Catalyst lifting unit, continuous catalytic reforming device and continuous catalytic reforming reaction method

Abstract

The invention relates to a catalyst lifting unit, a continuous catalytic reforming device and a continuous catalytic reforming reaction method, the lifting unit comprises a first lifting pipe and an expanded pipe which are communicated in sequence, and the diameter of the expanded pipe is larger than that of the first lifting pipe; the included angle alpha between the expanding pipe and the first lifting pipe is 135-179 degrees; and the pipe wall of the expanding pipe is connected with a collecting part. According to the lifting unit disclosed by the invention, a mini-ball catalyst and a large amount of ultrahigh-carbon-content catalysts in the catalyst can be separated out of a catalyst circulating system under the normal circulation condition of the catalyst; the inactivated'mini-ball 'catalyst is discharged out of a catalyst circulating system, so that the number of ultrahigh-carbon-content catalysts entering a scorching area of the regenerator is greatly reduced, and the phenomena of scorching overtemperature of the regenerator, damage to components in the regenerator, generation of the'mini-ball' catalyst and the like are reduced; the safe and stable operation of the continuous reforming device is facilitated.

Description

Technical Field

[0001] The present disclosure relates to the technical field of classification devices, and in particular to a catalyst lifting unit, a continuous catalytic reforming device, and a continuous catalytic reforming reaction method. Background Art

[0002] Catalytic reforming is a key process in the secondary processing of petroleum, aimed at producing high-octane gasoline and aromatic components. Continuous reforming units involve the continuous circulation of catalyst within a reaction-regeneration system. The catalyst lifting unit is a key component in enabling the continuous circulation of catalyst within the reaction-regeneration system. The catalyst flows downward through the reactor and regenerator by gravity, and then is lifted to the next higher point in the vessel by a lifting unit. The lifting gas between reactors is hydrogen, while the lifting gas between the last reactor and the regenerator is nitrogen. The lifting unit consists of a lifter and a riser. The lifter is the junction where the lifting gas and the transported catalyst meet, controlling the amount of catalyst transported and providing sufficient pneumatic force for gas transport. The riser is a wear-resistant metal circular tube. The catalyst is transported upward by the lifting gas, remaining in a dilute phase within the riser.

[0003] Catalysts accumulate carbon in the reaction system, typically with a carbon content of less than 6%. Continuous reforming units contain "dead zones," or areas of stagnant flow, at varying locations and volumes. Catalysts within these zones accumulate high levels of carbon, with some exhibiting carbon deposits exceeding 30%, termed ultra-high carbon content catalysts. The volume of these "dead zones" varies depending on reactor design and operating conditions, but is generally greater than 1%. Fluctuations in the catalyst circulation system can cause ultra-high carbon content catalysts to escape these zones and enter the regenerator. Carbon deposits cannot be completely burned off in the burnout zone, and upon entering the regenerator's oxychlorination zone, contact with gases containing a higher oxygen content can cause overheating in the zone. This can damage regenerator components and deactivate the ultra-high carbon content catalyst and nearby catalysts due to the high temperatures. The catalyst's carrier crystal phase changes from γ-alumina to α-alumina, and the catalyst's diameter decreases to 75% to 82% of its original size, resulting in a reduction in volume. These catalysts are often referred to as "mini-ball" catalysts.

[0004] Given these serious issues, when reloading catalyst after unloading and refilling this significantly high-carbon-content catalyst into the catalyst cycle, a short-term method is typically employed, where the high-oxygen-content gas is not introduced into the regenerator oxychlorination zone. After three catalyst cycles, high-oxygen-content gas is then introduced into the oxychlorination zone for normal regenerator operation, which can take over nine days. This method is unable to separate the small amount of "mini-ball" catalyst within the catalyst. During maintenance shutdowns or when the entire catalyst is removed from the reactor to address unit issues, an increasing number of continuous reforming units are employing specialized equipment from specialized companies to perform on-site catalyst density grading. This allows for the separation of ultra-high-carbon-content catalyst, "mini-ball" catalyst, and broken catalyst from the catalyst.

