34, and the outlet of the pipeline 34 is provided with a terminal blind seal.

[0014] The valve includes but is not limited to a ball valve and a shut-off valve, preferably the valve is a ball valve and a shut-off valve, and further preferably the ball valve and the flow limiting orifice plate are connected with the shut-off valve in parallel.

[0015] The center of the flange 4 is provided with a purge insertion tube orifice 41, and the periphery of the flange 4 is provided with a bolt hole 42, the number of the purge insertion tube orifices 41 is one or more, preferably two, Figure 5 three or four, Figure 6 and further preferably three.

[0016] Preferably, the top of the fluidized bed 1 is provided with a plurality of cyclone separators in parallel, each corresponding to one of the four gas flow control systems.

[0017] Further preferably, the fluidized bed 1 is provided with a pressure measuring device system on the outside wall; specifically, the bottom inlet of the fluidized bed 1 is provided with a pressure measuring purge port, the bottom of the side wall is provided with one or more pressure measuring purge ports, and the top outlet is provided with a pressure measuring purge port.

[0018] The pressure measuring purge port is connected through a differential pressure gauge.

[0019] The pressure measuring purge port on the bottom of the side wall of the fluidized bed 1 is connected to the side wall of the fluidized bed through a flange.

[0020] The differential pressure gauge is connected to the pressure measuring purge port through a pressure lead pipe.

[0021] The pressure measuring purge port and the pressure lead pipe are connected through threads; the differential pressure gauge has positive and negative ports, and the differential pressure gauge is connected to the pressure lead pipe through an instrument buckle.

[0022] To solve the above-mentioned second technical problem, the application discloses the application of the above-mentioned device in improving the pressure difference between the dense and dilute phases of the fluidized bed.

[0023] Specifically, the method comprises the following steps: a mixture of hydrogen and silicon tetrachloride is introduced into the fluidized bed 1 through a circulating hydrogen compressor, and silicon powder is introduced into the fluidized bed 1 by pneumatic conveying; after the silicon powder, hydrogen, and silicon tetrachloride enter the fluidized bed, the silicon powder is in a fluidized state under the action of circulating hydrogen, and under certain conditions, the three react to generate chlorosilane and discharge from the outlet of the fluidized bed 1, and fine powder particles (silicon powder) that cannot participate in the reaction are gradually taken to the upper part of the fluidized bed and then returned to the fluidized bed through the action of the cyclone separator.

[0024] After the silicon powder, hydrogen, and silicon tetrachloride enter the fluidized bed, the hydrogen is introduced into the corresponding orifice (such as orifice 711) in sequence through ball valve 514, orifice 714, ball valve 515, shut-off valve 10, flowmeter 11, ball valve 516, orifice 715, and check valve 12; the hydrogen is transported from the purge insertion pipe orifice 22 to the leg pipe 21 through ball valve 51, flow-limiting orifice plate 61, ball valve 52, orifice 72, ball valve 53, and flange 4 from orifice 711, and regular operation in this way can prevent blockage.

[0025] Further, in the above process, the flow rate of the purging hydrogen can be controlled, that is, according to the data collection of the pressure difference change, through simulation and actual working condition verification, a suitable material leg diameter, length and purging gas flow control flow rate are designed. Specifically, the flow rate of the purging hydrogen is controlled by increasing the flow capacity of the flow limiting orifice plate 61, 62 and 63, and the remote control is stable and reliable. For example, if the purging amount needs to be increased, the flow limiting orifice plate corresponding bypass hand valve can be opened to control.

