Fluidized bed reactor discharge system, method, and electronic device

Abstract

The present application relates to the technical field of fluidized bed reactor, and particularly relates to a fluidized bed reactor discharge system, a method and an electronic device, the system comprising a spraying device and a discharge tank, a gas inlet of the spraying device being connected to a first gas source through a first pipeline, a gas outlet of the spraying device being connected to a gas inlet of the fluidized bed reactor through a second pipeline, an ejector of the spraying device being connected to a first gas outlet of the discharge tank through a third pipeline, a feed inlet of the discharge tank being connected to a discharge outlet of the fluidized bed reactor through a fourth pipeline, a second gas outlet of the discharge tank being connected to the gas inlet of the fluidized bed reactor through a fifth pipeline, a first gas inlet of the discharge tank being connected to a circulating pipeline of the fluidized bed reactor through a sixth pipeline, a second gas inlet of the discharge tank being further connected to a second gas source through a seventh pipeline, and a discharge outlet of the discharge tank being connected to a downstream device through an eighth pipeline. The present application can improve the efficiency of the condensed polyethylene production process, shorten the gas recovery path, and simplify the operation process.

Description

Technical Field

[0001] This invention relates to the field of fluidized bed reactor technology, and in particular to a fluidized bed reactor discharge system, method, and electronic equipment. Background Technology

[0002] Gas-phase polymerization is one of the main processes for producing polyethylene, generally including several steps such as raw material refining, polymerization reaction, powder degassing, granulation, conveying, and packaging. In the polymerization unit, refined ethylene, comonomers (1-butene-1, 1-hexene, or 1-octene), isopentane (inducing condenser), hydrogen, and nitrogen are added to a fluidized bed reactor. Under the action of a catalyst and co-catalyst, a polymerization reaction occurs to produce polyethylene. Unreacted raw material gases are discharged from the top of the fluidized bed reactor, pressurized by a circulating gas compressor, and cooled by a circulating gas condenser before being recycled. The circulating gas keeps the polyethylene powder in the fluidized bed reactor in a fluidized state and removes the heat of reaction through the circulating gas cooler. When the polymerization reaction in the fluidized bed reactor reaches a certain stage, and the bed level and / or weight reach a set value, the discharge system is activated, discharging the polyethylene solids from the reactor through the discharge port on the reactor side wall. The solids are then transported to the product degassing chamber by nitrogen or exhaust gas recovery gas. Nitrogen gas introduced from the bottom of the degassing chamber carries hydrocarbon components from the resin powder and is blown out from the top of the degassing chamber into the exhaust gas recovery system. Liquid materials such as copolymer monomers and induced condensers are recovered and pumped back to the fluidized bed reactor. Non-condensable gases are sent back to the discharge system as transport gases, or partially discharged to the flare as required by pressure control.

[0003] The increasing demand for polyethylene resin underscores the importance of further enhancing the production capacity of existing industrial polyethylene plants. The biggest limiting factor for increasing the production capacity of gas-phase polyethylene is the removal of the heat of reaction. Existing technologies have proposed a "gas-phase fluidized bed polyethylene condensation process," which involves evaporating an easily condensable liquid in the reactor to remove the heat of polymerization, thereby significantly increasing the space-time yield of polyethylene.

[0004] For the vapor-phase polyethylene condensation process, many systematic methods exist for discharging solid materials from fluidized bed reactors. However, existing discharge systems and methods still present several potential problems: First, the high-pressure gas mixture (carrying a large amount of raw material gas or gas / liquid mixture) fills the pores inside and around the particles, leading to additional losses of unreacted raw materials. The lost gas needs to be replenished and recycled back into the system through compression, condensation, and other processes, increasing equipment costs and energy consumption. Second, in condensation processes, the condensate content of the material at the bottom of the fluidized bed polymerization reactor is high. If traditional discharge processes are used, the discharge pipeline leading from the bottom of the fluidized bed near the distribution plate often results in slow discharge rates and is prone to clogging due to the excessive condensate content. Simultaneously, the discharged material carries away a large amount of condensate, not only losing the condensing medium but also increasing the workload of the subsequent degassing chamber. Patents CN200780037815.5 and CN200780034097.6, both filed on September 10, 2007, describe a discharge system for removing solid / gas mixtures from a fluidized bed pressure vessel. Although this system reduces the loss of reaction raw materials and energy consumption, it not only fails to achieve the desired application effect for fluidized bed reactors in condensation processes, but also leads to greater energy consumption and a higher failure rate.

[0005] To improve the discharge efficiency of fluidized bed reactors in condensation processes and reduce raw material entrainment waste and energy loss, Chinese invention patent application CN201410645418.8, filed on November 6, 2014, discloses a fluidized bed reactor discharge system for condensation processes. The system includes a settling container and a transfer container, with an ejector installed between the settling container and the fluidized bed reactor. Compared to traditional discharge processes, this significantly reduces raw material gas loss and energy loss. Chinese invention patent application CN201510662171.5, filed on October 14, 2015, discloses a single-gas-phase fluidized bed discharge system and method for multi-zone polymerization reactions. This method uses three discharge ports, with each flash tank equipped with two filters and two buffer tanks. High-frequency, pulsed discharge from each system forms a continuous and stable discharge stream; however, the process is complex and difficult to operate.

[0006] Although existing discharge methods have improved the discharge efficiency of fluidized bed reactors in condensation processes and reduced raw material entrainment waste and energy loss, they still require discharge tanks and at least one transfer container, or at least two-stage flash evaporation systems. These methods result in high equipment costs, long recovery gas paths, cumbersome operation, long filling cycles, and limited product production rates, failing to meet the higher production requirements of current new processes. Summary of the Invention

[0007] To address the above problems, this invention provides a fluidized bed reactor discharge system, method, and electronic equipment.

[0008] The fluidized bed reactor discharge system provided by this invention includes:

[0009] An injection device is used to deliver raw material gas to a fluidized bed reactor and perform a suction operation on a discharge tank; wherein, the air inlet of the injection device is connected to a first gas source through a first pipeline, the air outlet of the injection device is connected to the air inlet of the fluidized bed reactor through a second pipeline, and the ejector port of the injection device is connected to the first air outlet of the discharge tank through a third pipeline.

[0010] A discharge tank is used to receive the material discharged from the fluidized bed reactor and transfer it to downstream devices. The discharge tank's inlet is connected to the fluidized bed reactor's outlet via a fourth pipeline; its second outlet is connected to the fluidized bed reactor's inlet via a fifth pipeline; its first inlet is connected to the fluidized bed reactor's circulation pipeline via a sixth pipeline; its second inlet is connected to a second gas source via a seventh pipeline; and its discharge outlet is connected to the downstream devices via an eighth pipeline. Furthermore, each pipeline is equipped with a control valve for opening and closing the pipeline.