[0005] CN106269506A discloses a negative pressure fluidized windmill type physical classification device for reforming catalysts. The device needs to be in a shutdown state to unload the catalyst to the outside of the reactor for classification. In this device, the catalyst to be classified falls vertically downward, and the hot air acts as a separation power to move horizontally. The catalysts of different densities are blown into different areas to complete the separation of crushed particle catalysts, ultra-high carbon catalysts, "mini ball" catalysts, and normal catalysts. This density classification catalyst method has been actually used in some devices. It is obvious that the ultra-high carbon content catalyst enters the catalyst circulation system due to the unloading and reloading of the catalyst, while the situation where the ultra-high carbon content catalyst enters the catalyst circulation system due to the fluctuation of the device is even more difficult to detect and prevent. Therefore, even if the device management personnel are cautious in the burning operation, there are still many devices with different frequencies of overheating damage to the regenerator internal components and the generation of "mini ball" catalysts due to the ultra-high carbon content catalyst entering the regenerator burning area. Summary of the Invention

[0006] The purpose of the present disclosure is to provide a catalyst lifting unit, a continuous catalytic reforming device and a method for continuous catalytic reforming reaction, wherein the lifting unit can separate the "mini ball" catalyst and a large amount of ultra-high carbon content catalyst in the catalyst from the catalyst circulation system under normal catalyst circulation conditions; discharge the deactivated "mini ball" catalyst from the catalyst circulation system, and greatly reduce the amount of ultra-high carbon content catalyst entering the regenerator burnt zone.

[0007] In order to achieve the above-mentioned object, the present disclosure provides a catalyst lifting unit in a first aspect, comprising a first lifting pipe and an expanding pipe connected in sequence;

[0008] The diameter of the expanding tube is greater than that of the first rising tube; the angle α between the expanding tube and the first rising tube is 135° to 179°; and a collecting portion is connected to the tube wall of the expanding tube.

[0009] Optionally, the included angle α between the expansion pipe and the first riser is 155° to 175°.

[0010] Optionally, the catalyst lifting unit further includes a second lifting pipe, and the expansion pipe is connected between the first lifting pipe and the second lifting pipe; the second lifting pipe is arranged at an angle to the expansion pipe, and the angle β between the expansion pipe and the second lifting pipe is 135° to 179°, preferably 155° to 175°.

[0011] Optionally, the first riser and the second riser are arranged in parallel; the first riser and the second riser have the same diameter.

[0012] Optionally, the diameter D2 of the expanded tube and the diameter D1 of the first riser satisfy the relationship shown in formula (1):

[0013] 1.04≤D2 / D1≤1.1, formula (1).

[0014] Optionally, the length of the first riser is greater than 3.7 m; the length of the expansion pipe is 1 to 3 m.

[0015] Optionally, the outlet end of the collecting portion and the first riser are located on the same side of the expanding tube; the collecting portion is formed as a reducing tube with a cross-sectional area that shrinks from the inlet to the outlet; the inlet diameter of the collecting portion is 1 to 2 times the diameter of the first riser;

[0016] The lifting unit further includes a collecting hopper, which is arranged below the collecting portion and is in sealed communication with the outlet end of the collecting portion through a collecting pipeline;

[0017] Optionally, the collecting part is further connected to a supplementary gas pipeline; a V valve and a B valve are provided on the collecting pipeline; and the collecting hopper is further connected to a venting pipeline and a protective gas pipeline.

[0018] A second aspect of the present disclosure provides a method for performing a continuous catalytic reforming reaction using the lifting unit described in the first aspect of the present disclosure, the method comprising: allowing the reforming catalyst to enter the lifting unit from the inlet of the first lifting pipe under the action of hydrogen lifting gas.

[0019] Optionally, the method further comprises: collecting materials containing abnormal catalysts from a collection portion; the abnormal catalysts include mini-ball catalysts and / or ultra-high carbon content catalysts; and the collection is performed intermittently;

[0020] Optionally, the material in the collecting portion is discharged into a collecting hopper, and during the discharge, hydrogen is added to the expanding tube, and the pressure of the collecting hopper is made the same as the pressure of the collecting portion;

[0021] Optionally, after all the catalysts pass through the expanded diameter section tube, the material is collected from the collecting portion.