[0026] The right side pressure measurement system reflects the amount of silicon powder in the fluidized bed through the difference of the pressure measurement points arranged at different heights, and can be visually observed through the DCS screen and historical trend. When the value of the pressure difference table increases, especially the eighth pressure difference table 148, it indicates that the fine powder (silicon powder) is enriched in the fluidized bed. At this time, the upper purging hydrogen flow rate needs to be increased, the internal airflow direction of the cyclone separator is changed, more unreacted fine powder is taken out of the fluidized bed with the circulating airflow, and the return material amount of the cyclone separator is reduced. Specifically, the stop valve is opened, the hydrogen flows from the pipeline containing the stop valve, the purging gas amount of the material leg is adjusted to change the separation efficiency of the cyclone separator, more fine powder is taken out of the fluidized bed, the return material amount is reduced, and then the stop valve is closed. If the effect is not obvious by opening only the stop valve 81, the stop valves 81, 82 and 83 can be opened at the same time until the pressure difference in the dilute phase section is reduced, and then the stop valves 81, 82 and 83 are closed. That is, the fine powder is taken out of the fluidized bed by controlling the flow rate of the purging hydrogen of the cyclone material leg, so as to improve the pressure difference in the dilute phase section.

[0027] When there is no wave crest in the remote pressure difference meter, it indicates that the wing valve is opened (only when the silicon powder weight on the valve surface reaches a certain degree, the wing valve will be opened), the material leg is blocked, the stop valve is opened, the hydrogen flows from the pipeline containing the stop valve, the silicon powder blocked in the material leg is taken out, and then the stop valve is closed. If there is still no wave crest in the remote pressure difference meter, the above process is repeated. If there is a wave crest in the remote pressure difference meter, the stop valve is closed.

[0028] The stop valve 81 corresponding to the orifice of the purging insertion pipe is opened, the purging hydrogen is introduced, the hydrogen flows through the ball valve 514, the orifice 714, the ball valve 515, the shut-off valve 10, the flowmeter 11, the ball valve 516, the orifice 715 and the check valve 12 in sequence, and then flows into the hydrogen from the corresponding orifice (such as the orifice 711). The hydrogen is transported from the orifice 711 to the material leg pipeline 21 through the orifice 71, the stop valve 81, the orifice 72, the ball valve 53 and the flange 4.

[0029] When the main road regulating valve fails to be normally used, the parallel ball valve 517 is opened, and the hydrogen is introduced through the bypass.

[0030] Advantages: Compared with the prior art, the present application has the following advantages:

[0031] 1. The pressure difference of the dense phase section of the fluidized bed, i.e. the bed pressure difference, is the difference between the fluidized bed distributor and the lower part of the dilute phase section. A good dense phase pressure difference is a prerequisite for good fluidization of the silicon powder. Maintaining a proper and stable bed pressure difference in the circulating fluidized bed is conducive to improving the conversion rate. Under the condition that the silicon powder supplement is constant and the system load is constant, the method can effectively handle the problem of high dilute phase section pressure difference and stabilize the bed.

[0032] 2. The device can adjust the valve opening according to the changes in the pressure difference of the dense phase section and the dilute phase section, and adjust the dilute phase section pressure difference to the ideal state.

[0033] 3. The device improves the existence of the dense phase and the dilute phase of the fluidized bed, makes the solid particles better into a fluidized state, and improves the yield.

[0034] 4. The device controls the flow of purge hydrogen to prevent and clear the blockage of the cyclone leg, and at the same time, makes the efficiency of the cyclone separator controllable. BRIEF DESCRIPTION OF DRAWINGS

[0035] The above and / or other aspects of the present application will become apparent and more readily appreciated from the following description, taken in conjunction with the accompanying drawings, in which:

[0036] Figure 1 The cyclone separator is in the prior art.

[0037] Figure 2 The device is a whole view.

[0038] Figure 3 The device is a partial schematic view.

[0039] Figure 4 The device is a cross-sectional view of the connection between the inside and outside of the fluidized bed (part 4).

[0040] Figure 5 The device is a cross-sectional view of the connection between the inside and outside of the fluidized bed (part 4).

[0041] Figure 6 The device is a cross-sectional view of the connection between the inside and outside of the fluidized bed (part 4).

[0042] Figure 7 The device is a partial schematic view.

