A dual-gas-flow catalyst reaction unit, device, system, and coupling method

Abstract

A double grain flow catalyst reaction unit, device, system and coupling method, comprising a first reactor with an inlet at the bottom and an outlet at the top end, a slanted pipe for feeding heavy and light granular catalysts is arranged on one side of the first reactor, the first reactor comprises a mixing buffer zone with an upper large and lower small conical structure in the longitudinal section at the lower part and a take-out control zone with an upper small and lower large conical structure in the longitudinal section at the upper part, the slanted pipe is communicated with the mixing buffer zone and the bottom end thereof is inclined downward to mix and feed the heavy and light granular catalysts to the bottom of the mixing buffer zone, and under the action of the lifting gas, the heavy and light granular catalysts form a uniform dense bed layer zone between the mixing buffer zone and the take-out control zone. The present application avoids the heavy granular catalyst from depositing to form a deposition zone at the bottom of the first reactor, mixes the heavy and light granular catalysts uniformly, and improves the heat transfer efficiency of the two.

Description

Technical Field

[0001] This invention relates to the field of dual-flow catalyst coupling technology, specifically a dual-flow catalyst reaction unit, apparatus, system, and coupling method. Background Technology

[0002] Most chemical reactions in fluidized bed reactors are accompanied by thermal effects, leading to significant changes in the bed temperature and causing the reaction temperature to deviate from the optimal temperature, ultimately resulting in poor conversion or product selectivity. Current technologies use gaseous or liquid-phase heat carriers to transfer the heat required for the chemical reaction or the excess heat generated by it into or out of the reactor via indirect heat transfer. The heated or deheated heat carrier is then transported to a heater or cooler for heating or cooling before being recycled back into the reactor. This method increases equipment investment costs, and the heat loss during heat carrier transport and the heating or cooling of the heat carrier itself result in energy waste.

[0003] Therefore, the patent applied for by the applicant in 2021 provides a dual-particle catalyst coupled catalysis method and reaction system, in which two chemical reactions occur in the same reaction system. Specifically, heavy particle catalyst and light particle catalyst are mixed in a first reactor. The heavy particle catalyst participates in the first chemical reaction, while the light particle catalyst provides or removes heat for the first chemical reaction, causing the light particle catalyst to cool down or heat up. This ensures the temperature of the reaction bed in the first reactor and also ensures that the light particle catalyst reaches the ideal temperature when entering the second reactor, achieving efficient heat utilization, avoiding heat waste, and reducing equipment investment. However, in practical applications, the heavy particle catalyst easily deposits at the bottom of the first reactor, forming a heavy particle catalyst deposition zone. The mixing effect of the heavy and light particle catalysts in the deposition zone is poor, resulting in low heat transfer efficiency for both. Even if the heavy and light particle catalysts are mixed uniformly in a certain proportion outside the first reactor and enter the first reactor, due to their different physical properties, the heavy particle catalyst will still deposit at the bottom of the first reactor after a period of operation, forming a deposition zone, resulting in low heat transfer efficiency for both. If the formation of a deposition zone is avoided simply by increasing the flow rate of the booster gas introduced into the first reactor, the light-particle catalyst will be blown out of the first reactor before completing heat transfer, resulting in low heat transfer efficiency between the two reactors. Summary of the Invention

[0004] To address the problem of uneven mixing of heavy and light particulate catalysts caused by the formation of a sedimentation zone at the bottom of the first reactor in existing technologies, this invention provides a dual-flow catalyst reaction unit, apparatus, system, and coupling method. This avoids the formation of a sedimentation zone at the bottom of the first reactor by heavy particulate catalysts, ensuring uniform mixing of heavy and light particulate catalysts and improving their heat transfer efficiency.

