A continuous fischer-tropsch synthesis reactor and method

Abstract

The present disclosure relates to a continuous Fischer-Tropsch synthesis reactor and method, which adopts a partitioning baffle to reasonably partition a reaction chamber, so that the catalyst is sequentially reacted in a peripheral reaction chamber, a middle reaction chamber and an internal discharge chamber, and then the obtained deactivated catalyst is discharged from the continuous Fischer-Tropsch synthesis reactor through a deactivated catalyst discharge pipe. Compared with the existing process of intermittently discharging catalyst, the present disclosure can not only weaken the back mixing phenomenon of the catalyst, ensure that the catalyst activity of the Fischer-Tropsch synthesis reaction is always at a high level, and improve the reaction effect of the Fischer-Tropsch synthesis reaction, but also reduce the replacement amount of the catalyst and reduce the consumption of the catalyst. Moreover, the Fischer-Tropsch synthesis reaction performed by using the continuous Fischer-Tropsch synthesis reactor of the present disclosure can reduce the wear of the catalyst in the filtration process, reduce the number of built-in filters used, and thus reduce the operating pressure drop of the built-in filter and the solid content in the liquid wax.

Description

Technical Field

[0001] This disclosure relates to the field of Fischer-Tropsch synthesis reactions, and more specifically, to a continuous Fischer-Tropsch synthesis reactor and method. Background Technology

[0002] The Fischer-Tropsch synthesis reaction is a process in which syngas is converted into products such as hydrocarbons, oxygen-containing compounds, and syngas water under the action of a catalyst. Slurry-bed reactors, with their simple structure, strong heat transfer capacity, and convenient operation, are the mainstream Fischer-Tropsch synthesis reactors used in industry. Currently, low-temperature Fischer-Tropsch iron-based catalysts are widely used in industry. Their disadvantages include a relatively rapid catalyst deactivation rate, requiring periodic replacement of the deactivated catalyst; furthermore, low-temperature Fischer-Tropsch iron-based catalysts are prepared using a precipitation method, making them prone to breakage under industrial conditions.

[0003] CN201610990605.9 discloses a gas-liquid-solid multiphase flow reactor and its control system and method. By setting multiple filter assemblies within the reactor and matching control strategies, filters near the reactor wall employ reduced filtration time and increased backflushing frequency and waiting time to alleviate pore blockage. As the filter element moves closer to the reactor center, filtration time is increased and backflushing frequency is reduced to decrease waiting time, thereby improving filtration capacity and filter element lifespan. CN201910277874.4 discloses a slurry bed reactor and its application and Fischer-Tropsch synthesis method. Based on a traditional slurry bed reactor, multiple baffles are arranged along the axial direction of the reactor body from bottom to top on the inner wall of the reactor body. This improves reactor bed flow, effectively controls slurry flow velocity, reduces shear force generated by slurry mixing in the catalyst bed, reduces catalyst loss, and reduces mist entrainment in the foam layer, resulting in more stable reactor operation.

[0004] Although existing technologies can achieve Fischer-Tropsch synthesis, mixing activated and deactivated catalysts during the reaction makes it impossible to precisely remove deactivated catalyst from the Fischer-Tropsch reactor, leading to reduced reaction activity. Furthermore, existing Fischer-Tropsch reactors are prone to catalyst backmixing during the reaction, causing catalyst wear, further reducing reaction activity, and resulting in high solid content in the synthesized wax. Summary of the Invention

[0005] The purpose of this disclosure is to provide a continuous Fischer-Tropsch synthesis reactor and method to solve the problems in the prior art, such as the inability to accurately remove deactivated catalyst in the Fischer-Tropsch synthesis reactor, low activity of the Fischer-Tropsch synthesis reaction, and high solid content in the synthesized wax.

[0006] To achieve the above objectives, the first aspect of this disclosure provides a continuous Fischer-Tropsch synthesis reactor, which includes a shell and a partition, a gas distributor, an internal filter, a deactivated catalyst discharge pipe, and an activated catalyst feed ring pipe disposed in the internal chamber of the shell; the bottom of the shell is provided with a synthesis gas inlet, and the top of the shell is provided with a Fischer-Tropsch tail gas outlet; The deactivated catalyst discharge pipe is arranged axially within the shell, with its top end extending to the upper part of the shell and its bottom end extending to the outside of the shell to form a deactivated catalyst outlet. Furthermore, the sidewall of the deactivated catalyst discharge pipe is provided with multiple deactivated catalyst discharge ports, so that the deactivated catalyst can exit the continuous Fischer-Tropsch synthesis reactor sequentially through the deactivated catalyst discharge ports and the deactivated catalyst outlet. The gas distributor is located in the lower part of the internal cavity of the shell, and is used to divide the cavity between the shell and the deactivated catalyst discharge pipe into a reaction chamber and a synthesis gas chamber arranged vertically. The partition is arranged axially along the shell within the reaction chamber; the partition includes an inner annular partition and an outer annular partition, the inner annular partition being disposed inside the outer annular partition; an internal discharge chamber is formed between the inner wall of the inner annular partition and the outer wall of the deactivated catalyst discharge pipe, an intermediate reaction chamber is formed between the outer wall of the inner annular partition and the inner wall of the outer annular partition, and an outer reaction chamber is formed between the outer wall of the outer annular partition and the inner wall of the shell; a catalyst flow zone is provided between the bottom of the inner annular partition and the gas distributor, and the intermediate reaction chamber and the internal discharge chamber are connected through the catalyst flow zone; the outer annular partition is fixed to the upper surface of the gas distributor; The built-in filter is located in the middle of the reaction chamber, and its height is below that of the inner annular partition. The height of the built-in filter is greater than the height of the top of the outer annular partition. The outlet of the built-in filter extends to the outside of the housing to form a synthetic wax outlet. The activation catalyst feed ring is located at the lower part of the peripheral reaction chamber; the inlet of the activation catalyst feed ring extends to the outside of the shell to form an activation catalyst inlet, and the side wall of the activation catalyst feed ring is provided with multiple outlets.

[0007] Optionally, the height ratio of the catalyst flow zone to the shell is (0.01-0.1):1.

[0008] Optionally, the top of the inner annular partition is located at 3 / 5 to 4 / 5 of the housing; the top of the outer annular partition is located at 2 / 5 to 3 / 5 of the housing.

[0009] Optionally, the ratio of the height of the built-in filter to the height of the housing is (0.5-0.7):1.