[0043] Notes: 1 is fluidized bed; 2 is internal cyclone separator; 31-33 are the first to third purge insertion pipes; 34 is the air inlet pipe; 4 is flange; 41 is the purge insertion pipe hole on flange 4; 42 is the bolt hole around flange 4; 51-517 are the first to seventeenth ball valves; 61-63 are the first to third flow limiting orifice plates; 71-715 are the first to fifteenth orifice; 81-83 are the first to third shut-off valves; 91-92 are the first and second remote differential pressure gauges; 10 is shut-off valve; 11 is flow meter; 12 is check valve; 131, 134, and 135 are the first, fourth, and fifth pressure measurement purge ports, respectively; 141, 143, 144, and 148 are the first, third, fourth, and eighth differential pressure gauges, respectively; 15 is the inlet of the fluidized bed reactor; 16 is the outlet of the fluidized bed reactor. Detailed Implementation

[0044] Example 1

[0045] One such Figure 2 The device shown is for improving the pressure difference between the dense and dilute phases of a fluidized bed. The fluidized bed 1 has an outlet 16 at the top and an inlet 15 at the bottom. An internal cyclone separator 2 is installed at the top inside the fluidized bed. The cyclone separator is connected to valves, flow restrictor plates, differential pressure gauges, pipelines, and check valves through pipes to form a system for controlling gas flow.

[0046] Among them, such as Figure 3 As shown, the system for controlling gas flow is as follows: the outlet of the internal cyclone separator 2 is provided with a material leg pipeline 21, the material leg pipeline 21 is provided with first to third purge insertion pipe ports 22, 23, and 24, and the bottom of the material leg pipeline 21 is also provided with an end wing valve mechanism 25. Under normal circumstances, the wing valve mechanism is in the closed state, and it will open when blocked.

[0047] The first to third purge insertion pipe orifices 22, 23, and 24 are connected to the first to third purge insertion pipes 31, 32, and 33, respectively. The first to third purge insertion pipes 31, 32, and 33 pass through the side wall of the fluidized bed 1 and are connected to the flange 4 outside the fluidized bed 1 by means of an insertion pipe. The first to third purge insertion pipes 31, 32, and 33 are φ15 pressure guiding lines to introduce hydrogen, and they are connected from the upper, middle, and lower parts by means of insertion pipes. The first to third purge insertion pipes 31, 32, and 33 are connected to the third ball valve 53, the sixth ball valve 56, and the ninth ball valve 59 by valves. They are connected to the material leg line 21 of the internal cyclone separator by welding.

[0048] Outside the fluidized bed 1, the purge insertion pipe is equipped with a ball valve, a flow-limiting orifice plate, and a shut-off valve to control the gas flow rate. The ball valve and the flow-limiting orifice plate are connected to the shut-off valve in parallel. For the first purge insertion pipe: the ball valve 51, the flow-limiting orifice plate 61, and the ball valve 52 are connected in series and then in parallel through the first orifice 71 and the second orifice 72. The first orifice 71, the first shut-off valve 81, the second orifice 72, the third orifice 73, and the third ball valve 53 are connected in series on the first purge insertion pipe 31, and the outlet of the first purge insertion pipe 31 is then connected to the flange 4. The connection methods of the structures in the second purge insertion pipe 32 and the third purge insertion pipe 33 are the same.

[0049] The first purge insertion tube is provided with a third orifice 73, the second purge insertion tube is provided with a sixth orifice 76, and the third purge insertion tube is provided with a ninth orifice 79 and a tenth orifice 710. Each orifice is connected to a ball valve and a remote differential pressure gauge.

[0050] Specifically, the ninth port 79 on the third purge insertion tube 33 is connected in series with the tenth ball valve 510, the first remote differential pressure gauge 91, and the eleventh ball valve 511 to the sixth port 76 on the second purge insertion tube 32; the tenth port 710 on the third purge insertion tube 33 is connected in series with the twelfth ball valve 512, the second remote differential pressure gauge 92, and the thirteenth ball valve 513 to the third port 73 on the first purge insertion tube 31.