[0005] To achieve the above objectives, the specific solution adopted by the present invention is as follows: a dual-particle flow catalyst reaction unit, comprising a first reactor having an inlet at the bottom and an outlet at the top. The inlet includes an air inlet for supplying lifting gas into the first reactor and a feed inlet for supplying first reaction raw materials into the first reactor. An inclined pipe for introducing heavy particulate catalyst and light particulate catalyst is provided on one side of the first reactor. The first reactor includes a mixing buffer zone located at its lower part with a longitudinal section of a cone structure with a larger upper section and a smaller lower section located at its upper part with a longitudinal section of a cone structure with a smaller upper section and a larger lower section. The inclined pipe is connected to the mixing buffer zone and its bottom end is inclined downward to mix and send the heavy particulate catalyst and light particulate catalyst to the bottom of the mixing buffer zone. Under the action of the lifting gas, the heavy particulate catalyst and light particulate catalyst form a uniform dense phase bed zone between the mixing buffer zone and the carry-out control zone.

[0006] As an optimized solution for the above-mentioned dual-particle flow catalyst reaction unit: an inner conveying pipe with openings at both ends and extending along the height direction of the first reactor is provided in the carry-out control zone, and a supplementary gas pipe for introducing lifting gas into the carry-out control zone is provided on one side of the carry-out control zone near its bottom.

[0007] As another optimized solution for the above-mentioned dual-particle flow catalyst reaction unit: the top of the inner conveying pipe moves towards the center to form an inner constriction, and the bottom of the inner conveying pipe extends outward to form an outer expansion, with the bottom end of the outer expansion close to the interface of the uniform dense phase bed region.

[0008] As another optimized solution for the aforementioned dual-flow catalyst reaction unit, the inner delivery pipe, outlet, and inlet are coaxially arranged.

[0009] As another optimization scheme for the above-mentioned dual-particle catalyst reaction unit: the bottom of the mixing buffer is a spherical structure.

[0010] As another optimization of the above-mentioned dual-particle catalyst reaction unit: the bottom end of the inclined tube faces the air inlet.

[0011] As another optimization scheme for the above-mentioned dual-flow catalyst reaction unit: the acute angle formed by the inclined tube and the axis of the first reactor is 30-60°.

[0012] A dual-flow catalyst reaction device includes a reaction unit connected to a second reactor located above it and open at its top. The bottom of the second reactor is provided with a raw material inlet for introducing a second chemical reaction raw material into it. The reaction unit is the aforementioned reaction unit, and the second reactor is connected to the outlet of the first reactor.

[0013] A dual-flow catalyst reaction system includes a reaction device connected in series to form a closed loop, a settling tank located above the reaction device, and a regenerator unit located on one side of the reaction device. The reaction device is the aforementioned reaction device. The settling tank is connected to the outlet of a second reactor. The regenerator unit includes a first regenerator and a second regenerator that are interconnected, with the second regenerator located above the first regenerator. The first regenerator is connected to the settling tank. Both the first and second regenerators are connected to an inclined pipe. The bottom of the first regenerator is provided with an air inlet for introducing main air, allowing light particulate catalyst to enter the second regenerator while heavy particulate catalyst remains in the first regenerator.

[0014] As an optimized solution for the aforementioned dual-flow catalyst reaction system: the first regenerator is connected to the inclined tube via a first inclined tube, the second regenerator is connected to the inclined tube via a second inclined tube, and a flow control valve is provided on the first and second inclined tubes.

[0015] As another optimized solution for the above-mentioned dual-particle-flow catalyst reaction system: the settling tank and the first regenerator are connected by a waiting-to-regenerate inclined tube, and a waiting-to-regenerate valve is provided on the waiting-to-regenerate inclined tube. The deactivated heavy particle catalyst and light particle catalyst in the settling tank enter the first regenerator through the waiting-to-regenerate inclined tube.

[0016] As another optimized solution for the above-mentioned dual-particle catalyst reaction system: the bottom of the first regenerator is provided with a feed port for replenishing heavy particulate catalyst, and the bottom of the second regenerator is provided with a feed port for replenishing light particulate catalyst.

[0017] As another optimized solution for the aforementioned dual-particle-flow catalyst reaction system: the bottom end of the second regenerator is recessed towards its center to form a conical region, and the bottom end of the conical region is connected to the upper port of the first regenerator.

