Device and method for on-line replacement of catalyst of slurry bed reactor

Abstract

The invention relates to the technical field of Fischer-Tropsch synthesis, in particular to a device and a method for online replacement of a catalyst of a slurry bed reactor, the device comprises the slurry bed reactor (1), the slurry bed reactor (1) is used for performing Fischer-Tropsch synthesis reaction on activated catalyst slurry and synthesis gas, and gas, heavy wax and wax residue are obtained after the reaction; the standing separation tank (3) is used for separating the wax residue into high-concentration wax residue and an oil wax product; the gas-solid fluidized bed activation reactor (9) is used for activating the catalyst to obtain the activated catalyst; and the catalyst mixing tank (6) is used for mixing the activated catalyst with the oil wax product to obtain activated catalyst slurry. According to the invention, the catalyst replacement mode in the slurry bed reactor is changed from an intermittent mode to a continuous mode, the device system fluctuation caused by the catalyst replacement process is reduced, the oil wax product separated from the deactivated catalyst is recycled, the operation of adding externally supplied slurry in the agent adding process is omitted, and the energy for heating the externally supplied slurry is saved.

Description

Technical Field

[0001] The invention relates to the technical field of Fischer-Tropsch synthesis, and in particular to a device and method for online replacement of a catalyst in a slurry bed reactor. Background Art

[0002] Slurry bed reactors are widely used in industrial applications, the most important of which is slurry bed Fischer-Tropsch synthesis. Taking Fischer-Tropsch synthesis as an example, in order to maintain a high activity in the Fischer-Tropsch synthesis slurry bed reactor, it is necessary to regularly discharge the deactivated catalyst material in the slurry bed reactor and add activated catalyst material to the slurry bed reactor.

[0003] The current unloading method is to discharge the slag wax (slurry containing deactivated catalyst) into the slag wax storage tank through the discharge port of the slurry bed reactor, and then transfer it to the filtration unit to separate the deactivated catalyst from the slurry, wherein the deactivated catalyst is sent to the downstream for separate treatment and the slurry is recovered. When the gas-solid fluidized bed is used to activate the catalyst, the current feeding method is to transport the activated catalyst alone to another container and mix it with liquid such as heavy wood or liquid wax to form a slurry, and then transport it to the slurry bed reactor.

[0004] CN114736714A discloses an online replacement method for Fischer-Tropsch synthesis catalyst, wherein the catalyst obtained after activation in a gas-solid fluidized bed is first transported to a storage tank for storage, and then transported to a slurry tank filled with liquid paraffin and / or heavy wood, mixed to form a slurry, and then the slurry is pressed into a Fischer-Tropsch synthesis reactor. However, in this replacement method, the residual wax discharged during the catalyst replacement in the slurry bed reactor contains only about 10% of the deactivated catalyst, and the rest is the oil wax product that needs to be recovered.

[0005] CN210176795U discloses a catalytic cracking catalyst charging and unloading mechanism, which greatly avoids the influence of excessive temperature difference in catalyst charging and unloading on the production process by changing the catalyst charging and unloading positions. However, this system is only applicable to the regeneration system of catalytic cracking catalyst, and the whole system is gas-solid two-phase, and cannot be applied to the catalyst replacement process of the slurry bed Fischer-Tropsch synthesis system.

[0006] Therefore, there are several major defects in the prior art: First, the catalyst replacement process is an intermittent periodic replacement, and each replacement time is short and the replacement volume is large, which leads to large fluctuations in the slurry and reaction in the reactor, affecting the performance of the device; Second, a large amount of slag wax regularly discharged from the slurry bed Fischer-Tropsch synthesis reactor needs to be sent to the downstream slag wax processing unit, and the processing workload is large; Third, in the process of slag wax discharge from the reactor, catalyst activation, and mixing the activated catalyst with heavy wood or liquid wax into slurry, the transportation and filtration of slag wax, the storage, transportation and filling, and heating of heavy wood all require a large amount of material and energy consumption. Summary of the invention

[0007] The purpose of the present invention is to solve the problems raised in the background technology and to provide a device and method for online replacement of catalyst in a slurry bed reactor.