[0051] The inlets of the first to third purge insertion tubes 31, 32, and 33, namely the eleventh to thirteenth orifices 711, 712, and 713, are sequentially connected in series on the intake pipe 34. The intake pipe 34 is provided with the following inlets in sequence: fourteenth ball valve 514, fourteenth orifice 714, fifteenth ball valve 515, tenth shut-off valve 10, eleventh flow meter 11, sixteenth ball valve 516, fifteenth orifice 715, twelfth check valve 12, inlet 711 of the first purge insertion tube 31, inlet 712 of the second purge insertion tube 32, and inlet 713 of the third purge insertion tube 33. The seventeenth ball valve 517 is connected in parallel to the intake pipe 34 through the fourteenth orifice 714 and the fifteenth orifice 715. The outlet of the intake pipe 34 is provided with an end blind seal.

[0052] The first to third purge insertion tube orifices 22, 23, and 24 are respectively located at the upper, middle, and lower parts of the material leg pipeline 21.

[0053] Among them, such as Figure 4 As shown, the flange 4 has three purge insertion pipe holes 41 at its center and bolt holes 42 around its perimeter.

[0054] In addition, the external sidewall of the fluidized bed 1 is also equipped with a pressure measuring device system.

[0055] Among them, such as Figure 7 As shown, the pressure measuring device system is specifically as follows: the bottom inlet of the fluidized bed 1 is provided with a pressure measuring purge port, the bottom of the side wall is provided with a first and a fourth pressure measuring purge port 131 and 134, the top outlet of the side wall is provided with a fifth pressure measuring purge port 135, and a pipeline is led out from the purge pipeline of each pressure measuring purge port and connected to both sides of the differential pressure gauge.

[0056] The fluidized bed inlet is connected to the fluidized bed outlet via a first differential pressure gauge 141, where the differential pressure represents the pressure difference between the fluidized bed inlet and outlet. The fluidized bed inlet is also connected to a first pressure-measuring purge port 131 via a third differential pressure gauge 143, where the differential pressure represents the pressure difference of the distributor. This pressure difference indicates the fluidization effect of the silicon powder at the distributor. Since the distributor is located between the first pressure-measuring purge port and the inlet, the distributor pressure difference mentioned in this invention is the pressure difference between the first pressure-measuring purge port 131 and the fluidized bed inlet.

[0057] The first pressure measurement purge port 131 is connected to the fifth pressure measurement purge port 135 via the fourth differential pressure gauge 144, and the fourth pressure measurement purge port 134 is connected to the fifth pressure measurement purge port 135 via the eighth differential pressure gauge 148. Each pair of pressure measurement ports is connected to a differential pressure gauge, and the fluidization effect in the bed can be determined by the pressure difference.

[0058] The pressure testing and purging ports 131, 134 and 135 are respectively connected to the side wall of the fluidized bed via flanges.

[0059] The differential pressure gauges are connected to the pressure measurement and purging port, the inlet of the fluidized bed, and the outlet of the fluidized bed via pressure taps.

[0060] The pressure testing and purging port is connected to the pressure tapping tube by a thread; the differential pressure gauge has positive and negative ports, and the differential pressure gauge is connected to the pressure tapping tube by an instrument clip.

[0061] Example 2

[0062] The application of the device described in Example 1 in improving the pressure difference between the dense and dilute phases of a fluidized bed includes the following steps:

[0063] (1) The mixture of hydrogen and silicon tetrachloride is introduced into the fluidized bed 1 through the circulating hydrogen compressor, and the silicon powder is introduced into the fluidized bed 1 by pneumatic conveying. After the silicon powder, hydrogen and silicon tetrachloride enter the fluidized bed, the silicon powder is in a fluidized state under the action of circulating hydrogen, and under certain conditions, the three react to generate chlorosilane which is discharged from the outlet of the fluidized bed 1, and the fine powder particles (silicon powder) that cannot participate in the reaction are gradually taken to the upper part of the fluidized bed and then returned to the fluidized bed through the action of the cyclone separator.