[0018] A dual-particle catalyst coupling method, based on a dual-particle catalyst reaction system according to claims 8-12, includes the following steps:

[0019] S1, the heavy particulate catalyst and the light particulate catalyst enter the first reactor through the regeneration unit. The heavy particulate catalyst is used to catalyze the first chemical reaction, so that the first reaction raw material is converted into the first reaction product. The light particulate catalyst is used to heat or remove heat from the first chemical reaction and then enters the second reactor, so that the second reaction raw material is converted into the second reaction product.

[0020] S2, the deactivated heavy particulate catalyst and light particulate catalyst are transported to the regeneration unit for regeneration after passing through the settler;

[0021] S3, the regenerated heavy particulate catalyst and light particulate catalyst enter the first reactor;

[0022] In S1, the flow direction of the heavy and light particulate catalysts entering the mixing buffer forms an acute angle of 20-70° with the axis of the first reactor, and the inflow velocity is 0.5-3 m / s. The velocity of the lift gas entering the first reactor through the inlet is 0.1-1 m / s. In S2, the make-up gas pipe introduces lift gas into the inner conveying pipe to ensure that the heavy particulate catalyst is carried out into the settler. The lift gas velocity in the make-up gas pipe is 1-10 m / s, and the direction is vertically upward. The velocity of the main air introduced into the bottom of the first regenerator is 0.5-2 m / s, and the direction is vertically upward.

[0023] As an optimized scheme of the above-mentioned dual-particle catalyst reaction coupling method: the particle size of the heavy particle catalyst is larger than that of the light particle catalyst, and the weight of the heavy particle catalyst is greater than that of the light particle catalyst.

[0024] As another optimized scheme of the above-mentioned dual-particle catalyst reaction coupling method: the heavy particle catalyst is regenerated in the first regenerator, and part of the light particle catalyst is regenerated in the first regenerator and the other part is regenerated in the second regenerator.

[0025] Compared with the prior art, the present invention has the following beneficial effects:

[0026] 1. This invention provides a dual-particle flow catalyst reaction unit, apparatus, system, and coupling method. Because the cross-section of the mixing buffer is a conical structure with a larger top and smaller bottom, the gas velocity at the bottom of the mixing buffer is greater than that at the top, thus avoiding the formation of a deposition zone of heavy particle catalyst at the bottom of the first reactor. Simultaneously, the gas velocity gradually decreases with increasing height within the mixing buffer, buffering the heavy and light particle catalysts that tilt into the bottom of the mixing buffer, reducing their impact on the dynamic balance of the heavy and light particle catalyst ratios. The heavy and light particle catalysts in the uniform dense-phase bed region are mixed evenly, improving the mixing effect.

[0027] 2. In this invention, the cross-section of the control zone is a conical structure with a smaller top and a larger bottom. As the height increases, the speed of the lifting gas gradually increases. At the same time, an inner conveying pipe is provided in the control zone. Lifting gas is introduced into the inner conveying pipe through the gas supply pipe, which can carry out the heavy particulate catalyst in the first reactor, so that the heavy particulate catalyst and the light particulate catalyst enter the second reactor together.

[0028] 3. In this invention, heavy particulate catalyst and light particulate catalyst are mixed and fed into the first regenerator. By controlling the main airflow velocity in the first regenerator, the heavy particulate catalyst is located in the first regenerator and the light particulate catalyst is located in the second regenerator. Finally, the heavy particulate catalyst regenerated in the first regenerator and the light particulate catalyst regenerated in the second regenerator are fed back into the first reactor in the required ratio, so as to realize the quantitative circulation of heavy particulate catalyst and light particulate catalyst, that is, the circulation amount of heavy particulate catalyst and light particulate catalyst can be controlled. Attached Figure Description

[0029] Figure 1 This is a schematic diagram of the reaction device of the present invention;

[0030] Figure 2 This is a schematic diagram of the reaction system of the present invention;

[0031] Reference numerals: 1. First reactor; 101. Carry-out control zone; 1011. Air supply pipe; 102. Dense phase bed zone; 103. Mixing buffer zone; 2. Second reactor; 3. Settler; 4. Waiting inclined tube; 5. First regenerator; 6. Second regenerator; 7. First inclined tube; 8. Second inclined tube; 9. Air inlet; 10. Feed inlet; 11. Raw material inlet; 12. Air inlet; 13. Inner conveying pipe; 1301. Outward expansion section; 1302. Inward contraction section; 14. Inclined tube. Detailed Implementation

[0032] The technical solution of the present invention will be further described in detail below with reference to specific embodiments. Parts not described or disclosed in detail in the following embodiments of the present invention should be understood as prior art known or should be known by those skilled in the art, such as the structure of the settling device, the structure of the first regenerator, and the structure of the second regenerator.