[0010] Optionally, the continuous Fischer-Tropsch synthesis reactor further includes partitions; the partitions are rectangular in shape. The partition plate is arranged along the axial direction of the shell in the reaction chamber, and the partition plate, the inner annular partition plate and the outer annular partition plate are inserted together to divide the outer reaction chamber into multiple outer reaction zones, the intermediate reaction chamber into multiple intermediate reaction zones and the inner discharge chamber into multiple inner discharge zones.

[0011] Optionally, the continuous Fischer-Tropsch synthesis reactor has 2-8 peripheral reaction zones, intermediate reaction zones, and internal discharge zones.

[0012] Optionally, the continuous Fischer-Tropsch synthesis reactor further includes a accumulator tray; the accumulator tray is fitted onto the deactivated catalyst discharge pipe so that the accumulator tray and the deactivated catalyst discharge pipe form an accumulator zone; the deactivated catalyst discharge port is located inside the accumulator zone.

[0013] Optionally, the continuous Fischer-Tropsch synthesis reactor also includes a demister and a temperature control device; The demister is located at the top of the housing and is used to remove the generated foam; The temperature control device is installed in the reaction chamber and is used to control the operating temperature of the continuous Fischer-Tropsch synthesis reactor.

[0014] A second aspect of this disclosure provides a method for a continuous Fischer-Tropsch synthesis reaction, the method comprising: The activated catalyst is continuously fed into the continuous Fischer-Tropsch synthesis reactor described in the first aspect through the activated catalyst inlet, and contacts the Fischer-Tropsch synthesis gas that enters the continuous Fischer-Tropsch synthesis reactor through the synthesis gas inlet to carry out the Fischer-Tropsch synthesis reaction, to obtain Fischer-Tropsch tail gas, liquid wax and slag wax containing deactivated catalyst and part of liquid wax. The activated catalyst undergoes the Fischer-Tropsch synthesis reaction sequentially through the outer reaction chamber, the intermediate reaction chamber, and the inner discharge chamber of the continuous Fischer-Tropsch synthesis reactor, and the resulting deactivated catalyst leaves the continuous Fischer-Tropsch synthesis reactor sequentially through the deactivated catalyst discharge port and the deactivated catalyst outlet. The liquid wax exits the continuous Fischer-Tropsch synthesis reactor sequentially through a built-in filter and a synthetic wax outlet; The Fischer-Tropsch tail gas is discharged from the Fischer-Tropsch tail gas outlet of the continuous Fischer-Tropsch synthesis reactor.

[0015] Optionally, the method further includes mixing the activated catalyst and liquid wax to form an activated catalyst slurry, and continuously feeding the activated catalyst slurry into the continuous Fischer-Tropsch synthesis reactor through an activated catalyst inlet; the solid content of the activated catalyst slurry is 5-25% by weight. The conditions for the Fischer-Tropsch synthesis reaction include: a reaction temperature of 250-300℃, a reaction pressure of 2.0-5.0MPa, an apparent gas velocity of 0.2-1.0m / s, and the hydrogen-to-carbon ratio of the Fischer-Tropsch synthesis gas maintained at 2-10.

[0016] The above technical solution uses partitions to rationally divide the reaction chamber, allowing the activated catalyst to react sequentially through the outer reaction chamber, the intermediate reaction chamber, and the inner discharge chamber of the continuous Fischer-Tropsch synthesis reactor. The resulting deactivated catalyst exits the reactor sequentially through the deactivated catalyst discharge port and the deactivated catalyst outlet. Compared to existing intermittent catalyst discharge processes, this significantly reduces catalyst backmixing, ensuring that most of the discharged catalyst is deactivated, maintaining a consistently high catalyst activity in the Fischer-Tropsch synthesis reaction, and improving the reaction efficiency. Furthermore, it enables continuous catalyst entry and continuous deactivated catalyst discharge, improving catalyst utilization efficiency, reducing catalyst replacement, and lowering catalyst consumption. Furthermore, because the activated catalyst flows upwards in the continuous Fischer-Tropsch synthesis reactor from the bottom up in the outer reaction chamber, then moves towards the inner intermediate reaction chamber, and finally flows towards the inner discharge chamber, the abrasion between catalysts is reduced, resulting in less fine catalyst powder. This not only reduces the number of built-in filters required and the pressure drop of the built-in filters, but also lowers the solid content in the liquid wax. In addition, the continuous Fischer-Tropsch synthesis reactor disclosed herein enables continuous operation, simplifies the operation process, and stabilizes the process conditions within the reactor.

[0017] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Attached Figure Description

[0018] The accompanying drawings are provided to further illustrate the present disclosure and form part of the specification. They are used together with the following detailed description to explain the present disclosure, but do not constitute a limitation thereof. In the drawings: Figure 1 This is a schematic diagram of a continuous Fischer-Tropsch synthesis reactor disclosed herein.

[0019] Figure 2 This is a schematic diagram of a continuous Fischer-Tropsch synthesis reaction system disclosed herein.

[0020] Figure 3This is a schematic diagram of a Fischer-Tropsch synthesis reactor as shown in Comparative Example 1 of this disclosure.

[0021] Explanation of reference numerals in the attached figures 1. Fresh catalyst feeder; 2. Catalyst activator; 3. Circulating gas compressor; 4. Activated catalyst buffer tank; 5. Continuous Fischer-Tropsch synthesis reactor; 6. Gas-liquid-solid separation unit; 7. Tail gas decarbonization unit; 8. Circulating gas compressor; 9. Oil recovery unit; 10. Solid-liquid separation unit; 21. Shell; 22. Activated catalyst inlet; 23. Synthesis gas inlet; 24. Fischer-Tropsch tail gas outlet; 25. Deactivated catalyst outlet; 26. Synthetic wax outlet; 27. Activated catalyst feed ring pipe; 28. Baffle; 28A. Inner annular baffle; 28B. Outer annular baffle; 29. ​​Gas distributor; 30. Built-in filter; 31. Deactivated catalyst discharge pipe; 32. Liquid collection tray; 33. Zone baffle; 34. Deactivated catalyst discharge port; 35. Heat exchanger; 36. Cyclone separator; a. Fischer-Tropsch synthesis gas; b. Activated synthesis gas; c. Fresh catalyst; d. Activated tail gas; e. Liquid wax; f. Fischer-Tropsch tail gas; g. First synthetic wax; h. First slag wax; i. Second slag wax; j. Third slag wax; k. Second synthetic wax; l. First recycle gas; m. Second recycle gas; n. Decarbonization tail gas; o. Light oil; p. Heavy oil; q. Synthetic water; r. Synthetic wax product; s. Solid waste; u. Exhaust gas phase. Detailed Implementation

[0022] The specific embodiments of this disclosure will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit this disclosure.