[0011] Specifically, a first control valve is installed on the first pipeline, a second control valve is installed on the second pipeline, a third control valve is installed on the third pipeline, a fourth control valve is installed on the fourth pipeline, a fifth control valve is installed on the fifth pipeline, a sixth control valve is installed on the sixth pipeline, a seventh control valve is installed on the seventh pipeline, and an eighth control valve is installed on the eighth pipeline.

[0012] Furthermore, the system also includes:

[0013] The first gas purging line is connected to the first gas purging line inlet on the fourth line.

[0014] The outlet of the second gas purging line is connected to the inlet of the second gas purging line on the fifth line.

[0015] The outlet of the third gas purging line is connected to the inlet of the third gas purging line on the second line.

[0016] Furthermore, each gas purging line is equipped with a control valve for controlling the opening and closing of the gas purging line;

[0017] A ninth control valve is installed on the first gas purging line, a tenth control valve is installed on the second gas purging line, and an eleventh control valve is installed on the third gas purging line.

[0018] Furthermore, the inlet of the first gas purging line is located at a preset position between the fluidized bed reactor and the fourth control valve;

[0019] The inlet of the second gas purging line is located at a preset position between the fluidized bed reactor and the fifth control valve;

[0020] The inlet of the third gas purging line is located at a preset position between the fluidized bed reactor and the second control valve.

[0021] Furthermore, the system also includes:

[0022] A gas filter is installed at the top of the discharge tank, and a third pipeline is connected to the first exhaust port of the discharge tank through the gas filter.

[0023] Furthermore, the sixth pipeline is connected to the first air inlet of the discharge tank via a gas filter.

[0024] The fluidized bed reactor discharge method provided by this invention is based on the above-described system and includes the following steps:

[0025] Control the third, fourth, fifth, sixth, seventh, and eighth pipelines to perform shutdown operations;

[0026] When the preset discharge conditions are met, the fourth and fifth pipelines are controlled to start, so that the fluidized bed reactor discharges through the fourth pipeline and recovers the gas overflowing from the discharge tank during the discharge process through the fifth pipeline.

[0027] After the discharge operation is completed, the fourth and fifth pipelines are controlled to close, and the first, second and third pipelines are controlled to open, so that the injection device receives raw gas from the first gas source through the first pipeline, transports the raw gas to the fluidized bed reactor through the second pipeline, and pumps the discharge tank through the third pipeline to reduce the pressure of the discharge tank.

[0028] After the pressure value of the discharge tank drops to the preset first pressure threshold, the third pipeline is controlled to perform a closing operation, and the seventh and eighth pipelines are controlled to perform an opening operation, so that the conveying gas from the second gas source is input into the discharge tank through the seventh pipeline, and the material in the discharge tank is transferred to the downstream device through the eighth pipeline.

[0029] After the material transfer is completed, control the seventh and eighth pipelines to perform the closing operation, and control the sixth pipeline to perform the opening operation. Pressurize the discharge tank through the sixth pipeline until the pressure value of the discharge tank reaches the preset second pressure threshold, and control the sixth pipeline to perform the closing operation to wait for the next discharge.

[0030] Furthermore, the first pressure threshold is preset to be no greater than 1 MPa; the second pressure threshold is preset to be no less than 0.6 MPa.

[0031] Furthermore, before controlling the fourth and fifth pipelines to start when the preset discharge conditions are met, so that the fluidized bed reactor discharges material through the fourth pipeline and recovers the gas overflowing from the discharge tank during the discharge process through the fifth pipeline, the method further includes:

[0032] The pressure value of the discharge tank is controlled within the preset pressure range, and the pressure difference between the fluidized bed reactor and the discharge tank is controlled within the preset pressure difference range.

[0033] The present invention also provides a computer-readable storage medium storing a computer program that, when executed by one or more processors, implements the steps of the above-described method.

[0034] The present invention also provides an electronic device, including a memory and one or more processors, wherein a computer program is stored on the memory, and the memory and one or more processors are communicatively connected to each other, and when the computer program is executed by one or more processors, the steps of the above method are performed.

[0035] The fluidized bed reactor discharge system, method, and electronic equipment provided by this invention have at least the following beneficial effects:

[0036] (1) Set up a multi-functional discharge tank. The discharge tank has two functions: settling and transfer. It combines the settling container and the transfer container into one, which greatly simplifies the discharge process, significantly improves the discharge rate of the fluidized bed in the process, reduces the use of control valves, and reduces the probability of failure.

[0037] (2) Introduce raw material gas (high-pressure ethylene gas) into the injection device, and depressurize the discharge tank by drawing gas from the discharge tank. After the discharge tank is vented, the pressure can be reduced to below 0.01 MPa. Operate under slightly positive or negative pressure to maximize the flash evaporation of low molecular weight compounds adsorbed in the polymer, while reducing the amount of gas entering the downstream system to a low level. The remaining solid material directly enters the downstream device (degassing chamber) from the discharge tank, eliminating the transfer container in the original discharge system, reducing the path of low molecular weight compounds circulating in the system, avoiding the introduction of impurities, reducing raw material consumption, reducing the devolatilization and recovery load of the downstream system, and helping to improve product quality.

[0038] (3) A branch line (sixth line) is drawn from the circulating pipeline of the fluidized bed reactor and connected to the first air inlet of the discharge tank. The circulating gas in the circulating pipeline of the fluidized bed reactor is used to pressurize the discharge tank after the material is transferred, reducing the pipeline oscillation during the subsequent discharge process. At the same time, the circulating gas flow rate can be adjusted to form a sufficient pressure difference between the fluidized bed reactor and the discharge tank, allowing the fluidized bed to discharge material at a high level, reducing the liquid content in the discharged material, and ensuring the high discharge efficiency and quality of the fluidized bed reactor in the gas phase polyethylene condensation process.

[0039] (4) The material discharged from the discharge tank has a lower liquid content, which can reduce the burden on downstream equipment (degassing chamber) and reduce energy consumption. After the material in the discharge tank is transferred to the downstream equipment, the discharge tank is pressurized by circulating gas, which improves the recycling value of the circulating gas. The elimination of the transfer container reduces equipment costs, the simplified operation process reduces operating costs, and the shortened production cycle also increases the production capacity per unit time, resulting in a significant improvement in the overall economic benefits of the process. Attached Figure Description

[0040] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0041] Figure 1 This is a schematic diagram of the fluidized bed reactor discharge system provided in one embodiment of the present invention;

[0042] Figure 2 This is a schematic diagram of the fluidized bed reactor discharge system provided in another embodiment of the present invention;

[0043] Figure 3 This is a schematic diagram of the structure of a spraying device provided in an embodiment of the present invention;

[0044] Figure 4 for Figure 3 A schematic diagram of the nozzle structure in the diagram;