[0033] Example 1

[0034] A dual-particle flow catalyst reaction unit, such as Figure 1As shown, a first reactor 1 includes an inlet at the bottom and an outlet at the top. A first chemical reaction takes place inside the first reactor 1. In this embodiment, the reaction raw material is a first reactant used to participate in the first chemical reaction. The inlet includes an air inlet 9 for lifting gas into the first reactor 1 and a feed inlet 10 for the reactant to enter the first reactor 1. An inclined pipe 14 for introducing heavy particulate catalyst and light particulate catalyst is provided on one side of the first reactor 1. The inclined pipe 14 has a tubular structure. The heavy particulate catalyst participates in the first chemical reaction in the first reactor 1, converting the first reactant into the first reaction product. At the same time, the heavy particulate catalyst is deactivated, and the light particulate catalyst provides heat or removes heat for the first chemical reaction in the first reactor 1. The first reactor 1 has a circular cross-section. It includes a mixing buffer zone 103 at its lower part, with a longitudinal section that is larger at the top and smaller at the bottom (conical shape), and an extraction control zone 101 at its upper part, with a longitudinal section that is smaller at the top and larger at the bottom (conical shape). Specifically, the mixing buffer zone 103 is a frustum-shaped structure with a larger diameter at the top than at the bottom and a closed bottom with an open top. The velocity of the lifting gas within the mixing buffer zone 103 gradually decreases as the height of the first reactor 1 increases. The high velocity of the lifting gas at the bottom can drive the heavy catalyst particles upwards, preventing the formation of a deposition zone at the bottom of the first reactor 1. The extraction control zone 101 is a frustum-shaped structure with a smaller diameter at the top than at the bottom and open at both ends. The mixing buffer zone 103 and the extraction control zone 101 are coaxially arranged. The velocity of the lifting gas within the extraction control zone 101 gradually increases as the height of the first reactor 1 increases, facilitating the extraction of deactivated heavy catalyst particles from the first reactor 1. The air inlet 9 is located at the center of the bottom plate of the mixing buffer zone 103, which is closed at the bottom. The feed inlet 10 is located on the side wall of the mixing buffer zone 103 near the bottom plate. The bottom of the mixing buffer 103 is a spherical structure, that is, the base plate is a spherical structure.

[0035] An inclined pipe 14, connected to a mixing buffer 103 and tilted downwards at its bottom, mixes and delivers heavy and light particulate catalysts to the bottom of the mixing buffer 103. Under the action of a lifting gas, the heavy and light particulate catalysts form a uniform dense-phase bed region 102 between the mixing buffer 103 and the carry-out control zone 101. The mixed flow of heavy and light particulate catalysts enters the mixing buffer 103, which buffers the flow, reducing pressure fluctuations and thus minimizing the impact of the heavy and light particulate catalysts on the dynamic balance of their proportion within the first reactor 1. Simultaneously, the inclined pipe 14, introduced at the bottom of the mixing buffer 103, rises to the uniform dense-phase bed region 102 under the action of the lifting gas, increasing the disturbance in the mixing buffer 103 and preventing the formation of a deposition zone at the bottom of the first reactor 1. This also improves the mixing effect of the heavy and light particulate catalysts, thereby increasing the heat transfer efficiency between them.

[0036] In this embodiment, the cross-section of the uniform dense phase bed region 102 is a rectangular structure, with its top diameter equal to the bottom diameter of the carry-out control region 101 and its bottom diameter equal to the top diameter of the mixing buffer zone 103. The velocity of the lifting gas in the uniform dense phase bed region 102 is minimized, ensuring that the heavy particulate catalyst and the first reaction raw material have enough time to participate in the first chemical reaction. At the same time, it ensures that the light particulate catalyst can transfer heat sufficiently, thus improving the heat transfer efficiency.