[0008] In order to achieve the above-mentioned object of the invention, the first aspect of the present invention provides a device for replacing catalyst in a slurry bed reactor, the device comprising:

[0009] A slurry bed reactor is used to carry out a Fischer-Tropsch synthesis reaction between the activated catalyst slurry and the synthesis gas, and obtain gas, heavy wax and residual wax after the reaction;

[0010] A static separation tank connected to the slurry bed reactor through a first connecting pipe and a third connecting pipe, and used for separating the slag wax into high-concentration slag wax and oil wax products;

[0011] A catalyst mixing tank, connected to the static separation tank via a second connecting pipe, and connected to the slurry bed reactor via a fourth connecting pipe, for mixing the activated catalyst with the oil wax product to obtain an activated catalyst slurry;

[0012] The gas-solid fluidized bed activation reactor is connected to the third connecting pipe via a fifth connecting pipe and is used to activate the catalyst to obtain an activated catalyst.

[0013] A second aspect of the present invention provides a method for online replacement of a catalyst in a slurry bed reactor, the method using the above-mentioned device for online replacement of the catalyst, the method comprising the following steps:

[0014] S1: The residual wax in the slurry bed reactor enters the static separation tank through the first connecting pipe, and the oil wax product and the high-concentration residual wax are obtained after separation;

[0015] S2: The oil wax product enters the catalyst mixing tank through the second connecting pipe;

[0016] S3: The catalyst activated by the gas-solid fluidized bed activation reactor passes through the fifth connecting pipe and enters the catalyst mixing tank together with the oil wax product through the second connecting pipe;

[0017] S4: The oil wax product is mixed with the catalyst to form an activated catalyst slurry, which enters the slurry bed reactor through the fourth connecting pipe.

[0018] Compared with the prior art, the present invention has the following beneficial effects:

[0019] 1. In the catalyst replacement process of the present invention, the residual wax in the slurry bed reactor continuously enters the static separation tank, the static separation tank continuously discharges the oil wax product by overflow, and the activated catalyst slurry continuously enters the slurry bed reactor, and the periodic intermittent large-dose replacement process in the slurry reactor is replaced by a continuous low-dose replacement process. In this way, the average amount of slurry entering and exiting the slurry reactor per hour is only about 1% of the total volume of the reactor, so the change of the slurry in the reactor is small, ensuring the stable reaction of the device.

[0020] 2. When the deactivated catalyst is unloaded in the present invention, a static separation tank is set outside the slurry bed reactor to separate the oil wax product and the high-concentration residue wax in the residue wax. The obtained oil wax product can be recycled, and the high-concentration residue wax is sent to the residue wax processing unit, thereby reducing the processing capacity of the downstream residue wax processing unit.

[0021] 3. When adding the activated catalyst of the present invention, a catalyst mixing tank is arranged outside the slurry bed reactor, and the activated catalyst is directly mixed with the hot oil wax product obtained from the static separation tank, thereby realizing the reuse of the oil wax (product) in the slurry, eliminating the use of external slurry such as heavy wood or liquid wax and its heating operation. In addition, the transportation of a small amount of high-concentration residual wax at the bottom of the static separation tank can be eliminated. Therefore, the online continuous catalyst replacement process provided by the present invention can save a lot of material and energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 A flow chart of online replacement of catalyst in a slurry bed reactor provided by the present invention;

[0023] Figure 2 A flow chart of online catalyst replacement in a slurry bed reactor provided as a comparative example.