[0045] Figure 5 This is a flowchart of the discharging method for a fluidized bed reactor provided in one embodiment of the present invention;

[0046] Figure 6 This is a schematic diagram of an electronic device structure provided in one embodiment of the present invention;

[0047] Figure label:

[0048] Figures 1 to 2In the middle: 1-Injection device, 2-Discharge tank, 3-Fluidized bed reactor, 4-First control valve, 5-Second control valve, 6-Third control valve, 7-Fourth control valve, 8-Fifth control valve, 9-Sixth control valve, 10-Seventh control valve, 11-Eighth control valve, 12-Ninth control valve, 13-Tenth control valve, 14-Eleventh control valve, 15-Raw gas compressor, 16-Circulating gas compressor, 17-Circulating gas condenser;

[0049] Figure 3 In the middle: 20-receiving chamber, 21-nozzle, 22-mixing chamber, 23-diffuser, 24-working fluid, 25-ejector fluid;

[0050] Figure 6 In Chinese: 600-Electronic device, 601-Processor, 602-Communication bus, 603-User interface, 604-Communication interface, 605-Memory. Detailed Implementation

[0051] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of the present invention, and not all of them. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of the present invention. The terms "first," "second," "third," "fourth," "fifth," "sixth," "seventh," "eighth," "ninth," "tenth," and "eleventh" used in the claims and specification of the present invention are for ease of distinction only, have no special meaning, and are not intended to limit the present invention.

[0052] In one embodiment of the present invention, a fluidized bed reactor discharge system is provided, such as... Figure 1 As shown, the system includes:

[0053] The injection device 1 is used to deliver raw material gas to the fluidized bed reactor and perform suction operation on the discharge tank. The air inlet of the injection device 1 is connected to the first gas source through the first pipeline a, the air outlet of the injection device 1 is connected to the air inlet of the fluidized bed reactor 3 through the second pipeline b, and the ejector port of the injection device 1 is connected to the first exhaust port of the discharge tank 2 through the third pipeline c.

[0054] The discharge tank 2 is used to receive the material discharged from the fluidized bed reactor and transfer the material to the downstream device. The inlet of the discharge tank 2 is connected to the outlet of the fluidized bed reactor 3 through the fourth pipeline d. The second exhaust port of the discharge tank 2 is connected to the air inlet of the fluidized bed reactor 3 through the fifth pipeline e. The first air inlet of the discharge tank 2 is connected to the circulation pipeline of the fluidized bed reactor through the sixth pipeline f. The second air inlet of the discharge tank 2 is connected to the second air source through the seventh pipeline g. The discharge port of the discharge tank 2 is connected to the downstream device through the eighth pipeline h.

[0055] Among them, the spray device 1 can be selected Figure 3 The nozzle of the spray device 1 shown can be selected from the spray device shown. Figure 4 The nozzle shown.

[0056] Specifically, a first gas source provides raw material gas, which is continuously transported to the injection device 1 through the first pipeline a, so that the injection device 1 can operate continuously. In one implementation, the raw material gas is ethylene gas. The ethylene gas provided by the first gas source is first compressed and pressurized by the raw material gas compressor 15 to obtain high-pressure ethylene gas, and then transported to the injection device 1 through the first pipeline a. The high-pressure ethylene gas can specifically be ethylene gas with a pressure greater than or equal to 5 MPa. A second gas source provides conveying gas, which enters the discharge tank 2 through the seventh pipeline g, thereby realizing the transfer of materials in the discharge tank 2 to downstream devices using the conveying gas. In one implementation, the second gas source uses an exhaust gas recovery system to provide conveying gas, and the conveying gas is selected from the PDS conveying gas from the exhaust gas recovery system. The fluidized bed reactor circulation pipeline is the circulation pipeline in the fluidized bed reaction system, wherein the fluidized bed reaction system includes a fluidized bed reactor 3, a circulating gas compressor 16, and a circulating gas condenser 17, which are connected in sequence to form a circulating gas loop. The pipeline in the circulating gas loop is the circulation pipeline in the fluidized bed reaction system. Further, see Figure 1 or Figure 2 The sixth pipeline f connects to the pipeline between the circulating gas compressor 16 and the circulating gas condenser 17, thereby receiving the circulating gas compressed by the circulating gas compressor 16. The downstream device is a degassing chamber.

[0057] More specifically, each pipeline is equipped with a control valve for controlling the opening and closing of the pipeline. Specifically, a first control valve 4 is installed on the first pipeline a, a second control valve 5 is installed on the second pipeline b, a third control valve 6 is installed on the third pipeline c, a fourth control valve 7 is installed on the fourth pipeline d, a fifth control valve 8 is installed on the fifth pipeline e, a sixth control valve 9 is installed on the sixth pipeline f, a seventh control valve 10 is installed on the seventh pipeline g, and an eighth control valve 11 is installed on the eighth pipeline h.

[0058] In this embodiment, the opening and closing of the control pipeline is achieved by opening and closing the control valve on the control pipeline.

[0059] In one implementation of this embodiment, the first control valve 4, in addition to controlling the opening and closing of the first pipeline a, can also control the gas flow rate of the raw material gas entering the injection device 1 from the first gas source; the third control valve 6, in addition to controlling the opening and closing of the third pipeline c, is also used to control the gas flow rate for drawing residual gas from the discharge tank 2 to the injection device 1; the fourth control valve 7, in addition to controlling the opening and closing of the fourth pipeline d, is also used to control the material flow rate; the sixth control valve 9, in addition to controlling the opening and closing of the sixth pipeline f, is also used to control the flow rate of the circulating gas entering the discharge tank 2 from the fluidized bed reactor circulation pipeline; and the seventh control valve 10, in addition to controlling the opening and closing of the seventh pipeline g, is also used to control the flow rate of the conveying gas.

[0060] The discharge method using the fluidized bed reactor discharge system provided in this embodiment is as follows:

[0061] (1) Control the third pipeline c, the fourth pipeline d, the fifth pipeline e, the sixth pipeline f, the seventh pipeline g, and the eighth pipeline h to perform a shutdown operation.

[0062] (2) When the preset discharge conditions are met, control the fourth pipeline d and the fifth pipeline e to perform the opening operation so that the fluidized bed reactor 3 discharges through the fourth pipeline d and recovers the gas overflowing from the discharge tank 2 during the discharge process through the fifth pipeline e.

[0063] Specifically, the preset discharge conditions are set in advance by those skilled in the art, and the present invention does not limit this. In one implementation, the preset discharge conditions are that the bed level and / or weight in the fluidized bed reactor reach a set value.

[0064] After the fourth pipeline d is opened, under the action of pressure difference and gravity, the material in the fluidized bed reactor 3 is discharged from the outlet of the fluidized bed reactor 3 into the discharge tank 2 through the fourth pipeline d. As the material enters the discharge tank 2, a large amount of raw material gas or gas / liquid mixture is carried between solid particles and in the gaps. During the material discharge process, some gas is released from the material and returned to the fluidized bed reactor 3 through the fifth pipeline e.