[0022] A third aspect of the present disclosure provides a continuous catalytic reforming device comprising the lifting unit described in the first aspect of the present disclosure.

[0023] Through the above technical solution, the present disclosure provides a diameter expansion tube on the normal riser to change the velocity of the lifting gas, and the speed of the catalyst moving relative to the diameter expansion tube changes accordingly. The difference in the relative speed of different catalysts is used to separate the "mini ball" catalyst and the ultra-high carbon content catalyst from the catalyst. The lifting unit of the present disclosure can separate the "mini ball" catalyst and a large amount of ultra-high carbon content catalyst from the catalyst circulation system under normal catalyst circulation conditions; discharge the deactivated "mini ball" catalyst from the catalyst circulation system, significantly reducing the amount of ultra-high carbon content catalyst entering the regenerator burn zone, thereby reducing the phenomena of regenerator burnout and overheating, damage to regenerator internal components, and the formation of "mini ball" catalyst; and is conducive to the safe and stable operation of the continuous reforming device.

[0024] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] The accompanying drawings are used to provide a further understanding of the present disclosure and constitute a part of the specification. Together with the following detailed description, they are used to explain the present disclosure but do not constitute a limitation of the present disclosure. In the accompanying drawings:

[0026] Figure 1 It is the lifting unit in Example 1 of the present disclosure.

[0027] Figure 2 Schematic diagram of the catalyst grading device in Comparative Example 1 of the present disclosure.

[0028] Description of Reference Numerals

[0029] Figure 1 Middle: 1: reforming catalyst; 2: first riser; 3: expansion pipe; 4: collecting hopper; 5: catalyst discharge line; 6: make-up gas line; 7: protective gas line; 8: vent line; 9: second riser; 10: collecting section; 11: V-valve; 12: B-valve; D1: diameter of first riser; D2: diameter of expansion pipe.

[0030] Figure 2Middle: 21: Lifting machine; 22: Grading silo; 23: Electromagnetic unloading valve; 24: Balanced feeder; 25: Electric heating air area; 26: Hot air distribution and guiding area; 27: Control area; 28: Grading adjustment plate; 29: First induced draft area; 30: Second induced draft area; 31: Coarse dust collection area; 32: Low carbon catalyst collection area; 33: Small particle low carbon catalyst collection area; 34: High carbon catalyst collection area; 35: Dwarf ball collection area. DETAILED DESCRIPTION

[0031] The following describes the specific embodiments of the present disclosure in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present disclosure and are not intended to limit the present disclosure.

[0032] A first aspect of the present disclosure provides a catalyst lifting unit, comprising a first lifting pipe and an expanding pipe connected in sequence;

[0033] The diameter of the expanding tube is greater than that of the first rising tube; the angle α between the expanding tube and the first rising tube is 135° to 179°; and a collecting portion is connected to the tube wall of the expanding tube.

[0034] The present invention changes the velocity of the hydrogen lifting gas by arranging an expansion pipe between normal lifting pipes. The velocity of the lifting gas decreases after entering the expansion pipe. The reduced lifting gas velocity is less than the free settling velocity of the "mini ball" catalyst and the ultra-high carbon content catalyst. The abnormal catalyst generates a downward acceleration and falls into the collection part in a parabolic motion. The normal catalyst continues to be lifted under the action of the lifting gas, thereby separating the "mini ball" catalyst and the ultra-high carbon content catalyst in the catalyst. The lifting unit of the present invention can separate the "mini ball" catalyst and a large amount of ultra-high carbon content catalyst from the catalyst circulation system under normal catalyst circulation conditions; discharge the deactivated "mini ball" catalyst from the catalyst circulation system, greatly reducing the amount of ultra-high carbon content catalyst entering the regenerator burn zone, thereby reducing the phenomena of regenerator burnout and overheating, regenerator internal component damage, "mini ball" catalyst generation, etc.; and is conducive to the safe and stable operation of the continuous reforming device.