[0024] Description of Reference Numerals

[0025] 1-slurry bed reactor; 2-first connecting pipe; 3-stationary separation tank; 4-second connecting pipe; 5-third connecting pipe; 6-catalyst mixing tank; 7-agitator; 8-fourth connecting pipe; 9-gas-solid fluidized bed reactor; 10-activated catalyst finished product tank; 11-fifth connecting pipe; 12-sixth connecting pipe; 13-seventh connecting pipe;

[0026] I-slurry bed reactor; II-wax discharge line; III-heavy fuel oil storage tank; IV-heavy fuel oil feeding line; V-heavy fuel oil feeding pump; VI-heavy fuel oil heater; VII-catalyst mixing tank; VIII-activated slurry filling line; IX-gas-solid fluidized bed reactor; X-activated catalyst finished product tank; XI-ventilation and pressurization pipeline; XII-activated catalyst storage line. DETAILED DESCRIPTION

[0027] The specific implementation of the present invention will be further described below in conjunction with the accompanying drawings.

[0028] It is easy to understand that according to the technical solution of the present invention, without changing the essential spirit of the present invention, a variety of structural modes and implementation modes that can be replaced by those skilled in the art can be replaced with each other. Therefore, the following specific implementation modes and drawings are only exemplary descriptions of the technical solution of the present invention, and should not be regarded as the whole of the present invention or as a limitation or restriction to the technical solution of the invention.

[0029] The directional terms such as up, down, left, right, front, back, front, back, top, bottom, etc. mentioned or may be mentioned in this specification are defined relative to the structures shown in the drawings. They are relative concepts and may change accordingly according to different positions and different usage conditions. Therefore, these or other directional terms should not be interpreted as restrictive terms.

[0030] The method for online replacement of the catalyst in the slurry bed reactor of the present invention is described in further detail below, but the present invention is not limited thereto.

[0031] A first aspect of the present invention provides a device for online replacement of catalyst in a slurry bed reactor, the device comprising:

[0032] A slurry bed reactor is used to carry out a Fischer-Tropsch synthesis reaction between the activated catalyst slurry and the synthesis gas, and obtain gas, heavy wax and residual wax after the reaction;

[0033] A static separation tank connected to the slurry bed reactor through a first connecting pipe and a third connecting pipe, and used for separating the slag wax into high-concentration slag wax and oil wax products;

[0034] A catalyst mixing tank, connected to the static separation tank via a second connecting pipe, and connected to the slurry bed reactor via a fourth connecting pipe, for mixing the activated catalyst with the oil wax product to obtain an activated catalyst slurry;

[0035] The gas-solid fluidized bed activation reactor is connected to the third connecting pipe via a fifth connecting pipe and is used to activate the catalyst to obtain an activated catalyst.

[0036] In some embodiments, the gas in the slurry bed reactor is gaseous hydrocarbon products, water vapor products and unreacted synthesis gas, and the heavy wax is C5-C 100 The hydrocarbon products are sludge containing deactivated catalyst.

[0037] In some embodiments, the high-consistency wax residue contains a high concentration of deactivated catalyst.

[0038] In some embodiments, the oil wax product is mainly composed of a liquid medium (a solvent for the catalyst) and also contains a low concentration of deactivated catalyst.

[0039] Furthermore, the liquid medium is exemplarily liquid paraffin and / or heavy wood, and the liquid medium can effectively reduce the collision and wear of the activated catalyst during the feeding process.

[0040] In the present invention, the static separation tank can utilize density difference to separate high-concentration residual wax from oil wax products in the residual wax.

[0041] In some embodiments, the temperature of the static separation tank is in the range of 20°C lower than the temperature of the slurry bed reactor to the same temperature as the slurry bed reactor, and the pressure is the same as that of the slurry bed reactor. Too low a temperature will cause the oil wax product to condense and be inconvenient to flow.

[0042] In some embodiments, the material separated in the static separation tank includes, in addition to the high-concentration residual wax and oil wax products, gaseous hydrocarbon products, water vapor products, and unreacted synthesis gas in the residual wax.

[0043] Furthermore, the high-concentration residual wax separated in the static separation tank is located at the bottom of the static separation tank and is sent to the downstream residual wax processing unit through the sixth connecting pipe.

[0044] Furthermore, the oil-wax product separated in the static separation tank is located at the upper part of the static separation tank and enters the catalyst mixing tank through the second connecting pipe.