[0065] (3) After the discharge operation is completed, control the fourth pipeline d and the fifth pipeline e to perform the closing operation, and control the first pipeline a, the second pipeline b and the third pipeline c to perform the opening operation, so that the injection device 1 receives the raw material gas from the first gas source through the first pipeline a, transports the raw material gas to the fluidized bed reactor 3 through the second pipeline b, and sucks the discharge tank 2 through the third pipeline c to reduce the pressure of the discharge tank.

[0066] Specifically, the discharge operation is completed when the material no longer transfers from the fluidized bed reactor 3 to the discharge tank 2, and an equilibrium is reached between the two. After the discharge operation is completed, the material in the discharge tank 2 still carries a large amount of raw material gas or gas / liquid mixture. By controlling the opening operation of the third pipeline c, the discharge tank 2 is evacuated, causing the pressure in the discharge tank 2 to be reduced. The gas released during the pressure reduction process is recovered to the injection device 1 through the third pipeline e, and together with the raw material gas received by the injection device 1, it is input into the fluidized bed reactor 3, thereby further realizing the recovery and utilization of unreacted raw material gas.

[0067] (4) After the pressure value of the discharge tank 2 drops to the preset first pressure threshold, control the third pipeline c to perform the closing operation, and control the seventh pipeline g and the eighth pipeline h to perform the opening operation, so that the conveying gas from the second gas source is input to the discharge tank 2 through the seventh pipeline g, and the material in the discharge tank 2 is transferred to the downstream device through the eighth pipeline h.

[0068] Furthermore, through high-frequency, pulsed discharge, the aggregated product material can be continuously and stably transferred into downstream devices.

[0069] (5) After the material transfer is completed, control the seventh pipeline g and the eighth pipeline h to perform the closing operation, control the sixth pipeline f to perform the opening operation, pressurize the discharge tank 2 through the sixth pipeline f until the pressure value of the discharge tank 2 reaches the preset second pressure threshold, so as to control the sixth pipeline f to perform the closing operation, and wait for the next discharge.

[0070] After the material transfer is completed, the pressure of discharge tank 2 returns to normal pressure due to the connection with the outside world, while the pressure in fluidized bed reactor 3 is 2.0-2.4 MPa. After shutting off the eighth pipeline h, circulating gas is introduced into discharge tank 2 to raise the pressure of discharge tank 2 to 1.0-1.1 MPa. This provides an appropriate pressure difference between fluidized bed reactor 3 and discharge tank 2 for the next material discharge, ensuring that the material discharged from the reactor can enter discharge tank 2 under a sufficient pressure difference, and also preventing the pipeline from oscillating violently due to excessive pressure difference.

[0071] Specifically, the first pressure threshold and the second pressure threshold can be set by those skilled in the art according to actual needs, and the present invention does not impose any restrictions on this. The first pressure threshold is preferably a value not greater than 1 MPa, more preferably a value not greater than 0.5 MPa, even more preferably a value not greater than 0.1 MPa, and even more preferably a value not greater than 0.01 MPa; the second pressure threshold is preferably a value not less than 0.6 MPa.

[0072] In one implementation, during discharge, the flow rate of the raw material gas entering the injection device 1 is adjusted to 5t / h to 15t / h. The pressure of the discharge tank 2 is reduced from 1.1MPa to 0.6MPa to 0.7MPa by suction. After suction, the material in the discharge tank 2 is transferred to the downstream device by the second gas source. After the transfer is completed, the pressure of the discharge tank 2 returns to normal pressure. The flow rate of the circulating gas in the sixth pipeline f is adjusted to 5t / h to 15t / h to increase the pressure of the discharge tank 2 to 1.0MPa to 1.1MPa.

[0073] The fluidized bed reactor discharge system provided in this embodiment features a multi-functional discharge tank that combines settling and transfer functions into one, significantly simplifying the discharge process, greatly improving the discharge rate of the fluidized bed, reducing the use of control valves, and lowering the probability of failure. Raw material gas (high-pressure ethylene gas) is introduced into the injection device, and the gas in the discharge tank is drawn in to depressurize the tank. After venting, the pressure in the discharge tank can be reduced to below 0.01 MPa. Operating under slightly positive or negative pressure maximizes the flash evaporation of low-molecular-weight compounds adsorbed in the polymer, while simultaneously reducing the amount of gas entering the downstream system to a low level. The remaining solid material directly enters the downstream unit (degassing chamber) from the discharge tank, eliminating the need for the transfer container in the original discharge system, reducing the path of low-molecular-weight compounds circulating within the system, avoiding the introduction of impurities, reducing raw material consumption, alleviating the devolatilization and recovery load of the downstream system, and contributing to improved product quality. A branch line (sixth line) is drawn from the fluidized bed reactor's circulation pipeline and connected to the first air inlet of the discharge tank. The circulating gas from the fluidized bed reactor's circulation pipeline pressurizes the discharge tank after the material has been transferred, reducing pipeline oscillation during subsequent discharge. Simultaneously, the circulating gas flow rate can be adjusted to create a sufficient pressure difference between the fluidized bed reactor and the discharge tank, allowing for high-level discharge from the fluidized bed and reducing the liquid content in the discharged material. This ensures high discharge efficiency and quality of the fluidized bed reactor in the gas-phase polyethylene condensation process. The lower liquid content of the discharged material reduces the burden on downstream units (degassing chambers) and lowers energy consumption. After the material in the discharge tank is transferred to downstream units, the discharge tank is pressurized using circulating gas, enhancing the recycling value of the circulating gas. The elimination of the transfer container reduces equipment costs, the simplified operation process reduces operating costs, and the shortened production cycle increases the capacity per unit time, resulting in a significant improvement in the overall economic benefits of the process.

[0074] In another embodiment of the invention, such as Figure 4 As shown, the system also includes:

[0075] The outlet of the first gas purging line i is connected to the inlet of the first gas purging line on the fourth line d.

[0076] The outlet of the second gas purging line j is connected to the inlet of the second gas purging line on the fifth line e.

[0077] The outlet of the third gas purging line k is connected to the inlet of the third gas purging line on the second line b.

[0078] Furthermore, each gas purging line is equipped with a control valve for controlling the opening and closing of the gas purging line. The purging is achieved by controlling the opening or closing of the purging line through the control valve.

[0079] A ninth control valve 12 is installed on the first gas purging line i, a tenth control valve 13 is installed on the second gas purging line j, and an eleventh control valve 14 is installed on the third gas purging line k.