[0023] In this disclosure, unless otherwise stated, directional terms such as "upper" and "lower" generally refer to the upper and lower positions of the device in its normal operating state, for example, as shown in the reference. Figure 1 The orientation of the drawing, "inside" and "outside," refers to the orientation relative to the outline of the device. In the description of this disclosure, "a plurality of" means two or more, unless otherwise explicitly specified.

[0024] like Figure 1 As shown, the first aspect of this disclosure provides a continuous Fischer-Tropsch synthesis reactor, which includes a shell 21 and a partition 28, a gas distributor 29, an internal filter 30, a deactivated catalyst discharge pipe 31, and an activated catalyst feed ring pipe 27 disposed in the internal chamber of the shell 21; the bottom of the shell 21 is provided with a synthesis gas inlet 23, and the top of the shell 21 is provided with a Fischer-Tropsch tail gas outlet 24; The deactivated catalyst discharge pipe 31 is arranged axially within the shell 21. The top end of the deactivated catalyst discharge pipe 31 extends to the upper part of the shell 21, and the bottom end extends to the outside of the shell to form a deactivated catalyst outlet 25. Furthermore, the side wall of the deactivated catalyst discharge pipe 31 is provided with a plurality of deactivated catalyst discharge ports 34, so that the deactivated catalyst can leave the continuous Fischer-Tropsch synthesis reactor 5 sequentially through the deactivated catalyst discharge ports 34 and the deactivated catalyst outlet 25. The gas distributor 29 is disposed in the lower part of the internal cavity of the housing 21, and is used to divide the cavity between the housing 21 and the deactivated catalyst discharge pipe 31 into a reaction chamber and a synthesis gas chamber arranged vertically. The partition 28 is arranged axially along the housing 21 within the reaction chamber; the partition 28 includes an inner annular partition 28A and an outer annular partition 28B, with the inner annular partition 28A disposed inside the outer annular partition 28B; an internal discharge chamber is formed between the inner wall of the inner annular partition 28A and the outer wall of the deactivated catalyst discharge pipe 31, an intermediate reaction chamber is formed between the outer wall of the inner annular partition 28A and the inner wall of the outer annular partition 28B, and an outer reaction chamber is formed between the outer wall of the outer annular partition 28B and the inner wall of the housing 21; a catalyst flow zone is provided between the bottom of the inner annular partition 28A and the gas distributor 29, and the intermediate reaction chamber and the internal discharge chamber are connected through the catalyst flow zone; the outer annular partition 28B is fixed to the upper surface of the gas distributor 29. The built-in filter 30 is disposed in the middle of the reaction chamber, and the height of the built-in filter 30 is below the height of the inner annular partition 28A; the height of the built-in filter 30 is greater than the height of the top of the outer annular partition 28B; the outlet of the built-in filter 30 extends to the outside of the housing to form a synthetic wax outlet 26. The activation catalyst feed ring pipe 27 is located at the lower part of the outer reaction chamber; the inlet of the activation catalyst feed ring pipe 27 extends to the outside of the shell 21 to form the activation catalyst inlet 22, and the side wall of the activation catalyst feed ring pipe 27 is provided with multiple outlets.

[0025] The above technical solution uses partitions to rationally divide the reaction chamber, allowing the activated catalyst to react sequentially through the outer reaction chamber, the intermediate reaction chamber, and the inner discharge chamber of the continuous Fischer-Tropsch synthesis reactor. The resulting deactivated catalyst exits the reactor sequentially through the deactivated catalyst discharge port and the deactivated catalyst outlet. Compared to existing intermittent catalyst discharge processes, this significantly reduces catalyst backmixing, ensuring that most of the discharged catalyst is deactivated, maintaining a consistently high catalyst activity in the Fischer-Tropsch synthesis reaction, and improving the reaction efficiency. Furthermore, it enables continuous catalyst entry and continuous deactivated catalyst discharge, improving catalyst utilization efficiency, reducing catalyst replacement, and lowering catalyst consumption. Furthermore, because the activated catalyst flows upwards in the continuous Fischer-Tropsch synthesis reactor from the bottom up in the outer reaction chamber, then moves towards the inner intermediate reaction chamber, and finally flows towards the inner discharge chamber, the abrasion between catalysts is reduced, resulting in less fine catalyst powder. This not only reduces the number of built-in filters required and the pressure drop of the built-in filters, but also lowers the solid content in the liquid wax. In addition, the continuous Fischer-Tropsch synthesis reactor disclosed herein enables continuous operation, simplifies the operation process, and stabilizes the process conditions within the reactor.

[0026] In one embodiment, the dimensions of the housing 21 described herein can be flexibly set according to production needs. For example, the ratio of the diameter D to the height H of the housing 21 described herein is (5-10):1.

[0027] In one embodiment, the gas distributor 29 described in this disclosure can be a conventional choice in the art, and this application does not make any special requirements. For example, the gas distributor 29 is an orifice plate distributor.

[0028] In one embodiment, the gas distributor 29 is provided with multiple small-diameter synthesis gas through-holes, so that the Fischer-Tropsch synthesis gas in the gas chamber can enter the reaction chamber through the synthesis gas through-holes. The diameter of the synthesis gas through-holes can be flexibly adjusted according to actual production needs, as long as it prevents the activation catalyst or activated catalyst slurry from entering the synthesis gas chamber during the Fischer-Tropsch synthesis reaction in the continuous Fischer-Tropsch reactor 5.

[0029] In one embodiment, the multiple outlets of the activated catalyst feed ring pipe 27 described in this disclosure are evenly arranged on the side wall of the activated catalyst feed ring pipe 27, and the spray direction of the multiple outlets on the activated catalyst feed ring pipe 27 can be in any direction, preferably downward. The diameter of the multiple outlets of the activated catalyst feed ring pipe 27 can be flexibly set according to actual production needs, which will not be elaborated upon in this application.

[0030] In one embodiment, the number of outlets on the activated catalyst feed ring 27 is 12 to 20.

[0031] In one embodiment, the deactivated catalyst discharge pipe 31 includes a discharge section, a constricted section, and an outlet section connected sequentially from top to bottom; the bottom end of the discharge section of the deactivated catalyst discharge pipe 31 passes through the gas distributor 29. The constricted section is located inside the gas chamber, and the outlet section can be located outside the shell or partially inside the gas chamber. The outer diameter of the discharge section of the deactivated catalyst discharge pipe 31 can be flexibly set according to actual production needs. For example, the ratio of the diameter of the discharge section of the deactivated catalyst discharge pipe 31 to the diameter of the shell 21 is 1:(10-100), preferably 1:(40-60), and more preferably 1:50.