[0035] In the present disclosure, the diameter refers to the inner diameter of the riser or the expander. The ultra-high carbon content catalyst in the present disclosure refers to a catalyst with a carbon content of 30% by mass or more.

[0036] According to one embodiment of the present disclosure, the angle α between the expansion tube and the first riser is 155° to 175°. This embodiment facilitates the passage of abnormal catalyst into the collection section after entering the expansion tube, thereby facilitating its discharge from the catalyst circulation system while avoiding the loss of normal catalyst. Abnormal catalysts in this disclosure refer to "mini-ball" catalysts and ultra-high carbon content catalysts.

[0037] According to one embodiment of the present disclosure, the catalyst lifting unit further includes a second lifting pipe, and the expanding pipe is connected between the first lifting pipe and the second lifting pipe; the second lifting pipe is arranged at an angle to the expanding pipe, and the angle β between the expanding pipe and the second lifting pipe is 135° to 179°, preferably 155° to 175°. In a further embodiment, the catalyst lifting unit includes a first lifting pipe, an expanding pipe and a second lifting pipe connected in sequence. The above embodiment is conducive to allowing the abnormal catalyst to enter the collection part after entering the expanding pipe, thereby being more conducive to the discharge of the catalyst circulation system, and the normal catalyst can continue to be lifted.

[0038] According to the present disclosure, the connection between the expanded tube and the first riser, the connection between the expanded tube and the collecting part, and the connection between the expanded tube and the second riser are all set to be arc-shaped, which reduces the friction between the catalyst and the inside of the tube and avoids catalyst breakage.

[0039] According to one embodiment of the present disclosure, the first riser and the second riser are arranged in parallel; the first riser and the second riser have the same diameter. This embodiment facilitates the transfer of abnormal catalyst from the expansion tube to the collection section, thereby effectively discharging the catalyst circulation system. Normal catalyst can continue to be lifted, while also avoiding loss of normal catalyst.

[0040] According to one embodiment of the present disclosure, the diameter D2 of the expansion tube and the diameter D1 of the first riser satisfy the relationship shown in formula (1): 1.04≤D2 / D1≤1.1, formula (1). The above embodiment is conducive to allowing abnormal catalyst to enter the collection part after entering the expansion tube, which is conducive to better discharge of the catalyst circulation system, significantly reducing the amount of ultra-high carbon catalyst entering the regenerator burn zone, while avoiding the loss of normal catalyst, and thus reducing the phenomenon of regenerator burnout overheating, regenerator internal component damage, and "mini ball" catalyst generation.

[0041] According to one embodiment of the present disclosure, the length of the first riser is more than 3.7m, and the length of the expansion pipe is 1 to 3m. In one embodiment, the length of the second riser can be more than 0m. In actual industrial production, the total length of the catalyst lifting is about 30 to 80m. After the lengths of the first riser and the expansion pipe are determined, those skilled in the art can adjust the length of the second riser according to the actual needs of the device. The above embodiment is conducive to lifting the reforming catalyst to a certain height, with a certain movement speed relative to the riser. After entering the expansion pipe, the difference in the relative movement speed of the normal catalyst and the abnormal catalyst in the expansion pipe is utilized to better discharge the abnormal catalyst from the catalyst circulation system, and the normal catalyst continues to be lifted, avoiding the loss of the normal catalyst and avoiding affecting the lifting and circulation of the normal catalyst.

[0042] According to one embodiment of the present disclosure, the outlet end of the collecting section and the first riser are located on the same side of the expanding tube; the collecting section is formed as a reducing tube whose cross-sectional area shrinks from the inlet to the outlet; the inlet diameter of the collecting section is 1 to 2 times the diameter of the first riser; the lifting unit also includes a collecting hopper, which is arranged below the collecting section and is tightly connected to the outlet end of the collecting section through a collecting pipeline. In the present disclosure, the inlet diameter of the collecting section refers to the diameter of the connection between the collecting section and the first riser. The above embodiment is conducive to the abnormal catalyst falling into the collecting section in time and being concentrated downward under the action of gravity, which is more conducive to the discharge of the catalyst circulation system.