[0080] Furthermore, the first gas purge line inlet is located at a predetermined position between the fluidized bed reactor 3 and the fourth control valve 7; the second gas purge line inlet is located at a predetermined position between the fluidized bed reactor 3 and the fifth control valve 8; and the third gas purge line inlet is located at a predetermined position between the fluidized bed reactor 3 and the second control valve 5. These predetermined positions can be adjusted by those skilled in the art according to actual needs, and this invention does not impose any limitations on this.

[0081] In this embodiment, by setting a first gas purging pipeline, a second gas purging pipeline, and a third gas purging pipeline in the system, it is possible to achieve the following steps: using clean gas to purge residual material from the discharge pipeline (fourth pipeline), using clean gas to purge residual gas from the exhaust pipeline (second and fifth pipelines), using dry gas to purge the discharge tank, and using dry gas to purge the transfer pipeline (eighth pipeline), thereby preventing the polymer remaining in the pipeline from melting and plasticizing.

[0082] In another embodiment of the present invention, the system further includes:

[0083] A gas filter is installed at the top of the discharge tank, and the third pipeline c is connected to the first exhaust port of the discharge tank 2 through the gas filter.

[0084] Furthermore, the sixth pipeline f is connected to the first air inlet of the discharge tank 2 via a gas filter. When the sixth pipeline f is connected to the first air inlet of the discharge tank 2 via the gas filter, and the discharge tank is pressurized through the sixth pipeline f, the circulating gas first passes through the gas filter before entering the discharge tank, thus achieving backflushing of the gas filter during the pressurization process. In this case, the first air inlet and the first exhaust port are actually the same port.

[0085] In another embodiment of the present invention, the discharge tank 2 is provided with a material level detection instrument, a temperature detection instrument and a pressure detection instrument to monitor the material level, temperature and pressure of the discharge tank 2.

[0086] Furthermore, the system can also be equipped with monitoring devices to detect abnormal conditions, such as instruments and equipment for detecting pressure, flow rate, temperature, liquid level, material level, container stress, valve position or regulator position, and corresponding automatic control systems.

[0087] In another embodiment of the present invention, the solid material discharged in a single discharge process generally fills at least 80% of the volume of the discharge tank 2. A solid monitoring device (e.g., a material level detection instrument) can be installed in the discharge tank 2 to detect whether the solid material in the discharge tank has reached 80% of the volume of the discharge tank 2.

[0088] In another embodiment of the invention, such as Figure 5 As shown, a fluidized bed reactor discharge method is provided. This method is based on the fluidized bed reactor discharge system in the above embodiment, and specifically includes the following steps:

[0089] Step S501: Control the third, fourth, fifth, sixth, seventh, and eighth pipelines to perform a shutdown operation.

[0090] Step S502: When the preset discharge conditions are met, control the fourth and fifth pipelines to start, so that the fluidized bed reactor discharges through the fourth pipeline and recovers the gas overflowing from the discharge tank during the discharge process through the fifth pipeline.

[0091] Step S503: After the discharge operation is completed, control the fourth and fifth pipelines to perform the closing operation, and control the first, second and third pipelines to perform the opening operation, so that the injection device receives the raw material gas from the first gas source through the first pipeline, transports the raw material gas to the fluidized bed reactor through the second pipeline, and pumps the discharge tank through the third pipeline to reduce the pressure of the discharge tank.

[0092] Step S504: After the pressure value of the discharge tank drops to the preset first pressure threshold, control the third pipeline to perform a closing operation, and control the seventh and eighth pipelines to perform an opening operation, so that the conveying gas from the second gas source is input into the discharge tank through the seventh pipeline, and the material in the discharge tank is transferred to the downstream device through the eighth pipeline.

[0093] Step S505: After the material transfer is completed, control the seventh and eighth pipelines to perform the closing operation, control the sixth pipeline to perform the opening operation, pressurize the discharge tank through the sixth pipeline until the pressure value of the discharge tank reaches the preset second pressure threshold, and control the sixth pipeline to perform the closing operation to wait for the next discharge.

[0094] The first pressure threshold and the second pressure threshold can be set by those skilled in the art according to actual needs, and the present invention does not impose any restrictions on them.

[0095] The first pressure threshold is preferably no greater than 1 MPa, more preferably no greater than 0.5 MPa, even more preferably no greater than 0.1 MPa, and even more preferably no greater than 0.01 MPa; the second pressure threshold is preferably no less than 0.6 MPa.

[0096] In another embodiment of the present invention, before step S502, the fluidized bed reactor discharge method further includes controlling the pressure value of the discharge tank within a preset pressure range and controlling the pressure difference between the fluidized bed reactor and the discharge tank within a preset pressure difference range.

[0097] Adjust the pressure value of the discharge tank to the preset pressure range, and adjust the pressure difference between the fluidized bed reactor and the discharge tank to the preset pressure difference range, so that the fluidized bed reactor can discharge to the discharge tank under the action of pressure difference.

[0098] The pressure range and pressure difference range can be set by those skilled in the art according to actual needs, and this invention does not impose any restrictions on them. The preferred pressure range is not less than 0.6 MPa.

[0099] The pressure difference range is preferably no more than 1.5 MPa, more preferably no more than 1.2 MPa, and even more preferably no more than 1.0 MPa.

[0100] The fluidized bed reactor discharge method provided in this embodiment is based on the fluidized bed reactor discharge system provided in the above embodiments. It significantly simplifies the discharge process, significantly improves the discharge rate of the fluidized bed in the process, reduces the use of control valves, and lowers the probability of failure. By introducing raw material gas (high-pressure ethylene gas) into the injection device, the gas in the discharge tank is drawn to reduce the pressure of the discharge tank. After the discharge tank is vented, the pressure can be reduced to below 0.01 MPa. Operating under slightly positive or negative pressure maximizes the flash evaporation of low molecular weight compounds adsorbed in the polymer, while reducing the amount of gas entering the downstream system to a low level. The remaining solid material directly enters the downstream device (degassing chamber) from the discharge tank, eliminating the transfer container in the original discharge system, reducing the path of low molecular weight compounds circulating in the system, avoiding the introduction of impurities, reducing raw material consumption, and alleviating the devolatilization and recovery load of the downstream system, which helps to improve product quality. Furthermore, a branch line (sixth line) is drawn from the fluidized bed reactor's circulating pipeline to pressurize the discharge tank after material transfer using circulating gas. This reduces pipeline oscillation during subsequent suction processes and allows for adjustment of the circulating gas flow rate, creating a sufficient pressure difference between the fluidized bed reactor and the discharge tank. This allows for high-level discharge from the fluidized bed, reducing the liquid content in the discharged material and ensuring high discharge efficiency and quality of the fluidized bed reactor in the gas-phase polyethylene condensation process. The material discharged from the discharge tank has a lower liquid content, reducing the burden on downstream units (degassing chambers) and lowering energy consumption. After the material in the discharge tank is transferred to downstream units, the discharge tank is pressurized using circulating gas, enhancing the recycling value of the circulating gas. The elimination of the transfer container reduces equipment costs, the simplified operation process reduces operating costs, and the shortened production cycle increases the capacity per unit time, resulting in a significant improvement in the overall economic benefits of the process.