[0045] Furthermore, the gaseous hydrocarbon products, water vapor products and unreacted synthesis gas in the residual wax separated in the static separation tank are returned to the slurry bed reactor through the third connecting pipe.

[0046] In some embodiments, the static separation tank may be provided with baffles of different forms, exemplified by arcuate baffles and disc-ring baffles.

[0047] Furthermore, a plurality of vertically installed baffles are arranged inside the static separation tank, and the spacing between each layer of baffles is 0.2-0.5m according to the size of the tank body.

[0048] Furthermore, the baffles are installed vertically so that the residual wax can flow along the baffle walls during static separation, which greatly increases the separation time and further enhances the separation effect of the oil wax product and the high-concentration residual wax.

[0049] In the present invention, the third connecting pipe is used to maintain the pressure of the static separation tank stable. At the same time, in the reactor, the density of the gas in the slurry increases after being discharged, and it can return to the bottom of the slurry bed reactor by relying on the density difference.

[0050] In some embodiments, the temperature of the catalyst mixing tank is in the range of 20° C. lower than the temperature of the slurry bed reactor to the same temperature as the slurry bed reactor, and the pressure is the same as that of the slurry bed reactor.

[0051] In the present invention, the activated catalyst can be directly mixed with the hot oil wax product without the need to provide additional heated external slurry (liquid medium).

[0052] It is known to those skilled in the art that the gas-solid fluidized bed activation reactor is used to contact the iron-based Fischer-Tropsch synthesis catalyst to be activated with a reducing gas to carry out a reduction reaction to obtain an activated catalyst.

[0053] In some embodiments, an activated catalyst product tank may be provided between the gas-solid fluidized bed activation reactor and the fifth connecting pipe.

[0054] Furthermore, the temperature of the activated catalyst finished product tank is in the range of 20°C lower than the temperature of the slurry bed reactor to the same temperature as the slurry bed reactor, and the pressure is 0.01-3.0 MPa.

[0055] In some embodiments, the activated catalyst product tank and the gas-solid fluidized bed activation reactor may be connected via a seventh connecting pipe.

[0056] In some embodiments, the finished catalyst tank is used to place the catalyst activated by the gas-solid fluidized bed, so that the gas-solid fluidized bed activation process of the catalyst can be separated from the catalyst replacement process. That is, as long as there is activated catalyst in the finished catalyst tank, the replacement process can be kept continuous regardless of whether the gas-solid fluidized bed is running or shut down.

[0057] In some embodiments, the catalyst mixing tank may be provided with internal components such as baffles, or an agitator, depending on the slurrying speed and the size of the tank body, to enhance the mixing of the activated catalyst and the oil wax product.

[0058] Furthermore, a stirrer is arranged inside the catalyst mixing tank and is perpendicular to the tank bottom, and the bottom of the stirrer is 0.2-0.5m away from the tank bottom; or,

[0059] The catalyst mixing tank is provided with horizontally installed multi-layer baffles, and the spacing between each layer of baffles is 0.2-0.5m; or,

[0060] The catalyst mixing tank is provided with an agitator perpendicular to the tank bottom and horizontally installed multi-layer baffles. The spacing between each layer of the multi-layer baffles is 0.2m, and the uppermost baffle is 0.2m away from the bottom of the agitator.

[0061] Furthermore, the baffle is arranged to be installed horizontally to provide more contact area for the activated catalyst and the oil wax product, thereby further enhancing their mixing effect.

[0062] A second aspect of the present invention provides a method for online replacement of a catalyst in a slurry bed reactor, comprising the following steps:

[0063] S1: The residual wax in the slurry bed reactor enters the static separation tank through the first connecting pipe, and the oil wax product and the high-concentration residual wax are obtained after separation;

[0064] S2: The oil wax product enters the catalyst mixing tank through the second connecting pipe;

[0065] S3: The catalyst activated by the gas-solid fluidized bed activation reactor passes through the fifth connecting pipe and enters the catalyst mixing tank together with the oil wax product through the second connecting pipe;

[0066] S4: The oil wax product is mixed with the catalyst to form an activated catalyst slurry, which enters the slurry bed reactor through the fourth connecting pipe.

