fluidized bed

It uses strong air volume to blow the fuel and fluidize it in the furnace for combustion.

I thought it was a fluidized bed reactor!

Go to the library and check it out. There will be very detailed information.~~

1. Process flow description 1. Process description This fluidized bed reactor is based on the HIMONT process bulk polymerization device and is used to produce high-impact copolymers. The dry homopolymer (polypropylene) with residual activity flows from the flash tank D-301 to the gas phase copolymerization reactor R-401 under the action of pressure difference. Under the control of a gas analyzer, hydrogen is added to the ethylene feed pipe to improve the intrinsic viscosity of the polymer to meet processing needs. The polymer enters the fluidized bed reactor from the top and falls onto the bed of the fluidized bed. The fluidizing gas (reaction monomer) enters the reactor through a specially designed grid. The polymer level is maintained by a control valve on the outlet line at the bottom of the reactor. The polymer material level determines the residence time and thus the degree of polymerization. In order to avoid excessive polymerization of scaly products from accumulating on the reactor wall, the reactor is equipped with a slowly rotating scraper to keep the reactor wall clean. The polymer fines entrained in the lower part of the grid are removed by a small cyclone separator S401 and sent to the downstream bag filter. All unreacted monomer is recycled back to the suction port of the fluidizing compressor. The recovered gas phase from the top of the ethylene stripper is combined with the recycled monomer at the gas phase reactor outlet, while supplementary hydrogen, ethylene and propylene are added to the compressor discharge port. The circulating gas is analyzed with an industrial chromatograph, and the supplementary amounts of hydrogen and propylene are adjusted. The additional propylene feed is then adjusted to ensure that the feed gas to the reactor meets the composition required by the process. Desalted water is used as the cooling medium, and a vertical tube-and-tube heat exchanger is used to remove the polymerization heat. This heat exchanger is located before the cycle gas compressor. The reaction pressure of the copolymer is about 1.4Mpa (table), 70°C. Note that the system pressure is between the flash tank pressure and the bag filter pressure, thus forming a certain pressure gradient in the entire polymer pipeline to avoid back-mixing of materials between containers and causing the polymer to flow forward. 2. Reaction mechanism: Ethylene, propylene and the reaction mixture react in a fluidized bed reactor at a certain temperature of 70 degrees and a certain pressure of 1.35Mpa through the initiation of a dry homopolymer (polypropylene) with residual activity. At the same time, hydrogen is added to improve the intrinsic viscosity of the copolymer and generate a high impact copolymer. main raw materials: Ethylene, propylene, dry homopolymer with residual activity (polypropylene), hydrogen. main product: High impact copolymer (copolymer with ethylene and propylene monomers). by-products: none. reaction equation: n C2H4 + n C3H6————→n. 3. Equipment list A401: Scraper C401 for R401: R401 circulation compressor E401: R401 gas cooler E409: Jacketed Water Heater P401: Turn on the heat pump R401: Copolymerization reactor S401: R401 cyclone separator 4. Parameter description AI40111: H2 content in reaction productAI40121: Content of C2H4 in the reaction productAI40131: Content of C2H6 in the reaction productAI40141: Content of C3H6 in the reaction productAI40151: Content of C3H8 in the reaction product 2. Operating procedures of the device 1. Cold start-up procedures This operating procedure is for reference only, and the detailed operation is subject to the scoring system. 1.1. Preparation for driving includes:: The system is pressurized with nitrogen and circulated to heat the nitrogen, and then the system is replaced with ethylene (according to actual normal operation, replacing the system with ethylene needs to be done twice, but considering the time relationship, it is only done once). After this process is completed, the system will be ready to start driving alone. 1.1.1. System nitrogen charging and heating (1) Nitrogen charging: Open the nitrogen charging valve and use nitrogen to pressurize the reactor system. When the system pressure reaches 0.7Mpa (meter), close the nitrogen charging valve. (2) When the nitrogen pressure reaches 0.1Mpa (table), follow the correct operating procedures, start the C401 copolymerization cycle gas compressor, and set the guide vane (HIC402) at 40% (3) Fill the ring pipe with liquid: After starting the compressor, open the water inlet valve V4030, fill the water tank with liquid, and open the nitrogen sealing valve V4031. (4) When the liquid level in the water tank is greater than 10%, open the pump P401 inlet valve V4032, start the pump P401, and adjust the pump outlet valve V4034 to 60% opening. (5) Manually open the low-pressure steam valve HC451, start the heat exchanger E-409, and heat the circulating nitrogen. (6) Open the circulating water valve V4035. (7) When the circulating nitrogen temperature reaches 70°C, TC451 turns on automatically and adjusts its setting value to maintain the nitrogen temperature TC401 at around 70°C. 1.1.2. Nitrogen circulation (1) When the reaction system pressure reaches 0.7Mpa, close the nitrogen filling valve. (2) Without stopping the compressor, use PIC402 and the discharge valve to relieve the pressure of the reaction system to 0.0Mpa (table). (3) During the nitrogen filling and pressure relief operation, continuously adjust the TC451 setting value to maintain the TC401 temperature at around 70°C. 1.1.3. Ethylene pressurization (1) When the system pressure drops to 0.0Mpa (table), close the discharge valve. (2) Start ethylene feeding from FC403. When the ethylene feeding amount is set at 567.0kg/hr, automatic adjustment is started. Ethylene will charge the system pressure to 0.25Mpa (table). 