[0032] In one embodiment, the continuous Fischer-Tropsch synthesis reactor further includes a accumulator tray 32; the accumulator tray 32 is sleeved on the deactivated catalyst discharge pipe 31 so that the accumulator tray 32 and the deactivated catalyst discharge pipe 31 form an accumulator zone; the deactivated catalyst discharge port 34 is disposed inside the accumulator zone.

[0033] In one embodiment, the number of liquid collection pans 32 fitted on the deactivated catalyst discharge pipe 31 is 1-10, preferably 3.

[0034] In one embodiment, the position of the liquid collection tray 32 can be flexibly set according to actual production needs, as long as the height of the uppermost liquid collection tray 32 is less than the height of the built-in filter 30.

[0035] In one embodiment, a catalyst flow zone is provided between the bottom of the inner annular baffle 28A and the gas distributor 29, and the top of the inner annular baffle 28A extends upward by a certain distance. In this embodiment, the catalyst flow zone refers to a zone where part or all of the bottom of the inner annular baffle 28A does not contact the upper surface of the gas distributor 29, thereby allowing the deactivated catalyst slurry in the intermediate reaction chamber to enter the internal discharge chamber through the catalyst flow zone.

[0036] In one embodiment, the height ratio of the catalyst flow zone to the shell is (0.01-0.1):1.

[0037] In one embodiment, the top of the inner annular partition 28A is located at 3 / 5 to 4 / 5 of the housing 21.

[0038] In a preferred embodiment, the top of the inner annular partition 28A is located at 7 / 10 of the housing 21.

[0039] In one embodiment, the bottom of the outer annular partition 28B is fixed to the upper surface of the gas distributor 29, and the top of the outer annular partition 28B extends upward to a certain height.

[0040] In one embodiment, the top of the outer annular partition 28B is located at 2 / 5 to 3 / 5 of the housing 21.

[0041] In a preferred embodiment, the top of the outer annular partition 28B is located at 1 / 2 of the housing 21.

[0042] In one embodiment, the outer reaction chamber, the intermediate reaction chamber, and the inner discharge chamber described in this disclosure all have annular cross-sections along the radial direction of the shell.

[0043] In a preferred embodiment, the area ratio of the cross-sections of the outer reaction chamber, the intermediate reaction chamber, and the inner discharge chamber along the radial direction of the shell is (0.8-2):(0.8-2):1, preferably (1.2-1.5):(1.2-1.5):1.

[0044] In one embodiment, the number of built-in filters 30 in the continuous Fischer-Tropsch synthesis reactor 5 can be set according to actual production needs, which will not be elaborated here. In this embodiment, the operating pressure of the built-in filters 30 can be flexibly adjusted according to actual production needs. During the Fischer-Tropsch synthesis reaction, the higher the content of catalyst fine powder generated by catalyst wear, the greater the pressure drop of the built-in filters 30; the lower the content of catalyst fine powder generated by catalyst wear, the smaller the pressure drop of the built-in filters 30.

[0045] In one embodiment, the number of built-in filters 30 operating during the Fischer-Tropsch synthesis reaction is more than 30% of the number of built-in filters 30 in the continuous Fischer-Tropsch synthesis reactor 5.

[0046] In a preferred embodiment, the number of built-in filters 30 operating during the Fischer-Tropsch synthesis reaction is more than 50% of the number of built-in filters 30 in the continuous Fischer-Tropsch synthesis reactor 5.

[0047] In one embodiment, the built-in filter 30 of this disclosure includes a filtration section and a discharge section. The shape and size of the filtration section can be flexibly set according to actual production needs, as long as it can filter the catalyst powder in the liquid wax, which will not be elaborated here; the discharge section is an "L"-shaped tube, the horizontal section of which is perpendicular to the side wall of the housing 21, and the vertical section is parallel to the side wall of the housing 21.

[0048] In one embodiment, the filter section of the built-in filter 30 described in this disclosure is disposed below the horizontal section of the "L"-shaped tube. In this embodiment, the placement position of the built-in filter 30 refers to the placement position of the filter section, and the placement height of the built-in filter 30 refers to the placement height of the horizontal section of the "L"-shaped tube.

[0049] In one embodiment, the filter section of the built-in filter 30 can be disposed inside the outer reaction chamber, the intermediate reaction chamber and the inner discharge chamber, or it can be disposed outside the outer reaction chamber, the intermediate reaction chamber and the inner discharge chamber.

[0050] In a preferred embodiment, the built-in filter 30 is disposed in the middle of the reaction chamber, and the built-in filter 30 is disposed above the peripheral reaction chamber.

[0051] In one embodiment, the filter element of the built-in filter 30 is made of stainless steel and / or ceramic.

[0052] In one embodiment, the height of the built-in filter 30 is greater than the height of the top of the outer annular partition 28B; the height of the built-in filter 30 is lower than the height of the top of the inner annular partition 28A. In this embodiment, the height of the catalyst outlet pipe 31 can be higher than, lower than, or the same as the inner annular partition 28A.

[0053] In a preferred embodiment, the height of the catalyst discharge pipe 31 is between the height of the inner annular partition 28A and the height of the outer annular partition 28B.

[0054] In one embodiment, the ratio of the height of the built-in filter 30 to the height of the housing 21 is (0.5-0.7):1.

[0055] In a preferred embodiment, the ratio of the height of the built-in filter 30 to the height of the housing 21 is 0.6:1.

[0056] In one embodiment, the continuous Fischer-Tropsch synthesis reactor further includes a partition plate 33; the partition plate 33 is rectangular in shape; the partition plate 33 is arranged axially along the shell 21 in the reaction chamber, and the partition plate 33, the inner annular partition plate 28A and the outer annular partition plate 28B are inserted together to divide the outer reaction chamber into multiple outer reaction zones, the intermediate reaction chamber into multiple intermediate reaction zones, and the inner discharge chamber into multiple inner discharge zones.

[0057] In one embodiment, the bottom of the partition plate 33 is fixed to the upper surface of the gas distributor 29.

[0058] In one embodiment, the top of the partition plate 33 may be higher than or equal to the inner annular partition plate 28A; the top of the partition plate 33 is located at 7 / 10 to 9 / 10 of the housing 21, preferably at 4 / 5.

[0059] In one embodiment, the continuous Fischer-Tropsch synthesis reactor 5 has 2-8 peripheral reaction zones, intermediate reaction zones, and internal discharge zones.