[0067] In some embodiments, the online replacement volume of the slurry bed reactor per hour is 0.01-10% of the total volume of the slurry in the slurry bed reactor, that is, the volume discharged per hour from the slurry bed reactor through the first connecting pipe is 0.01%-10% of the total volume of the slurry in the slurry bed reactor, and at the same time, the volume of the activated catalyst entering the catalyst mixing tank through the second connecting pipe through the fifth connecting pipe together with the oil wax product is also 0.05%-10% of the total volume of the slurry in the slurry bed reactor per hour, preferably 0.1-1%.

[0068] In some embodiments, the temperature inside the static separation tank and the catalyst mixing tank is in the range of 20° C. lower than the temperature of the slurry bed reactor to the same as the temperature of the slurry bed reactor.

[0069] A finished catalyst tank after activation is arranged between the gas-solid fluidized bed activation reactor and the third lower connecting pipe.

[0070] Furthermore, the temperature inside the activated catalyst product tank is in the range of 20°C lower than the temperature of the slurry bed reactor to the same temperature as the slurry bed reactor, and the pressure is 0.01-3MPa.

[0071] In order to further illustrate the present invention, an apparatus and method for online replacement of catalyst in a Fischer-Tropsch synthesis slurry bed reactor provided by the present invention are described in detail below in conjunction with embodiments, but it should not be construed as limiting the scope of protection of the present invention.

[0072] Example 1

[0073] S1: 7 tons of catalyst are activated using a gas-solid fluidized bed reactor 9, and the activated catalyst is transported through a seventh connecting pipe 13 and stored in an activated catalyst finished product tank 10 (temperature is 270° C., pressure is 2.9 MPa);

[0074] S2: The slag wax at 270°C in the slurry bed reactor is discharged into the static separation tank 3 through the first connecting pipe 2 at a flow rate of 1 t / h, and the light oil wax product on the upper layer of the static separation tank 3 flows into the catalyst mixing tank 6 through the second connecting pipe 4, at which time the temperature of the oil wax product is 270°C; the heavy deactivated catalyst on the lower layer of the static separation tank 3 sinks to the bottom of the tank, and is discharged into the downstream slag wax processing unit through the sixth connecting pipe 12;

[0075] The total amount of solid catalyst in the slurry bed reactor 1 is 70t, accounting for 10% of the total volume of the slurry, and the concentration of the deactivated catalyst in the slag wax is 10%. The flow rate can be controlled by the valves attached to each device;

[0076] S3: After activation, the catalyst in the finished catalyst tank 10 is connected to the second connecting pipe 4 through the fifth connecting pipe 11, and enters the catalyst mixing tank 6 together with the oil wax product;

[0077] Among them, the flow rate of oil wax product is 0.9 t / h, the flow rate of activated catalyst is 0.1 t / h, and the replacement amount of catalyst per hour is 0.14% of the total volume of slurry;

[0078] S4: After the oil wax product and the activated catalyst are fully and continuously mixed in the catalyst mixing tank 6 , they are added into the slurry bed reactor 1 through the fourth connecting pipe 8 .

[0079] Example 2

[0080] The difference from Example 1 is that in step S1, the temperature in the activated catalyst finished product tank 10 is 250°C; in step S2, the temperature of the oil wax product flowing into the catalyst mixing tank 6 is 250°C, that is, they are 20°C lower than the temperature of 270°C in the slurry bed reactor 1.

[0081] Example 3

[0082] The difference from Example 1 is that in step S2, the residual wax enters the static separation tank 3 at a flow rate of 0.35 t / h; in step S3, the flow rate of the oil wax product is 0.315 t / h, the flow rate of the activated catalyst is 0.035 t / h, and the catalyst replacement amount per hour is 0.05%.