[0043] According to one embodiment of the present disclosure, the collection section is further connected to a supplementary gas line; the supplementary gas line is provided with a valve; the collection line is provided with a V valve and a B valve; and the collection hopper is further connected to a vent line and a protective gas line. The installation and use of the collection line are well known to those skilled in the art and will not be described in detail here.

[0044] A second aspect of the present disclosure provides a method for performing a continuous catalytic reforming reaction using the lifting unit described in the first aspect of the present disclosure, the method comprising: allowing the reforming catalyst to enter the lifting unit from the inlet of the first lifting pipe under the action of hydrogen lifting gas.

[0045] The method disclosed herein does not specifically limit the flow rate of the hydrogen lifting gas and can be a conventional setting in the field. The reforming catalyst is lifted under the action of the hydrogen lifting gas. Within the specific length and inner diameter ratio range of the first lifting tube and the expansion tube, the gas velocity of the hydrogen in the first lifting tube can reach more than 14 m / s, so that the normal catalyst and the abnormal catalyst in the catalyst have a certain movement speed relative to the lifting tube respectively. After the catalyst enters the expansion tube, the lifting gas speed changes. The difference in the movement speed of different catalysts relative to the expansion tube is used to separate the "mini ball" catalyst and the ultra-high carbon content catalyst in the catalyst.

[0046] According to one embodiment of the present disclosure, the first riser is arranged vertically. In a further embodiment, the first riser, the expansion tube, and the second riser are arranged sequentially from bottom to top. This embodiment facilitates density classification under normal operating conditions of the continuous reformer by utilizing the difference in movement speed of normal and abnormal catalysts relative to the expansion tube.

[0047] According to one embodiment of the present disclosure, the method further includes: collecting materials containing abnormal catalysts from a collection section; the abnormal catalysts include mini-ball catalysts and ultra-high carbon content catalysts; the collection is an intermittent operation; in one embodiment, the collection section is also connected to a supplementary gas pipeline, and a valve is provided on the supplementary gas pipeline, so that the material in the collection section is discharged into the collection hopper. During the discharge, hydrogen can be added to the expansion tube through the supplementary gas pipeline, and the pressure of the collection hopper is made the same as the pressure of the collection section. The above embodiment is conducive to discharging abnormal catalysts from the catalyst circulation system while avoiding affecting the circulation of normal catalysts.

[0048] According to one embodiment of the present disclosure, the method further includes collecting the material from the collecting portion after all the catalysts have passed through the expanded diameter section tube.

[0049] According to one embodiment of the present disclosure, the method further includes stopping the supply of oxygen to the oxychlorination zone of the regenerator when the catalyst circulation system exhibits significant fluctuations. This embodiment allows the removal of abnormal catalyst from the catalyst circulation system without shutting down the continuous catalytic reforming unit, thereby improving reaction efficiency and reducing operating costs.

[0050] A third aspect of the present disclosure provides a continuous catalytic reforming apparatus comprising the lifting unit described in the first aspect of the present disclosure. In one embodiment, the lifting unit is used between two reactors, and the lifting gas is hydrogen. The remaining components of the continuous catalytic reforming apparatus described in the present disclosure, such as the regenerator and heating furnace, are conventional in the art and are not described in detail here.

[0051] The present disclosure is described in detail below with reference to specific embodiments. The following embodiments will help those skilled in the art to further understand the present disclosure, but are not intended to limit the present disclosure in any form.