[0060] In this embodiment, the combined structure of partition 33, inner annular partition 28A and outer annular partition 28B can significantly weaken the backmixing flow of the catalyst, thereby significantly reducing catalyst wear.

[0061] In one embodiment, the continuous Fischer-Tropsch synthesis reactor further includes a demister and a temperature control device; the demister is disposed at the top of the shell 21 for removing generated foam; the temperature control device is disposed in the reaction chamber for controlling the operating temperature of the continuous Fischer-Tropsch synthesis reactor. The demister and temperature control device, as well as their arrangement, are conventional choices in the art and are not specifically required in this application.

[0062] A second aspect of this disclosure provides a method for a continuous Fischer-Tropsch synthesis reaction, the method comprising: The activated catalyst is continuously introduced into the continuous Fischer-Tropsch synthesis reactor described in the first aspect through the activated catalyst inlet 22, and contacts the Fischer-Tropsch synthesis gas that enters the continuous Fischer-Tropsch synthesis reactor through the synthesis gas inlet 23 to carry out the Fischer-Tropsch synthesis reaction, and obtains Fischer-Tropsch tail gas, liquid wax and slag wax containing deactivated catalyst and part of liquid wax. The activated catalyst is sequentially passed through the outer reaction chamber, the intermediate reaction chamber and the inner discharge chamber of the continuous Fischer-Tropsch synthesis reactor to carry out the Fischer-Tropsch synthesis reaction, and the resulting deactivated catalyst is sequentially discharged from the continuous Fischer-Tropsch synthesis reactor 5 through the deactivated catalyst discharge port 34 and the deactivated catalyst outlet 25. The liquid wax exits the continuous Fischer-Tropsch synthesis reactor 5 sequentially through the built-in filter 30 and the synthetic wax outlet 26; The Fischer-Tropsch tail gas is discharged from the Fischer-Tropsch tail gas outlet 24 of the continuous Fischer-Tropsch synthesis reactor 5.

[0063] Through the above technical solution, the activated catalyst and Fischer-Tropsch synthesis gas undergo a Fischer-Tropsch synthesis reaction in the outer reaction chamber. The reacted catalyst is pushed upwards by continuously added activated catalyst. The catalyst at the top of the outer reaction chamber enters the intermediate reaction chamber, where it continues to react with the Fischer-Tropsch synthesis gas. The resulting catalyst then flows through the catalyst flow zone at the bottom of the inner annular partition 28A into the inner discharge zone to continue the Fischer-Tropsch synthesis reaction, yielding a deactivated catalyst. This continues until the height of the deactivated catalyst reaches the deactivated catalyst outlet 34. The deactivated catalyst and a portion of the liquid wax then exit the continuous Fischer-Tropsch synthesis reactor 5 sequentially through the deactivated catalyst outlet 34 and the deactivated catalyst outlet 25. Using this method, not only can the backmixing phenomenon of the catalyst be reduced, ensuring that the catalyst activity in the Fischer-Tropsch synthesis reaction remains at a high level and improving the reaction efficiency, but it can also reduce the catalyst replacement amount and decrease catalyst consumption. Furthermore, this method can reduce the number of built-in filters, reduce catalyst wear during filtration, and reduce the solid content in the liquid wax.

[0064] In one embodiment, the method further includes mixing the activated catalyst and liquid wax to form an activated catalyst slurry, and continuously feeding the activated catalyst slurry into the continuous Fischer-Tropsch synthesis reactor 5 through the activated catalyst inlet 22.

[0065] In one embodiment, the solid content of the activated catalyst slurry is 5-25% by weight.

[0066] In a preferred embodiment, the solid content of the activated catalyst slurry is 8-15% by weight.

[0067] In one embodiment, the method further includes continuously introducing the Fischer-Tropsch synthesis catalyst slurry into multiple peripheral reaction zones via an activated catalyst inlet 22. In this embodiment, the Fischer-Tropsch synthesis catalyst slurry reacts in multiple peripheral reaction zones, which can further reduce catalyst backmixing and thus significantly reduce catalyst wear.

[0068] In one embodiment, the conditions for the Fischer-Tropsch synthesis reaction include: a reaction temperature of 250-300°C, a reaction pressure of 2.0-5.0 MPa, an apparent gas velocity of 0.2-1.0 m / s, and the hydrogen-to-carbon ratio of the Fischer-Tropsch synthesis gas maintained at 2-10.

[0069] In a preferred embodiment, the conditions for the Fischer-Tropsch synthesis reaction include: a reaction temperature of 260-280°C, a reaction pressure of 2.5-3.5 MPa, an apparent gas velocity of 0.3-0.5 m / s, and the hydrogen-to-carbon ratio of the Fischer-Tropsch synthesis gas maintained at 3-5.

[0070] In one embodiment, the reaction type of the continuous Fischer-Tropsch synthesis reactor 5 described in this disclosure includes a slurry bed reactor, a fluidized bed reactor, or a boiling bed reactor, preferably a slurry bed reactor.

[0071] In one implementation, such as Figure 2 As shown, a continuous Fischer-Tropsch synthesis system includes a fresh catalyst feeder 1, a catalyst activator 2, a recirculating gas compressor 3, an activated catalyst buffer tank 4, a continuous Fischer-Tropsch synthesis reactor 5, and a gas-liquid-solid separation unit. The inlet of the fresh catalyst feeder 1 is connected to the fresh catalyst source, and the outlet of the fresh catalyst feeder 1 is connected to the catalyst inlet of the catalyst activator 2, so that the fresh catalyst c enters the catalyst activator 2 through the fresh catalyst feeder 1. The catalyst outlet of the catalyst activator 2 is connected to the catalyst inlet of the activated catalyst buffer tank 4 so that the activated catalyst enters the activated catalyst buffer tank 4. The activation gas inlet of the catalyst activator 2 is connected to the activation gas source, the activation tail gas outlet of the catalyst activator 2 is connected to the inlet of the circulating gas compressor 3, and the outlet of the circulating gas compressor 3 is connected to the activation gas inlet of the catalyst activator 2, so that the activated synthesis gas b enters the catalyst activator 2 for activation treatment, and the obtained activation tail gas is returned to the catalyst activator 2 via the circulating gas compressor 3. When the feed to the continuous Fischer-Tropsch synthesis reactor 5 is activated catalyst powder, the liquid wax inlet of the activated catalyst buffer tank 4 is closed so that the activated catalyst in the activated catalyst buffer tank 4 is powder; when the feed to the continuous Fischer-Tropsch synthesis reactor 5 is activated catalyst slurry, the liquid wax inlet of the activated catalyst buffer tank 4 is connected to a liquid wax source so that liquid wax can enter the activated catalyst buffer tank 4 to prepare the activated catalyst slurry; the gas phase outlet of the activated catalyst buffer tank 4 is connected to the atmosphere; The catalyst slurry outlet of the activated catalyst buffer tank 4 is connected to the activated catalyst inlet 22 of the continuous Fischer-Tropsch synthesis reactor 5. The syngas inlet 23 of the continuous Fischer-Tropsch synthesis reactor 5 is used to connect with a syngas source so that Fischer-Tropsch synthesis gas a enters the continuous Fischer-Tropsch synthesis reactor 5 and reacts with the activated catalyst. The Fischer-Tropsch tail gas outlet 24, the synthetic wax outlet 26, and the deactivated catalyst outlet 25 of the continuous Fischer-Tropsch synthesis reactor 5 are respectively connected to the inlet of the gas-liquid-solid separation unit, so that the Fischer-Tropsch tail gas f, the first synthetic wax g, and the second slag wax i enter the gas-liquid-solid separation unit for separation and treatment to obtain light oil o, heavy oil p, synthetic water q, synthetic wax product r, and solid waste s.