[0083] Comparative Example

[0084] S1: 7 tons of catalyst to be added is activated using a gas-solid fluidized bed reactor IX, and the activated catalyst is transported through an activated catalyst storage line XII and stored in an activated catalyst finished product tank X (temperature is 270° C., pressure is 2.9 MPa);

[0085] S2: 63 tons of heavy fuel oil in the heavy fuel oil storage tank III enters the heavy fuel oil feeding pump V through the heavy fuel oil feeding line IV and is sent to the heavy fuel oil heater VI. After the heavy fuel oil is heated to 270°C, it is sent to the catalyst mixing tank VII. At this time, 7 tons of activated catalyst in the catalyst finished product tank X is added to the catalyst mixing tank VII and mixed evenly;

[0086] S3: While carrying out S1 and S2, the 70t of liquid slag wax in the slurry bed reactor I is sent to the downstream slag wax processing unit through the slag wax discharge line II;

[0087] S4: The pressure of the catalyst mixing tank VII is increased to 3.2 MPa by gas pressurization, and the mixed slurry passes through the activated slurry filling line VIII and is pressurized by the ventilation and pressurization pipeline XI to enter the slurry bed reactor I;

[0088] According to the existing operating requirements, a batch of catalyst replacement is required every 70 hours. The catalyst replaced each time accounts for about 10% of the total volume of the slurry in the slurry bed reactor. Each time the catalyst is unloaded and added, it takes about 3 hours.

[0089] The effects of the embodiments and comparative examples on the reaction performance and heat consumption of the device are compared in the table below.

[0090] serial number (CO in synthesis gas) raw material conversion rate Additional heavy wood heating energy consumption Example 1 99％ 0 Example 2 98.5％ 0 Example 3 97.5％ 0 Comparative Example 96％ <![CDATA[6×10 9 kJ]]>

[0091] From the above embodiments and comparative examples, it can be seen that the catalyst replacement process of the existing slurry bed reactor will bring some adverse effects: (1) The catalyst replacement process is an intermittent replacement process, and the entire replacement cycle is generally 70 hours. Each replacement process takes about 3 hours, and the replacement amount accounts for about 10% of the total volume of the slurry in the reactor; and the operation process of replacing 10% of the total volume of materials in 3 hours causes a large change in the slurry in the reactor, resulting in a large fluctuation in the Fischer-Tropsch synthesis reaction, affecting the performance of the slurry reaction system; (2) The slurry bed reactor regularly discharges slag wax, and the slag wax enters the slag wax treatment unit. The deactivated catalyst in the slag wax is separated from the oil wax product by filtering and other means, and the workload of slag wax treatment is large; at the same time, the catalyst activation process is the same as the cycle of slag wax discharge. In order to keep the reactor liquid level unchanged, after the catalyst activation is completed, the volume of the activated catalyst slurry finally transferred to the catalyst mixing tank of the slurry bed reactor must be the same as the volume of the discharged slag wax. In this process, the transportation and filtration of the slag wax, the storage, transportation and filling of heavy wood, and the heating and heating all require a large amount of material and energy consumption.

[0092] In the online continuous catalyst replacement process provided by the present invention, in Example 1, an average of 0.1 t of catalyst is replaced per hour, and 7 t of catalyst is also replaced in 70 hours. However, due to the stability of the continuous replacement device, the CO raw material conversion rate in the synthesis gas can be increased by 2%, and the effect is obvious. In Example 3, an average of 0.035 t of catalyst is replaced per hour, and 2.45 t of catalyst is replaced in 70 hours. When the catalyst replacement amount is much lower than that of the comparative example, the CO raw material conversion rate in the synthesis gas is also higher than that of the comparative example. In addition, since the heating of heavy wood is not required in the embodiment, about 6.0×10 9 kJ of energy.

[0093] In addition, Examples 1-3 achieve the reuse of the oil wax (product) in the slurry, and can also greatly reduce the processing volume of the downstream slag wax filtration unit, saving the use of white clay / diatomaceous earth in the slag wax filtration process, and significantly saving material and energy consumption.