[0101] To more clearly illustrate the advantages of the material feeding system provided by this invention compared to existing material feeding systems, specific examples are given below:

[0102] 1. Comparative Example (using existing material feeding systems and methods)

[0103] Taking a gas-phase fluidized bed process unit with an annual production capacity of 300,000 tons of linear low-density polyethylene (LLDPE) as an example, the production of conventional single-peak LLDPE film products involves approximately 25 discharges per hour, with a fluidized bed inlet temperature of approximately 49°C and a discharge temperature of approximately 60–65°C. The discharge system is located on a single-phase fluidized bed reaction system, which includes a circulating gas loop consisting of a gas-phase fluidized bed reactor, a circulating gas compressor, and a circulating gas condenser connected in sequence. It also includes a catalyst feeding system and various raw material feeding systems. From the bottom to the top of the fluidized bed reactor, the concentration of the raw material gas decreases sequentially. A portion of the raw material gas undergoes polymerization in the bottom of the reactor, while unreacted and incompletely polymerized particles continue to polymerize in the upper part of the gas-phase fluidized bed reactor with the rising raw material gas flow. Some unreacted raw material gas is discharged from the top of the fluidized bed reactor and recycled along with the raw material gas, forming a circulating gas loop. The discharge port is located on the gas-phase fluidized bed reactor. The discharge system and method described in patent application CN200780037815.5, filed on September 10, 2007, include a settling container and a transfer container. The settling container's inlet is connected to the discharge port of a single-phase fluidized bed reactor, the bottom of the settling container is connected to the inlet of the transfer container, the bottom of the transfer container is connected to a downstream degassing chamber, and the tops of both the settling container and the transfer container are connected to the single-phase fluidized bed reactor. Traditional fluidized bed reactors use a discharge port 0.3m above the fluidized bed distribution plate at the bottom of the fluidized bed. The discharge system begins discharging after the polymerization reaction has progressed to a certain stage. However, because the fluidized bed reactor has a bottom feed, a significant amount of unreacted material is carried away during the bottom discharge process. The operating pressure of the gas-phase fluidized bed reactor is approximately 2.0 to 2.3 MPa, the operating pressure of the settling container is approximately 1.1 to 1.2 MPa, and the operating pressure of the transfer container is approximately 0.5 to 0.6 MPa. Each discharge contains approximately 35 wt% to 38 wt% gas (mainly ethylene, hydrogen, nitrogen, etc.) and approximately 200 to 250 kg / m³ of dissolved liquid hydrocarbons (mainly comonomers and refrigerants). 3 .

[0104] 2. Example 1 (Discharge using the fluidized bed reactor discharge system and method provided by this invention)

[0105] Taking a gas-phase fluidized bed process unit with an annual production capacity of 300,000 tons of linear low-density polyethylene (LLDPE) as an example, for the production of conventional LLDPE film products, the upper bed temperature of the fluidized bed reactor is approximately 88°C, and the pressure is approximately 2.3 MPa. A condensate solution with a content of approximately 5 wt% is introduced into the lower part of the fluidized bed reactor. The reactor discharges approximately 25 times per hour. The fluidized bed inlet temperature is approximately 49°C, and the discharge temperature is approximately 60–65°C. The discharge system is located on the side wall of the gas-phase fluidized bed reactor. The gas-phase fluidized bed reaction system includes a circulating gas loop consisting of a gas-phase fluidized bed reactor, a circulating gas compressor, and a circulating gas condenser connected in sequence. It also includes a catalyst feeding system and various raw material feeding systems. From the bottom to the top of the fluidized bed reactor, the concentration of the feed gas decreases sequentially. A portion of the feed gas undergoes polymerization in the bottom of the reactor, while unreacted and fully polymerized particles continue to polymerize in the top of the gas-phase fluidized bed reactor along with the rising feed gas stream. Some unreacted feed gas is discharged from the top of the fluidized bed reactor and recycled together with the feed gas to form a circulating gas loop. The discharge port is located on the gas-phase fluidized bed reactor.

[0106] This example uses the fluidized bed reactor discharge system provided by this invention. The structure of the fluidized bed reactor discharge system is described in [reference needed]. Figure 1 , Figure 2 As described above, I will not repeat myself here.

[0107] The discharge tank operates intermittently, while the spraying device operates continuously. The specific discharge method is as follows:

[0108] (1) Control the third pipeline c, the fourth pipeline d, the fifth pipeline e, the sixth pipeline f, the seventh pipeline g, and the eighth pipeline h to perform a shutdown operation.

[0109] Specifically, the control valves on the third, fourth, fifth, sixth, seventh, and eighth pipelines are all closed, thereby controlling the third, fourth, fifth, sixth, seventh, and eighth pipelines to perform a shut-off operation.

[0110] (2) Confirm that the pressure in the discharge tank is within the preset pressure range, and the pressure difference between the fluidized bed reactor and the discharge tank is within the preset pressure difference range. In this example, the pressure range is not less than 0.6 MPa. The preset pressure difference range is not greater than 1.2 MPa.

[0111] (3) When the material level and bed weight reach the set values, control the fourth and fifth pipelines to open (specifically by opening the fourth and fifth control valves). Under the action of gravity and differential pressure, the material is discharged from the fourth pipeline into the discharge tank, with an average discharge flow rate of 37.5 t / hr for LLDPE powder. When the material no longer transfers from the fluidized bed reactor to the discharge tank, a balance is formed between the two, and the discharge is completed. At this time, the pressure in the discharge tank is approximately 2.3 MPa. 80% of the solid material in the discharge tank is discharged in one discharge process. The discharge time is generally less than 60 seconds.

[0112] (4) Control the fourth and fifth pipelines to perform a shut-off operation, and control the first pipeline a, the second pipeline b, and the third pipeline to perform an open operation (achieved by closing the fourth and fifth control valves and opening the first, second, and third control valves), so that the injection device 1 receives the raw material gas from the first gas source through the first pipeline a, and transports the raw material gas to the fluidized bed reactor 3 through the second pipeline b, and evacuates the discharge tank, further reducing the pressure in the discharge tank to a first specified value, which in this example is 0.25 MPa. The gas released by depressurization enters the injection device through the third pipeline and is carried back to the fluidized bed reactor by the high-pressure raw material gas.

[0113] In this example, the feed gas is 5.0 MPa ethylene feed gas. The first gas source continuously supplies feed gas to the injection device 1 to ensure continuous operation of the injection device.