[0072] In one embodiment, the gas-liquid-solid separation unit includes a gas-liquid-solid separation device 6, a tail gas decarbonization device 7, a circulating gas compressor 8, an oil recovery device 9, and a solid-liquid separation device 10. The inlet of the gas-liquid-solid separation device 6 is connected to the Fischer-Tropsch tail gas outlet 24 of the continuous Fischer-Tropsch synthesis reactor 5, so that the Fischer-Tropsch tail gas f is separated by the gas-liquid-solid separation device 6 to obtain circulating gas and solid-liquid mixture. The gas phase outlet of the gas-liquid-solid separation device 6 is connected to the inlet of the tail gas decarbonization device 7 and the inlet of the circulating gas compressor 8, respectively. The decarbonized tail gas outlet of the tail gas decarbonization device 7 is connected to the inlet of the circulating gas compressor 8. The outlet of the circulating gas compressor 8 is connected to the synthesis gas inlet 23 of the continuous Fischer-Tropsch synthesis reactor 5, so that part of the circulating gas is used as the first circulating gas l and the other part of the circulating gas is used as the second circulating gas m. The first circulating gas l is processed by the tail gas decarbonization device 7, and the resulting decarbonized tail gas n and the second circulating gas m are mixed and then pressurized by the circulating gas compressor 8 before being returned to the continuous Fischer-Tropsch synthesis reactor 5. The solid-liquid outlet of the gas-liquid-solid separation device 6 is connected to the inlet of the oil recovery device 9 to separate the solid-liquid mixture into light oil o, heavy oil p, synthetic water q, and third residue wax j. The residue and wax outlet of the oil recovery device 9, the residue and wax outlet of the continuous Fischer-Tropsch synthesis reactor 5, and the residue and wax outlet of the activated catalyst buffer tank 4 are respectively connected to the inlet of the solid-liquid separation device 10, so that the first synthetic wax g, the second residue and wax i, and the first residue and wax h enter the solid-liquid separation device 10 for separation to obtain the second synthetic wax k and solid waste s; the synthetic wax outlet pipeline of the solid-liquid separation device 10 and the residue and wax outlet pipeline of the continuous Fischer-Tropsch synthesis reactor 5 merge to form a synthetic wax product pipeline, so that the first synthetic wax g and the second synthetic wax k are mixed to form synthetic wax product r.

[0073] In one embodiment, the operating conditions of other devices in the continuous Fischer-Tropsch synthesis system described in this disclosure, excluding the continuous Fischer-Tropsch synthesis reactor 5, can be flexibly adjusted according to actual production conditions.

[0074] The present disclosure is further illustrated by the following examples, but the disclosure is not limited thereto. The fresh catalyst used in the following examples and comparative examples is the CNFT-1 type iron-based catalyst independently developed by the Beijing Low Carbon Clean Energy Research Institute.

[0075] Example 1 The system used in this embodiment for a continuous Fischer-Tropsch synthesis reaction is as follows: Figure 2 As shown, the specific structure of the continuous Fischer-Tropsch synthesis reactor is as follows: Figure 1As shown, the continuous Fischer-Tropsch synthesis reactor has the following specifications: diameter 10m, height 70m, and catalyst storage capacity of 50t. The top of the inner annular baffle 28A is located at 7 / 10 of the shell 21. The height ratio of the catalyst flow zone to the shell is 0.05:1. The top of the outer annular baffle 28B is located at 1 / 2 of the shell 21. The height ratio of the built-in filter 30 to the shell 21 is 0.6:1. The continuous Fischer-Tropsch synthesis reactor contains 200 built-in filters.

[0076] Methods for continuous Fischer-Tropsch synthesis include: 14 tons of fresh catalyst preheated to 180°C was added to catalyst activator 2 and activated under an activating gas atmosphere for 16 hours at a constant temperature (apparent gas velocity 0.3 m / s, activation temperature 260°C, activation pressure 3.0 MPa, inlet hydrogen-to-carbon ratio 10.0). The entire activation operation cycle was 1.5 days.

[0077] The activation catalyst buffer tank 4 is pressurized to 2.7 MPa, and fluidizing gas with an apparent gas velocity of 0.1 m / s is introduced. The activation catalyst is transferred to the activation catalyst buffer tank 4 and mixed with liquid wax to form an activation catalyst slurry with a solid content of 20%, maintaining good fluidity of the catalyst slurry.