Claims

1. A device for online replacement of catalyst in a slurry bed reactor, characterized in that: The device comprises: A slurry bed reactor (1) is used for performing a Fischer-Tropsch synthesis reaction between the activated catalyst slurry and the synthesis gas, and after the reaction, gas, heavy wax and residual wax are obtained; A static separation tank (3) is connected to the slurry bed reactor (1) via a first connecting pipe (2) and a third connecting pipe (5), and is used to separate the residual wax into high-concentration residual wax and oil wax products; The catalyst mixing tank (6) is connected to the static separation tank (3) via a second connecting pipe (4) and connected to the slurry bed reactor (1) via a fourth connecting pipe (8) and is used to mix the activated catalyst with the oil wax product to obtain an activated catalyst slurry. The gas-solid fluidized bed activation reactor (9) is connected to the third connecting pipe (4) via a fifth connecting pipe (11) and is used to activate the catalyst to obtain an activated catalyst.

2. The device according to claim 1, characterized in that The temperature inside the static separation tank (3) is in the range of 20°C lower than the temperature of the slurry bed reactor and the same as the temperature of the slurry bed reactor.

3. The device according to claim 1, characterized in that The temperature inside the catalyst mixing tank (6) is in the range of 20°C lower than the temperature of the slurry bed reactor to the same as the temperature of the slurry bed reactor.

4. The device according to claim 1, characterized in that An activated catalyst product tank (10) is arranged between the gas-solid fluidized bed activation reactor (9) and the fifth connecting pipe (11).

5. The device according to claim 4, characterized in that The temperature inside the activated catalyst finished product tank (10) is in the range of 20°C lower than the temperature of the slurry bed reactor and the same as the temperature of the slurry bed reactor; The pressure inside the activated catalyst finished product tank (10) is 0.01-3 MPa.

6. The device according to claim 1 or 2, characterized in that: The interior of the static separation tank (3) is provided with multiple layers of baffles installed vertically, and the spacing between each layer of baffles is 0.2-0.5m.

7. The device according to claim 1 or 3, characterized in that: The catalyst mixing tank (6) is provided with an agitator vertical to the tank bottom, and the bottom of the agitator is 0.2-0.5 m away from the tank bottom; or, The catalyst mixing tank (6) is provided with multiple layers of baffles installed horizontally, and the spacing between each layer of baffles is 0.2-0.5m; or, The catalyst mixing tank (6) is provided with an agitator perpendicular to the tank bottom and horizontally installed multi-layer baffles, the spacing between each layer of the multi-layer baffles is 0.2m, and the top baffle is 0.2m away from the bottom of the agitator.

8. A method for online replacement of catalyst in a slurry bed reactor, characterized in that: The method uses the device according to any one of claims 1 to 7, and the method The following steps are involved: S1: The residual wax in the slurry bed reactor (1) enters the static separation tank (3) through the first connecting pipe (2), and the oil wax product and the high-concentration residual wax are obtained after separation; S2: the oil wax product enters the catalyst mixing tank (6) through the second connecting pipe (4); S3: The catalyst activated by the gas-solid fluidized bed activation reactor (9) passes through the fifth connecting pipe (11) and enters the catalyst mixing tank (6) through the second connecting pipe (4) together with the oil wax product; S4: The oil wax product is mixed with the catalyst to form an activated catalyst slurry, which enters the slurry bed reactor (1) through the fourth connecting pipe (8).

9. The method according to claim 8, characterized in that The online replacement volume per hour of the slurry bed reactor is 0.01-10% of the total volume of the slurry in the slurry bed reactor.

10. The method according to claim 8 or 9, characterized in that: The temperature inside the static separation tank and the catalyst mixing tank is in the range of 20°C lower than the temperature of the slurry bed reactor and the same as the temperature of the slurry bed reactor; An activated catalyst product tank (10) is arranged between the gas-solid fluidized bed activation reactor (9) and the third lower connecting pipe (11), wherein the temperature inside the activated catalyst product tank (10) is in the range of 20°C lower than the temperature of the slurry bed reactor to the same as the temperature of the slurry bed reactor, and the pressure is 0.01-3MPa.

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