[0064] (2) At the same time as step (1) is performed, after the silicon powder, hydrogen and silicon tetrachloride enter the fluidized bed, the hydrogen is introduced into the corresponding orifice (such as the eleventh orifice 711) in sequence through the fourteenth ball valve 514, the fourteenth orifice 714, the fifteenth ball valve 515, the tenth shut-off valve 10, the eleventh flow meter 11, the sixteenth ball valve 516, the fifteenth orifice 715 and the twelfth check valve 12. The hydrogen is then transported from the second purge insertion tube orifice 22 to the leg line 21 through the first ball valve 51, the first flow-limiting orifice plate 61, the second ball valve 52, the second orifice 72, the third ball valve 53 and the flange 4, thereby preventing clogging.

[0065] In step (2), the flow rate of the purge hydrogen can be controlled. That is, according to the data collection of the pressure difference change, through simulation and actual working condition verification, the appropriate leg diameter, length and purge gas flow rate control are designed. Specifically, the flow rate of the blowing hydrogen is controlled by increasing the flow rate of the first to third flow-limiting orifice plates 61, 62 and 63, and the remote control is stable and reliable. For example, if the purge amount needs to be increased, the bypass hand valve corresponding to the flow-limiting orifice plate can be opened to control it.

[0066] (3) The right side pressure measurement system reflects the amount of silicon powder in the fluidized bed by the difference between the pressure measurement points set at different heights, which can be visually observed through the DCS screen and historical trend. At the same time as step (1) is performed, when the value of the pressure difference table increases, especially the eighth pressure difference table 148, it indicates that the fine powder (silicon powder) is enriched in the fluidized bed. At this time, the upper purge hydrogen flow rate needs to be increased, and the airflow direction in the cyclone separator is changed, so that more unreacted fine powder is taken out of the fluidized bed with the circulating gas flow, and the return amount of the cyclone separator is reduced. Specifically, the shut-off valve is opened to make the hydrogen flow from the pipeline containing the shut-off valve, and the separation efficiency of the cyclone separator is changed by adjusting the leg purge gas amount, so that more fine powder is taken out of the fluidized bed, the return amount is reduced, and the value of the pressure difference table is reduced, and then the shut-off valve is closed. If only the first shut-off valve 81 is opened, the effect is not obvious, and the first to third shut-off valves 81, 82 and 83 can be opened at the same time until the pressure difference in the dilute phase section is reduced, and then the first to third shut-off valves 81, 82 and 83 are closed. That is, the fine powder is taken out of the fluidized bed by controlling the flow rate of the hydrogen in the cyclone leg, thereby improving the pressure difference in the dilute phase section.

[0067] (4) In step (1), at the same time, when the remote differential pressure gauge has no wave crest, it indicates that the wing valve is opened (only when the valve surface silicon powder weight reaches a certain degree, the wing valve will be opened), the material leg is blocked, the stop valve is opened, the hydrogen gas flows from the pipeline containing the stop valve, the silicon powder blocked in the material leg is taken out, and the stop valve is closed. If the remote differential pressure gauge still has no wave crest, repeat the above process; if the remote differential pressure gauge has a wave crest, close the stop valve.

[0068] In steps (3) and (4), the first stop valve 81 corresponding to the purge insertion pipe orifice is opened, purge hydrogen is introduced, the hydrogen gas passes through the fourteenth ball valve 514, the fourteenth orifice 714, the fifteenth ball valve 515, the tenth shut-off valve 10, the eleventh flow meter 11, the sixteenth ball valve 516, the fifteenth orifice 715, and the twelfth check valve 12, and is introduced into the corresponding orifice (such as the eleventh orifice 711) in turn; the hydrogen gas is transported from the second purge insertion pipe orifice 22 to the material leg pipeline 21 through the orifice first 71, the first stop valve 81, the second orifice 72, the third ball valve 53, and the flange 4.