[0078] The activated catalyst slurry is continuously fed into the continuous Fischer-Tropsch synthesis reactor via the activated catalyst inlet 22 at a flow rate of 350 kg / h using a transfer pump. It contacts the Fischer-Tropsch synthesis gas entering the reactor via the synthesis gas inlet 23 to carry out the Fischer-Tropsch synthesis reaction, yielding Fischer-Tropsch tail gas, liquid wax, and slag wax containing deactivated catalyst and some liquid wax. The conditions for the Fischer-Tropsch synthesis reaction include: reaction temperature 275℃, reaction pressure 2.85 MPa, apparent gas velocity 0.3 m / s, inlet hydrogen-to-carbon ratio of 3.5, and catalyst solids content of 8%. A total of 30% of the catalyst is used... An internal filter allows a portion of the liquid wax to exit the continuous Fischer-Tropsch synthesis reactor 5 sequentially through the internal filter 30 and the synthetic wax outlet 26; another portion of the slag wax and the first slag wax formed by the deactivated catalyst sequentially enter the internal discharge chamber of the continuous Fischer-Tropsch synthesis reactor through the outer reaction chamber and the intermediate reaction chamber, and exit the continuous Fischer-Tropsch synthesis reactor sequentially through the deactivated catalyst outlet 34 and the deactivated catalyst outlet 25 at a flow rate of 870 kg / h; the Fischer-Tropsch tail gas exits the continuous Fischer-Tropsch synthesis reactor through the Fischer-Tropsch tail gas outlet 24. Liquid wax is obtained from the filter inside the Fischer-Tropsch slurry bed reactor as the first synthetic wax, and Fischer-Tropsch tail gas is obtained from the top. The Fischer-Tropsch tail gas is passed into a gas-liquid-solid separator to obtain oil, first recycle gas and second recycle gas. The oil is then processed by an oil recovery unit to obtain third residue wax, light oil, synthetic water and heavy oil. The first residue wax, second residue wax and third residue wax are mixed and then passed through a liquid-solid separation unit to obtain second synthetic wax and solid waste. The first synthetic wax and second synthetic wax are mixed to obtain synthetic wax. The first recycle gas is passed into a tail gas decarbonization unit to obtain decarbonized tail gas and relatively pure CO2. The decarbonized tail gas and second recycle gas are pressurized by a Fischer-Tropsch synthesis recycle gas compressor and then mixed with Fischer-Tropsch synthesis gas before entering the Fischer-Tropsch synthesis reactor. The relatively pure CO2 is purified and pressurized and then used as fluidizing gas in the catalyst activation buffer tank.

[0079] Using 100 built-in filters 30 for filtration, with an operating pressure drop of 10 kPa, the solid content of the catalyst in the first synthetic wax was measured to be <20 ppm. The bed temperature rise of the continuous Fischer-Tropsch synthesis reactor was <0.5℃, and the consumption per ton of oil (C5) was [missing information]. + The above-mentioned oil products have a yield of 1.42 kg / t oil (meaning 1.42 kg of catalyst can produce 1.0 ton of oil products).

[0080] Example 2 The method of continuous Fischer-Tropsch synthesis is the same as in Example 1, except that 95 built-in filters 30 are used for filtration, the operating pressure drop of the built-in filters 30 is increased by 8%, the solid content of the catalyst in the first synthetic wax is measured to be <20ppm, the bed temperature rise of the continuous Fischer-Tropsch synthesis reactor is <0.5℃, and the consumption per ton of oil is 1.43kg / t oil.

[0081] Example 3 The method for continuous Fischer-Tropsch synthesis is the same as in Example 1, except that the shell does not have partition plates 33. The operating pressure drop of the built-in filter 30 was increased by 5%, the solid content of the catalyst in the first synthetic wax increased to <50ppm, the bed temperature rise of the continuous Fischer-Tropsch synthesis reactor was <0.5℃, and the oil consumption was 1.47 kg / t oil.

[0082] Example 4 The method for continuous Fischer-Tropsch synthesis is the same as in Example 1, except that no liquid wax is added to the catalyst buffer tank 4, that is, the activated catalyst entering the continuous Fischer-Tropsch synthesis reactor 5 is activated catalyst powder, which is transported to the continuous Fischer-Tropsch synthesis reactor at a mass flow rate of 70 kg / h using a dense phase pump.

[0083] The measured operating pressure drop of the built-in filter 30 showed no significant change, the solid content of the catalyst in the first synthetic wax was <20ppm, the bed temperature rise of the continuous Fischer-Tropsch synthesis reactor was <0.5℃, and the consumption per ton of oil was 1.45kg / t oil.

[0084] Comparative Example 1 Adopting such Figure 3 The conventional Fischer-Tropsch synthesis reactor shown is different from the Fischer-Tropsch synthesis reactor in Example 1 in that, from bottom to top, the conventional Fischer-Tropsch synthesis reactor contains a heat exchange tube 35, an internal filter 30, a heat exchange tube 35, and a cyclone separator 36. Methods for Fischer-Tropsch synthesis include: 50 tons of activated catalyst were added to a conventional Fischer-Tropsch synthesis reactor for 3 days. Then, 10% of the catalyst stock in the reactor was replaced before continuing the Fischer-Tropsch synthesis reaction. When catalyst replacement was required, 10% of the total catalyst stock was first discharged from both inside and outside the reactor, followed by the addition of the same amount of activated catalyst. To achieve the same filtration pressure differential as in Example 1, 30% more built-in filters were used than in Example 1.

[0085] The solid content of the catalyst in the first synthetic wax was measured to be >50ppm, the bed temperature rise of the Fischer-Tropsch synthesis reactor was >3.0℃, and the consumption per ton of oil was 1.54kg / t oil.

[0086] A comparison of the data from Examples 1-4 and Comparative Example 1 shows that the continuous Fischer-Tropsch synthesis reactor of this disclosure not only reduces catalyst backmixing, ensuring the catalyst activity of the Fischer-Tropsch synthesis reaction remains at a high level and improving the reaction efficiency, but also reduces catalyst replacement and consumption. Furthermore, this method reduces the number of built-in filters used, decreases catalyst wear during filtration, and lowers the solid content in the liquid wax. A comparison of the data from Examples 1 and 2 shows that when the number of built-in filters operating during the Fischer-Tropsch synthesis reaction is more than 50% of the total number of built-in filters in the continuous Fischer-Tropsch synthesis reactor, the operating pressure drop of the built-in filters can be reduced, thereby reducing the consumption per ton of oil. A comparison of the data from Examples 1 and 3 shows that when partitions are installed inside the shell, catalyst wear is reduced, the operating pressure drop of the built-in filters is decreased, and the consumption per ton of oil is reduced. A comparison of the data from Examples 1 and 4 shows that when the activated catalyst entering the continuous Fischer-Tropsch synthesis reactor is an activated catalyst slurry, the consumption per ton of oil is reduced.