[0052] Example 1

[0053] Taking the countercurrent continuous catalytic reforming unit as an example, a lifting unit is set between the first reactor and the second reactor, such as Figure 1 As shown, the catalyst lifting unit includes, from bottom to top, a first riser 2, an expansion tube 3, and a second riser 9; the diameter D2 of the expansion tube is larger than the diameter D1 of the first riser, the diameter D2 of the expansion tube is 70.4 mm, the diameter D1 of the first riser is 66.4 mm, and the ratio D2 / D1 is 1.06; the angle α between the expansion tube and the first riser is 175°, the first riser and the second riser are arranged in parallel and have the same diameter; the length of the expansion tube is 2 m, and the length of the first riser is 4m, and the rest is the second lifting pipe; the lifting unit also includes a collecting hopper 4, which is arranged below the collecting part 10 and is tightly connected to the outlet end of the collecting part through a collecting pipeline, and the collecting hopper is also connected to a venting pipeline 8 and a protective gas pipeline 7; the collecting part is also connected to a supplementary gas pipeline 6; a V valve 11 and a B valve 12 are provided on the collecting pipeline; the collecting part is formed as a reducing pipe with a cross-sectional area that shrinks from the inlet to the outlet; the inlet diameter of the collecting part is 100mm, which is 1.5 times the diameter of the first lifting pipe.

[0054] The flow rate of hydrogen lifting gas in the first riser is 175m 3 / h, the hydrogen velocity in the first riser is 14.02m / s, and the catalyst circulation rate is 1.2m 3 / h, the ratio of the volume flow rate of catalyst in the riser to the volume flow rate of lifting gas is 0.007, which is dilute phase transport. The movement between catalysts is relatively independent. The ratio of the catalyst diameter to the inner diameter of the riser is 0.02, and the influence of the tube wall on the lifting can be ignored.

[0055] The reforming catalyst 1 is allowed to enter the lifting unit from the inlet of the first riser under the action of hydrogen lifting gas. When the reforming catalyst reaches the highest point A of the first riser, four representative catalyst types are selected for analysis. The specific catalyst data are shown in Table 1 below. At point A, the "mini ball" catalyst I moves at a speed of 0.1 m / s relative to the riser; the ultra-high carbon content catalyst II moves at a speed of 1.45 m / s relative to the riser; the catalyst III moves at a speed of 3.34 m / s relative to the riser; and the catalyst IV moves at a speed of 3.95 m / s relative to the riser. After the reforming catalyst passes point A, it enters the expansion pipe. After the expansion, the gas velocity of the hydrogen lifting gas is reduced to 12.48 m / s. The free settling velocity of the "mini ball" catalyst I and the ultra-high carbon content catalyst II is greater than the lifting hydrogen gas velocity, resulting in a downward acceleration, and falls into the collection part along a parabolic path. The normal catalyst is normally lifted under the lifting gas and enters the second riser.

[0056] When the collection section is full of abnormal catalyst, the "mini ball" catalyst and the ultra-high carbon content catalyst separated from the collection section of the riser are discharged into the collection hopper. During the discharge, hydrogen is added to the expansion tube to maintain the pressure. The pressure in the collection hopper needs to be the same as the pressure in the collection section of the riser.

[0057] In the event of significant fluctuations in the catalyst circulation system, a short period of operation without oxygen in the oxychlorination zone of the regenerator is employed. Once all catalyst has circulated through the separation zone of the lifting unit disclosed herein (approximately 3-4 days), the "mini-ball" catalyst and any ultra-high carbon content can be separated from the circulation system.

[0058] In the case where the unaware ultra-high carbon content catalyst enters the regenerator, more than 50% of the unaware ultra-high carbon content catalyst can be reduced from entering the regenerator.

[0059] Example 2

[0060] The embodiment is the same as that of Example 1, except that in this embodiment, the ratio D2 / D1 of the diameter D2 of the expanded tube to the diameter D1 of the first riser is 1.15, and the diameter D2 of the expanded tube is 76.41 mm.

[0061] The flow rate of hydrogen lifting gas in the first riser is 175m 3 / h, the hydrogen velocity in the first riser is 14.02m / s, and the catalyst circulation rate is 1.2m 3 / h, the ratio of the volume flow rate of catalyst in the riser to the volume flow rate of lifting gas is 0.007, which is dilute phase transport. The movement between catalysts is relatively independent. The ratio of the catalyst diameter to the inner diameter of the riser is 0.02, and the influence of the tube wall on the lifting can be ignored.