[0069] Wherein, when the main road regulating valve fails to be normally used, the parallel ball valve 517 is opened, and the hydrogen gas is ensured to be introduced through the bypass.

[0070] The application provides a device for improving the pressure difference of the dense and dilute phase sections of a fluidized bed, and a thought and method for application. There are many methods and approaches for specifically realizing the technical scheme. The above description is only a preferred embodiment of the application. It should be noted that those skilled in the art can make some improvements and refinements without departing from the principle of the application. These improvements and refinements should also be regarded as the protection scope of the application. The components not explicitly described in the embodiment can be realized by using the existing technology.

Claims

1. An apparatus for improving the pressure difference between the dense and dilute phases of a fluidized bed, wherein the fluidized bed (1) has an outlet at the top and an inlet at the bottom, characterized in that, The fluidized bed is provided with one or more internal cyclone separators (2) at the top. The outlet of the internal cyclone separator (2) is provided with a material leg pipeline (21). The material leg pipeline (21) is provided with three purge insertion pipe ports, namely the first purge insertion pipe port (22), the second purge insertion pipe port (23), and the third purge insertion pipe port (24), which are respectively located at the upper, middle, and lower parts of the material leg pipeline (21). The bottom of the material leg pipeline (21) is also provided with an end wing valve mechanism (25). The first purge insertion tube orifice (22), the second purge insertion tube orifice (23), and the third purge insertion tube orifice (24) are respectively connected to the first purge insertion tube (31), the second purge insertion tube (32), and the third purge insertion tube (33). The first purge insertion tube (31), the second purge insertion tube (32), and the third purge insertion tube (33) pass through the side wall of the fluidized bed (1) and are connected to the flange (4) outside the fluidized bed (1). Outside the fluidized bed (1), the purge insertion tube is also equipped with a valve and a flow-limiting orifice plate to control the gas flow rate of the purge insertion tube; The purge insertion tube is connected to the intake pipe, which is equipped with a ball valve, a shut-off valve (10), a flow meter (11), and a check valve (12) to control the flow rate of the gas entering the pipe; the outlet of the pipe is equipped with an end blind seal; the ball valve and the flow limiting orifice plate are connected to the shut-off valve in parallel; the first purge insertion tube is equipped with a third orifice (73), the second purge insertion tube is equipped with a sixth orifice (76), and the third purge insertion tube is equipped with a ninth orifice (79) and a tenth orifice (710); The ninth port (79) on the third purge insertion tube (33) is connected in series with the tenth ball valve (510), the first remote differential pressure gauge (91) and the eleventh ball valve (511) to the sixth port (76) on the second purge insertion tube (32); the tenth port (710) on the third purge insertion tube (33) is connected in series with the twelfth ball valve (512), the second remote differential pressure gauge (92) and the thirteenth ball valve (513) to the third port (73) on the first purge insertion tube (31); The fluidized bed (1) is provided with a pressure measurement purge port at the bottom inlet, one or more pressure measurement purge ports at the bottom of the side wall, and a pressure measurement purge port at the top outlet; the pressure measurement purge ports are connected by a differential pressure gauge. Each purge insertion tube orifice in the control gas flow system is equipped with an orifice, and each orifice is connected to a ball valve and a remote differential pressure gauge.

2. The apparatus according to claim 1, characterized in that, Bolt holes (42) are provided around the flange (4).

3. The application of the device according to claim 1 in improving the pressure difference between the dense and dilute phases of a fluidized bed.

4. The application according to claim 3, characterized in that, When the differential pressure gauge reading increases, open the shut-off valve to allow hydrogen to flow through the pipeline containing the shut-off valve until the differential pressure gauge reading decreases, then close the shut-off valve.

5. The application according to claim 3, characterized in that, When the remote differential pressure gauge has no peak, open the shut-off valve to allow hydrogen to flow through the pipeline containing the shut-off valve, and then close the shut-off valve. If the remote differential pressure gauge still has no peak, repeat the above process. If the remote differential pressure gauge has a peak, close the shut-off valve.

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