[0114] (5) After the suction is completed, control the third pipeline to perform the closing operation, and control the seventh and eighth pipelines to perform the opening operation (by closing the third control valve and opening the eighth and seventh control valves). Use the conveying gas to transfer the material in the discharge tank to the downstream degassing chamber. The conveying gas is PDS conveying gas from the exhaust gas recovery system.

[0115] (6) After the transfer is completed, control the seventh and eighth pipelines to perform the closing operation, and control the sixth pipeline to perform the opening operation (by closing the eighth and seventh control valves and opening the sixth control valve). Use the circulating gas from the fluidized bed reactor circulation pipeline to pressurize the discharge tank, and at the same time backflush the first and second filters above the discharge tank to increase the pressure of the discharge tank to the second specified value. In this example, the second specified value is 1.15 MPa.

[0116] (7) After pressurization is completed, control the sixth pipeline to perform a shut-off operation (by closing the sixth control valve), and the discharge tank returns to its initial state. This completes one discharge process and waits for the next discharge.

[0117] After adopting the above operating steps, the gas content in each discharge is approximately 18 wt% (mainly composed of ethylene, hydrogen, nitrogen, etc.), and the dissolved liquid hydrocarbon content (mainly composed of comonomers and refrigerants) is approximately 180 kg / m³. 3 .

[0118] 3. Example 2 (Discharging material using the fluidized bed reactor discharge system and method provided by this invention)

[0119] Taking a gas-phase fluidized bed process unit with an annual production capacity of 300,000 tons of linear low-density polyethylene (LLDPE) as an example, for the production of conventional LLDPE film products, the upper bed temperature of the fluidized bed reactor is approximately 88°C, the pressure is approximately 2.3 MPa, and condensate is introduced into the lower part of the fluidized bed reactor with a condensate content of approximately 5 wt%. The reactor discharges approximately 25 times per hour, the fluidized bed inlet temperature is approximately 49°C, and the discharge temperature is approximately 60–65°C. The discharge system is located on the side wall of the gas-phase fluidized bed reactor. The gas-phase fluidized bed reaction system includes a circulating gas loop consisting of a gas-phase fluidized bed reactor, a circulating gas compressor, and a circulating gas cooler connected in sequence, as well as a catalyst feeding system and various raw material feeding systems. From the bottom to the top of the fluidized bed reactor, the concentration of the feed gas decreases sequentially. A portion of the feed gas undergoes polymerization in the bottom of the reactor, while unreacted and fully polymerized particles continue to polymerize in the top of the gas-phase fluidized bed reactor along with the rising feed gas stream. Some unreacted feed gas is discharged from the top of the fluidized bed reactor and recycled together with the feed gas to form a circulating gas loop. The discharge port is located on the gas-phase fluidized bed reactor.

[0120] The fluidized bed reactor discharge system is the same as in Example 1, see [link / reference]. Figure 1 , Figure 2 As described above, I will not repeat myself here.

[0121] The specific discharge method in Example 2 is the same as in Example 1. The difference between Example 2 and Example 1 is that the first specified value is set to 0.12 MPa. After adopting the above operating steps, the gas content in each discharge is approximately 6 wt% (mainly composed of ethylene, hydrogen, nitrogen, etc.), and the dissolved liquid hydrocarbon content (mainly composed of comonomers and refrigerant) is approximately 150 kg / m³. 3 .

[0122] As can be seen from Comparative Example 1, Example 1, and Example 2, using the fluidized bed reactor discharge system and method provided by the present invention for discharge can significantly reduce the gas content and liquid content in the discharged material.

[0123] In another embodiment of the present invention, a computer program product is also provided, which includes a computer program or instructions. When the computer program or instructions are executed by a processor, they implement all or part of the steps of the method in the above method embodiment. This embodiment will not be repeated here.

[0124] Furthermore, the computer program product may include one or more computer-executable components configured to perform embodiments when the program is run; the computer program product may also include a computer program tangibly contained on a readable medium thereof, the computer program containing program code for performing any of the methods in the embodiments of the present invention. In such embodiments, the computer program may be downloaded and installed from a network via a communication component, and / or installed from a removable medium.

[0125] In another embodiment of the present invention, a computer-readable storage medium is also provided, wherein a computer program stored in the computer-readable storage medium, when executed by one or more processors, implements all or part of the steps of the method in the above method embodiment. This embodiment will not be repeated here.

[0126] In another embodiment of the present invention, an electronic device 600 is also provided. Figure 6 This is a schematic diagram of the composition structure of an electronic device provided in an embodiment of the present invention, such as... Figure 6 As shown, the electronic device 600 includes: at least one processor 601, at least one communication bus 602, a user interface 603, at least one external communication interface 604, and a memory 605. The communication bus 602 is configured to enable communication between these components. The user interface 603 may include a display screen, and the external communication interface 604 may include standard wired and wireless interfaces. The memory 605 stores a computer program, and the memory 605 and one or more processors 601 are communicatively connected. When the computer program is executed by one or more processors, the processor 601 is configured to execute the computer program stored in the memory to implement all or part of the steps of the method in the above-described method embodiments, which will not be repeated here.

[0127] The fluidized bed reactor discharge system, method, and electronic equipment provided by this invention feature a multi-functional discharge tank that combines settling and transfer functions into one, significantly simplifying the discharge process, greatly improving the discharge rate of the fluidized bed, reducing the use of control valves, and lowering the probability of failure. Raw material gas (high-pressure ethylene gas) is introduced into the injection device, and the gas in the discharge tank is drawn in to depressurize the tank. After venting, the pressure in the discharge tank can be reduced to below 0.01 MPa. Operating under slightly positive or negative pressure maximizes the flash evaporation of low-molecular-weight compounds adsorbed in the polymer, while simultaneously reducing the amount of gas entering the downstream system to a low level. The remaining solid material directly enters the downstream device (degassing chamber) from the discharge tank, eliminating the need for a transfer container in the original discharge system, reducing the path of low-molecular-weight compounds circulating within the system, avoiding the introduction of impurities, reducing raw material consumption, alleviating the devolatilization and recovery load of the downstream system, and contributing to improved product quality. A branch line (sixth line) is drawn from the fluidized bed reactor's circulation pipeline and connected to the first air inlet of the discharge tank. The circulating gas from the fluidized bed reactor's circulation pipeline pressurizes the discharge tank after the material has been transferred, reducing pipeline oscillation during subsequent discharge. Simultaneously, the circulating gas flow rate can be adjusted to create a sufficient pressure difference between the fluidized bed reactor and the discharge tank, allowing for high-level discharge from the fluidized bed and reducing the liquid content in the discharged material. This ensures high discharge efficiency and quality of the fluidized bed reactor in the gas-phase polyethylene condensation process. The lower liquid content of the discharged material reduces the burden on downstream units (degassing chambers) and lowers energy consumption. After the material in the discharge tank is transferred to downstream units, the discharge tank is pressurized using circulating gas, enhancing the recycling value of the circulating gas. The elimination of the transfer container reduces equipment costs, the simplified operation process reduces operating costs, and the shortened production cycle increases the capacity per unit time, resulting in a significant improvement in the overall economic benefits of the process.