[0062] The reforming catalyst was allowed to enter the lifting unit from the inlet of the first riser under the action of hydrogen lifting gas. When the reforming catalyst reached the highest point A of the first riser, four representative catalyst types were selected for analysis. Specific catalyst data are shown in Table 1 below. At point A, the relative movement speed of the "mini-ball" catalyst I was 0.1 m / s; the relative movement speed of the ultra-high carbon content catalyst II was 1.45 m / s; the relative movement speed of the catalyst III was 3.34 m / s; and the relative movement speed of the catalyst IV was 3.95 m / s. After the reforming catalyst passed point A, it entered the expansion tube. After the expansion, the gas velocity of the hydrogen lifting gas was reduced to 10.60 m / s. The free settling velocity of the "mini-ball" catalyst I and the ultra-high carbon content catalyst II was greater than the hydrogen lifting gas velocity, resulting in downward acceleration, and falling into the collection section along a parabolic path. Among the normal catalysts, the free settling velocity of catalyst III was greater than the hydrogen lifting gas velocity, resulting in downward acceleration, and falling into the collection section, affecting the lifting of some normal catalysts.

[0063] Example 3

[0064] The same as Example 1, except that the angle α between the expansion pipe and the first riser is 145°. The horizontal displacement of the catalyst in the riser is greater than that in Example 1, and the friction of the catalyst in the expansion pipe is greater than that in Example 1.

[0065] Comparative Example 1

[0066] In case of obvious fluctuation in the catalyst circulation system, the continuous reforming unit will be shut down and a professional catalyst density classification company will be employed to Figure 2 The grading device shown performs off-site density classification on all catalysts. The process flow is as follows: a catalyst-filled drum is lifted by a material lifter 21 into a top grading silo 22. An electromagnetic discharge valve 23 at the bottom of the grading silo controls the catalyst's weight flow. When the electromagnetic discharge valve 23 is opened to a certain degree, the catalyst flows down by weight onto a balanced feeder 24, which evenly distributes the catalyst. The first and second induced draft fans simultaneously induced air. Because the system is sealed on all sides, only the electrically heated air zone 25 is open. When the induced draft fans are operating, hot air flows through the catalyst drop zone, imparting force to the dropped catalyst, causing it to move laterally. Catalysts of similar particle size and low density are driven in the same direction by the lateral force of the hot air, causing the dropped catalyst to fall to different locations for collection. After classification, catalysts with a carbon content below 6% are reloaded in situ. "Mini-ball" catalysts, catalysts with a carbon content greater than 6%, and broken catalysts are all recovered. After loading, normal production operations resume.

[0067] The staging device cannot avoid the situation where catalyst with extremely high carbon content enters the regenerator without being noticed.

[0068] Comparative Example 2

[0069] In the event of significant fluctuations in the catalyst circulation system, a short-term operation of the regenerator oxychlorination zone without oxygen is employed. Typically, after three catalyst cycles, high-oxygen gas is introduced into the regenerator oxychlorination zone for normal regenerator operation, which takes more than nine days. This method prevents ultra-high carbon content catalyst from entering the regenerator oxychlorination zone. However, it is not possible to separate the small amount of "mini-ball" catalyst within the catalyst.

[0070] This method cannot avoid the situation where catalyst with extremely high carbon content enters the regenerator without being noticed.

[0071] Table 1

[0072]

[0073] The separation conditions of the catalysts in the above examples and comparative examples are listed in Table 2.

[0074] Table 2

[0075]

[0076] As can be seen from the data in Table 2, in the event of significant fluctuations in the catalyst circulation system, the present disclosure allows the "mini-ball catalyst" and ultra-high carbon content catalyst to be discharged from the catalyst circulation system without shutting down the continuous catalytic reforming unit, significantly reducing the amount of ultra-high carbon content catalyst entering the regenerator's burn zone, further reducing the risk of regenerator burnout, overheating, damage to regenerator internal components, and the formation of "mini-ball" catalyst. In situations where ultra-high carbon content catalyst may enter the catalyst circulation system undetectably due to unit fluctuations, the present disclosure can significantly reduce the amount of ultra-high carbon content catalyst entering the regenerator's burn zone while simultaneously separating the "mini-ball" catalyst, ensuring safe and stable operation of the regenerator in the continuous catalytic reforming unit.