[0087] The preferred embodiments of this disclosure have been described in detail above with reference to the accompanying drawings. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0088] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0089] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A continuous Fischer-Tropsch synthesis reactor, characterized in that, The continuous Fischer-Tropsch synthesis reactor (5) includes a shell (21) and a partition (28), a gas distributor (29), an internal filter (30), a deactivated catalyst outlet pipe (31), and an activated catalyst feed ring pipe (27) disposed in the internal chamber of the shell (21); the bottom of the shell (21) is provided with a synthesis gas inlet (23), and the top of the shell (21) is provided with a Fischer-Tropsch tail gas outlet (24); The deactivated catalyst discharge pipe (31) is arranged axially within the shell (21), with the top end of the deactivated catalyst discharge pipe (31) extending to the upper part of the shell (21) and the bottom end extending to the outside of the shell to form a deactivated catalyst outlet (25); and the side wall of the deactivated catalyst discharge pipe (31) is provided with a plurality of deactivated catalyst outlets (34) so ​​that the deactivated catalyst can leave the continuous Fischer-Tropsch synthesis reactor (5) sequentially through the deactivated catalyst outlets (34) and the deactivated catalyst outlet (25); The gas distributor (29) is located in the lower part of the internal cavity of the housing (21) and is used to divide the cavity between the housing (21) and the deactivated catalyst discharge pipe (31) into a reaction chamber and a synthesis gas chamber arranged vertically. The partition (28) is arranged in the reaction chamber along the axial direction of the shell (21); the partition (28) includes an inner annular partition (28A) and an outer annular partition (28B), the inner annular partition (28A) is arranged inside the outer annular partition (28B); the inner wall of the inner annular partition (28A) and the outer wall of the deactivated catalyst discharge pipe (31) form an internal discharge chamber, the outer wall of the inner annular partition (28A) and the inner wall of the outer annular partition (28B) form an intermediate reaction chamber, and the outer wall of the outer annular partition (28B) and the inner wall of the shell (21) form an outer reaction chamber; a catalyst flow zone is provided between the bottom of the inner annular partition (28A) and the gas distributor (29), and the intermediate reaction chamber and the internal discharge chamber are connected through the catalyst flow zone; the outer annular partition (28B) is fixed on the upper surface of the gas distributor (29); The built-in filter (30) is located in the middle of the reaction chamber. The height of the built-in filter (30) is below the height of the inner annular partition (28A). The height of the built-in filter (30) is greater than the height of the top of the outer annular partition (28B). The outlet of the built-in filter (30) extends to the outside of the housing to form a synthetic wax outlet (26). The activation catalyst feed ring pipe (27) is located at the lower part of the outer reaction chamber; the inlet of the activation catalyst feed ring pipe (27) extends to the outside of the shell (21) to form the activation catalyst inlet (22), and the side wall of the activation catalyst feed ring pipe (27) is provided with multiple outlets.

2. The continuous Fischer-Tropsch synthesis reactor according to claim 1, characterized in that, The height ratio of the catalyst flow zone to the shell is (0.01-0.1):

1.

3. The continuous Fischer-Tropsch synthesis reactor according to claim 2, characterized in that, The top of the inner annular partition (28A) is located at 3 / 5 to 4 / 5 of the housing (21); The top of the outer annular partition (28B) is located at 2 / 5 to 3 / 5 of the housing (21).

4. The continuous Fischer-Tropsch synthesis reactor according to claim 2, characterized in that, The ratio of the height of the built-in filter (30) to the height of the housing (21) is (0.5-0.7):

1.

5. The continuous Fischer-Tropsch synthesis reactor according to claim 1, characterized in that, The continuous Fischer-Tropsch synthesis reactor (5) also includes partitions (33); the partitions (33) are rectangular in shape. The partition plate (33) is arranged in the reaction chamber along the axial direction of the shell (21), and the partition plate (33), the inner annular partition plate (28A) and the outer annular partition plate (28B) are inserted together to divide the outer reaction chamber into multiple outer reaction zones, the intermediate reaction chamber into multiple intermediate reaction zones and the inner discharge chamber into multiple inner discharge zones.

6. The continuous Fischer-Tropsch synthesis reactor according to claim 5, characterized in that, The continuous Fischer-Tropsch synthesis reactor (5) has 2-8 peripheral reaction zones, intermediate reaction zones, and internal discharge zones.

7. The continuous Fischer-Tropsch synthesis reactor according to claim 1, characterized in that, The continuous Fischer-Tropsch synthesis reactor (5) also includes a liquid collection tray (32); The liquid accumulation plate (32) is sleeved on the deactivated catalyst discharge pipe (31) so that the liquid accumulation plate (32) and the deactivated catalyst discharge pipe (31) form a liquid accumulation area; The deactivated catalyst outlet (34) is located inside the liquid accumulation zone.

8. The continuous Fischer-Tropsch synthesis reactor according to claim 1, characterized in that, The continuous Fischer-Tropsch synthesis reactor (5) also includes a demister and a temperature control device; The demister is disposed at the top of the housing (21) for removing the generated foam; The temperature control device is installed in the reaction chamber and is used to control the operating temperature of the continuous Fischer-Tropsch synthesis reactor (5).

9. A method for continuous Fischer-Tropsch synthesis, characterized in that, The method includes: The activated catalyst is continuously introduced into the continuous Fischer-Tropsch synthesis reactor (5) according to any one of claims 1-8 through the activated catalyst inlet (22), and is contacted with the Fischer-Tropsch synthesis gas entering the continuous Fischer-Tropsch synthesis reactor (5) through the synthesis gas inlet (23) to carry out the Fischer-Tropsch synthesis reaction, and Fischer-Tropsch tail gas, liquid wax and slag wax containing deactivated catalyst and part of liquid wax are obtained. The activated catalyst is sequentially passed through the outer reaction chamber, the intermediate reaction chamber and the inner discharge chamber of the continuous Fischer-Tropsch synthesis reactor (5) to carry out the Fischer-Tropsch synthesis reaction, and the resulting deactivated catalyst is sequentially discharged from the continuous Fischer-Tropsch synthesis reactor (5) through the deactivated catalyst discharge port (34) and the deactivated catalyst outlet (25). The liquid wax is sequentially passed through the built-in filter (30) and the synthetic wax outlet (26) before leaving the continuous Fischer-Tropsch synthesis reactor (5); The Fischer-Tropsch tail gas is discharged from the Fischer-Tropsch tail gas outlet (24) of the continuous Fischer-Tropsch synthesis reactor (5).

10. The method according to claim 9, characterized in that, The method further includes mixing the activated catalyst and liquid wax to form an activated catalyst slurry, and continuously feeding the activated catalyst slurry into the continuous Fischer-Tropsch synthesis reactor (5) through the activated catalyst inlet (22); The solid content of the activated catalyst slurry is 5-25% by weight. The conditions for the Fischer-Tropsch synthesis reaction include: a reaction temperature of 250-300℃, a reaction pressure of 2.0-5.0MPa, an apparent gas velocity of 0.2-1.0m / s, and the hydrogen-to-carbon ratio of the Fischer-Tropsch synthesis gas maintained at 2-10.

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