[0128] The various embodiments in this invention are described in a progressive manner. For the same or similar parts between the various embodiments, please refer to each other. Each embodiment focuses on describing the differences from other embodiments.

[0129] The scope of protection of this invention is not limited to the embodiments described above. Obviously, those skilled in the art can make various modifications and variations to this invention without departing from its scope and spirit. If these modifications and variations fall within the scope of the claims of this invention and their equivalents, then the intent of this invention also includes these modifications and variations.

Claims

1. A fluidized bed reactor discharge system for use in a fluidized bed reaction system, characterized by, The fluidized bed reaction system comprises a fluidized bed reactor, a circulating gas compressor, and a circulating gas condenser, which are sequentially connected to form a circulating gas loop; a pipeline in the circulating gas loop is a circulating pipeline in the fluidized bed reaction system; and the discharge system comprises: a jet device for delivering raw material gas to the fluidized bed reactor and performing a suction operation on the discharge tank; an air inlet of the jet device is connected to a first gas source through a first pipeline, an air outlet of the jet device is connected to an air inlet of the fluidized bed reactor through a second pipeline, and an entraining port of the jet device is connected to a first air outlet of the discharge tank through a third pipeline; a discharge tank for receiving materials discharged from the fluidized bed reactor and transferring the materials to a downstream device; a material inlet of the discharge tank is connected to a material outlet of the fluidized bed reactor through a fourth pipeline, a second air outlet of the discharge tank is connected to an air inlet of the fluidized bed reactor through a fifth pipeline, a first air inlet of the discharge tank is connected to the circulating pipeline of the fluidized bed reactor through a sixth pipeline, a second air inlet of the discharge tank is connected to a second gas source through a seventh pipeline, and a material outlet of the discharge tank is connected to the downstream device through an eighth pipeline; the sixth pipeline is connected to a pipeline between the circulating gas compressor and the circulating gas condenser, so as to receive the circulating gas compressed by the circulating gas compressor; a gas filter arranged on the top of the discharge tank, and the third pipeline is connected to the first air outlet of the discharge tank through the gas filter; wherein the first gas source provides raw material gas, and the second gas source provides conveying gas.

2. The discharge system of the fluidized bed reactor according to claim 1, wherein a control valve for controlling opening and closing of each pipeline is arranged on each pipeline; wherein a first control valve is arranged on the first pipeline, a second control valve is arranged on the second pipeline, a third control valve is arranged on the third pipeline, a fourth control valve is arranged on the fourth pipeline, a fifth control valve is arranged on the fifth pipeline, a sixth control valve is arranged on the sixth pipeline, a seventh control valve is arranged on the seventh pipeline, and an eighth control valve is arranged on the eighth pipeline.

3. The fluidized bed reactor discharge system of claim 2, wherein, The system further comprises: a first gas purging pipeline, an air outlet of the first gas purging pipeline being connected to a first gas purging pipeline inlet on the fourth pipeline; a second gas purging pipeline, an air outlet of the second gas purging pipeline being connected to a second gas purging pipeline inlet on the fifth pipeline; a third gas purging pipeline, an air outlet of the third gas purging pipeline being connected to a third gas purging pipeline inlet on the second pipeline.

4. The discharge system of the fluidized bed reactor according to claim 3, wherein a control valve for controlling opening and closing of each gas purging pipeline is arranged on each gas purging pipeline; wherein a ninth control valve is arranged on the first gas purging pipeline, a tenth control valve is arranged on the second gas purging pipeline, and an eleventh control valve is arranged on the third gas purging pipeline.

5. The fluidized bed reactor discharge system of claim 3, wherein, the first gas purge line inlet is located at a preset position between the fluidized bed reactor and the fourth control valve; the second gas purge line inlet is located at a preset position between the fluidized bed reactor and the fifth control valve; the third gas purge line inlet is located at a preset position between the fluidized bed reactor and the second control valve.

6. The fluidized bed reactor discharge system of claim 1, wherein, the sixth line is connected to the first gas inlet of the discharge tank through the gas filter.

7. A fluidized bed reactor discharge method characterized by, The method is implemented based on the system of any one of claims 1 to 6, and the method comprises: controlling the third line, the fourth line, the fifth line, the sixth line, the seventh line, and the eighth line to perform a closing operation; when a preset discharge condition is met, controlling the fourth line and the fifth line to perform an opening operation, so that the fluidized bed reactor discharges through the fourth line and recovers the gas overflowing from the discharge tank during the discharging process through the fifth line; after the discharging operation is completed, controlling the fourth line and the fifth line to perform a closing operation, and controlling the first line, the second line, and the third line to perform an opening operation, so that the injection device receives raw material gas from the first gas source through the first line, transports the raw material gas to the fluidized bed reactor through the second line, and performs suction on the discharge tank through the third line to reduce the pressure of the discharge tank; after the pressure value of the discharge tank is reduced to a preset first pressure threshold, controlling the third line to perform a closing operation, and controlling the seventh line and the eighth line to perform an opening operation, so that the conveying gas from the second gas source is input into the discharge tank through the seventh line, and the material in the discharge tank is transferred to a downstream device through the eighth line; after the material transfer is completed, controlling the seventh line and the eighth line to perform a closing operation, and controlling the sixth line to perform an opening operation, so that the discharge tank is pressurized through the sixth line until the pressure value of the discharge tank reaches a preset second pressure threshold, and the sixth line is controlled to perform a closing operation to wait for the next discharge.

8. The fluidized bed reactor discharge method of claim 7, wherein, The preset first pressure threshold is not greater than 1 MPag, and the second pressure threshold is not less than 0.6 MPag.

9. The fluidized bed reactor discharge method of claim 7, wherein, Before the step of controlling the fourth line and the fifth line to perform an opening operation when a preset discharge condition is met, so that the fluidized bed reactor discharges through the fourth line and recovers the gas overflowing from the discharge tank during the discharging process through the fifth line, the method further comprises: controlling the pressure value of the discharge tank to be within a preset pressure range, and controlling the pressure difference between the fluidized bed reactor and the discharge tank to be within a preset pressure difference range.

10. A computer-readable storage medium, characterized in that, The computer program stored in the computer readable storage medium, when executed by one or more processors, implements the steps of the method of any one of claims 7 to 9.

11. An electronic device, comprising: A computer program product comprising a computer readable medium, the computer readable medium having stored thereon the computer program of claim 10, wherein the computer program is loadable into an internal memory of a computer or a processor and / or implemented by the computer or the processor and thereby causes the computer or the processor to execute the steps of the method of any one of claims 7 to 9 when the computer program is carried out by the computer or the processor.

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