[0077] Comparison of Examples 1 and 2 shows that within the preferred range of the diameter ratio of the expanded tube to the first riser, the separation of abnormal catalyst is effective while minimizing the impact on normal catalyst. Comparison of Examples 1 and 3 shows that within the preferred range of the angle between the expanded tube and the first riser, the separation of abnormal catalyst is effective while minimizing wear on the expanded tube wall and normal catalyst.

[0078] The preferred embodiments of the present disclosure are described in detail above in conjunction with the accompanying drawings. However, the present disclosure is not limited to the specific details of the above embodiments. Within the technical concept of the present disclosure, various simple modifications can be made to the technical solutions of the present disclosure, and these simple modifications all fall within the scope of protection of the present disclosure.

[0079] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the present disclosure will not further describe various possible combinations.

[0080] In addition, the various embodiments of the present disclosure may be arbitrarily combined, and as long as they do not violate the concept of the present disclosure, they should also be regarded as the contents disclosed by the present disclosure.

Claims

1. A catalyst upgrading unit, characterized in that: It includes a first riser and an expansion pipe connected in sequence; The diameter of the expanding tube is greater than that of the first rising tube; the angle α between the expanding tube and the first rising tube is 135° to 179°; and a collecting portion is connected to the tube wall of the expanding tube.

2. The lifting unit according to claim 1, wherein: The included angle α between the expanded tube and the first rising tube is 155° to 175°.

3. The lifting unit according to claim 1, wherein: The catalyst lifting unit also includes a second lifting pipe, and the expansion pipe is connected between the first and second lifting pipes; the second lifting pipe is arranged at an angle to the expansion pipe, and the angle β between the expansion pipe and the second lifting pipe is 135° to 179°, preferably 155° to 175°.

4. The lifting unit according to claim 3, wherein: The first riser and the second riser are arranged in parallel; the first riser and the second riser have the same diameter.

5. The lifting unit according to claim 1, wherein: The diameter D2 of the expanded tube and the diameter D1 of the first riser satisfy the relationship shown in formula (1): 1.04≤D2 / D1≤1.1, formula (1).

6. The lifting unit according to claim 1, wherein: The length of the first riser is more than 3.7 m; the length of the expansion pipe is 1 to 3 m.

7. The lifting unit according to any one of claims 1 to 6, wherein: The outlet end of the collecting section and the first riser are located on the same side of the expanding tube; the collecting section is formed as a reducing tube with a cross-sectional area that shrinks from the inlet to the outlet; the inlet diameter of the collecting section is 1 to 2 times the diameter of the first riser; The lifting unit further includes a collecting hopper, which is arranged below the collecting portion and is in sealed communication with the outlet end of the collecting portion through a collecting pipeline; Optionally, the collecting part is further connected to a supplementary gas pipeline; a V valve and a B valve are provided on the collecting pipeline; and the collecting hopper is further connected to a venting pipeline and a protective gas pipeline.

8. A method for continuous catalytic reforming reaction using the lifting unit according to any one of claims 1 to 7, characterized in that: The method includes: allowing the reforming catalyst to enter the lifting unit from the inlet of the first lifting pipe under the action of hydrogen lifting gas.

9. The method according to claim 8, wherein The method further comprises: collecting materials containing abnormal catalysts from a collection portion; the abnormal catalysts include mini-ball catalysts and / or ultra-high carbon content catalysts; and the collection is performed intermittently; Optionally, the material in the collecting portion is discharged into a collecting hopper, and during the discharge, hydrogen is added to the expanding tube, and the pressure of the collecting hopper is made the same as the pressure of the collecting portion; Optionally, after all the catalysts pass through the expanded diameter section tube, the material is collected from the collecting portion.

10. A continuous catalytic reforming device comprising the lifting unit according to any one of claims 1 to 7.

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