1.2. The dry operation start-up procedure aims to ensure that the coaggregation reaction system has a suitable monomer concentration before the polymer enters. In addition, through this step, the instrument can be operated and adjusted in advance under actual process conditions. 1.2.1. Reaction feed (1) When the ethylene pressure reaches 0.25Mpa (table), start the hydrogen feed valve FC402, set the hydrogen feed at 0.102kg/hr, and put FC402 into automatic control. (2) When the system pressure rises to 0.5Mpa (table), start the propylene feed valve FC404, set the propylene feed at 400kg/hr, and put FC404 into automatic control. (3) Open the feed valve V4010 from the ethylene stripper. (4) When the system pressure rises to 0.8Mpa (table), open the cyclone separator S-401 bottom valve HC403 to 20% opening to maintain the system pressure rising slowly. 1.2.2. Prepare to receive the homopolymer from D301 (1) Add propylene again, change FIC404 to manual, and adjust FV404 to 85%. (2) When AC402 and AC403 are stable, adjust the opening of HC403 to 25%. (3) Start the scraper of the copolymerization reactor and prepare to receive the homopolymer from the flash tank (D-301). 1.3. Start-up of the copolymerized reactant (1) Confirm that the system temperature TC451 is maintained at around 70 degrees. (2) When the system pressure rises to 1.2Mpa (table), increase the opening of HC403 to 40% and LV401 to 20-25% to maintain fluidization. (3) Open the polymer feed valve from D-301. (4) Stop the low-pressure heating steam and close HV451. 1.4. Transition to stable state 1.4.1. Reactor liquid level (1) As the R401 material level increases, the system temperature will increase. Reduce the set value of TC451 in time to continuously remove the reaction heat and maintain the TC401 temperature at around 70°C. (2) When the reaction system pressure is adjusted to 1.35Mpa (table), PC402 automatically controls. (3) Manually open LV401 to 30% to allow the copolymer to flow through the valve stably. (4) When the liquid level reaches 60%, set LC401 to automatic. (5) As the system pressure increases, the material level will slowly decrease, and the PC402 regulating valve will automatically open. In order to maintain the system pressure at 1.35Mpa, slowly increase the setting value of PC402 to 1.40Mpa (table). (6) After LC401 is put into automatic control at 60%, adjust the setting value of TC451. When TC401 stabilizes at about 70°C, TC401 and TC451 are controlled in cascade. 1.4.2. Reactor pressure and gas phase composition control (1) When the pressure and composition tend to be stable, put LC401 and PC403 into cascade. (2) FC404 and AC403 are connected in series. (3) FC402 and AC402 are connected in series. 2. Normal operating procedures and process parameters under normal working conditions: (1)FC402: Adjust the hydrogen feed amount (in series with AC402) to the normal value: 0.35kg/hr。 (2)FC403: Single loop adjustment of ethylene feed amount to normal value: 567.0kg/hr。 (3)FC404: Adjust the propylene feed amount (in series with AC403) to the normal value: 400.0kg/hr。 (4)PC402: Normal pressure value of single-circuit regulating system: 1.4Mpa。 (5)PC403: Normal value of main circuit regulating system pressure: 1.35Mpa。 (6)LC401: Reactor material level (cascade with PC403) normal value: 60%. (7)TC401: The main loop regulates the normal value of circulating gas temperature: 70℃. (8)TC451: Split-range adjustment to remove reaction heat (in series with TC401) normal value: 50℃. (9)AC402: The main loop adjusts the normal value of the H2/C2 ratio in the reaction product: 0.18. (10)AC403: The main loop adjusts the normal value of the ratio of C2/C3&C2 in the reaction product: 0.38. 3. Parking Operation Procedures This operating procedure is for reference only. Detailed operations are subject to the scoring system. Normal parking: 3.1. Lower the reactor material level (1) Close the catalyst feed valve TMP20. (2) Manually adjust the reactor material level slowly. 3.2. Turn off the ethylene feed and maintain pressure (1) When the reactor material level drops to 10%, turn off the ethylene feed. (2) When the reactor material level drops to 0%, close the reactor outlet valve. (3) Close the outlet valve on cyclone separator S-401. 3.3. Turn off propylene and hydrogen feed (1) Manually cut off the propylene feed valve. (2) Manually cut off the hydrogen feed valve. (3) Discharge pilot pressure to the torch. (4) Stop reactor scraper A401. 3.4. Nitrogen purge (1) Add nitrogen to the system. (2) Set off the torch when the pressure reaches 0.35Mpa. (3) Stop compressor C-401. 4. Instrument list Table number Description Type Normal value Range High limit Range low limit Engineering unit High report Low report High high report Low low report FC402 Hydrogen feed flow PID0.355.00.0Kg/h FC403 Ethylene feed flow PID567.01000.00.0Kg/h FC404 Propylene feed flow PID400.01000.0 0.0Kg/h PC402R-401 pressure PID1.403.00.0Mpa PC403R-401 pressure PID1.353.00.0Mpa LC401R-401 liquid level PID60.0100.00.0% TC401R-401 circulating gas temperature PID70.0150.00.0℃ FI401E-401 circulating water flow AI36.080.00.0T/h FI405R-401 gas phase feed flow AI120.0250.00.0T/h TI402 circulating gas E-401 inlet temperature AI 70.0 70. 0.0150.00.0℃ TI403E-401 outlet temperature AI65.0150.00.0℃ TI404R-401 inlet temperature AI75.0150.00.0℃ TI405/1E-401 inlet water temperature AI60.0150.00.0℃ TI405/2E-401 outlet water temperature AI70.0150.00.0℃ TI406E-401 outlet water temperature AI70.0150.00.0℃

There are many types of fluidized beds. For example, in catalysis, there are bubbling bed fluidization, turbulent bed fluidization, rapid bed fluidization, dense phase pneumatic conveying and dilute phase pneumatic conveying.