[0037] In this embodiment, both the outlet and the inlet 9 are coaxially arranged with the first reactor 1.

[0038] The bottom end of the inclined tube 14 is located near the bottom of the mixing buffer 103. The acute angle formed by the inclined tube 14 and the axis of the first reactor 1 is 30-60°, so that the bottom end of the inclined tube 14 can face the bottom of the mixing buffer 103, avoiding the bottom end of the inclined tube 14 facing the side wall of the mixing buffer 103. In this embodiment, the bottom end of the inclined tube 14 faces the air inlet 9.

[0039] The above are the basic embodiments of the present invention. Further improvements, optimizations, and limitations can be made based on the above to obtain the following embodiments:

[0040] Example 2

[0041] This embodiment is an improvement on Embodiment 1. Its main structure is the same as Embodiment 1, but the improvement lies in the following: an inner conveying pipe 13, open at both ends and extending along the height of the first reactor 1, is provided within the carry-out control zone 101. In this embodiment, the inner conveying pipe 13 is a circular tubular structure and coaxial with the carry-out control zone 101. The height of the inner conveying pipe 13 is less than the height of the carry-out control zone 101, meaning the top end of the inner conveying pipe 13 is located below the outlet of the first reactor 1 and has a gap with the inner wall of the carry-out control zone 101; the diameter of the inner conveying pipe 13 is equal to the diameter of the outlet of the first reactor 1. A supplementary gas pipe 1011 for introducing lifting gas into the carry-out control zone 101 is provided near its bottom on one side of the carry-out control zone 101. Figure 1 As shown, the gas supply pipe 1011 introduces boosting gas into the carry-out control zone 101. The boosting gas is water vapor or dry gas, which further increases the speed of the boosting gas in the carry-out control zone 101, ensuring that the light particulate catalyst is carried out of the first reactor 1 while the deactivated heavy particulate catalyst is also carried out of the first reactor 1.

[0042] The top of the inner conveying pipe 13 converges towards the center to form an inwardly narrowed portion 1302, and the bottom of the inner conveying pipe 13 expands outward to form an outwardly widened portion 1301. The bottom end of the outwardly widened portion 1301 is close to the interface of the uniform dense phase bed region 102. It should be noted that the interface of the uniform dense phase bed region 102 is located below the top of the dense phase bed region 102, and the bottom end of the outwardly widened portion 1301 extends into the uniform dense phase bed region 102 and is located above the interface of the uniform dense phase bed region 102, further ensuring that the booster gas carries the deactivated heavy particulate catalyst out of the first reactor 1.

[0043] Example 3

[0044] A dual-flow catalyst reactor includes a reaction unit connected to a second reactor 2 located above it and open at its top. The bottom of the second reactor 2 has a feed inlet 11 for introducing a second chemical reaction raw material. The reaction unit is the same as described in Example 2 above. The second reactor 2 is connected to the outlet of the first reactor 1. Figure 1 As shown, the second reactor 2 is a tubular structure with an inner diameter equal to the outlet diameter of the first reactor 1. The second reactor 2 is coaxially arranged with the first reactor 1 and extends along its height. A raw material inlet 11 for introducing the second reaction raw material is located near the outlet of the first reactor 1 in the second reactor 2. A second chemical reaction takes place inside the second reactor 2, where light particulate catalyst participates in the second chemical reaction, converting the second reaction raw material into the second reaction product. Simultaneously, the light particulate catalyst is deactivated. Under the action of the lifting gas, the first chemical product, the second chemical product, the deactivated heavy particulate catalyst, and the deactivated light particulate catalyst are carried out of the second reactor 2.

[0045] Example 4

[0046] A dual-flow catalyst reaction system, such as Figure 2 As shown, the reactor includes a reaction device connected in series to form a closed loop, a settling tank 3 located above the reaction device, and a regenerator unit located on one side of the reaction device. The reaction device is the same as the one described in Example 3 above. The settling tank 3 is connected to the outlet of the second reactor 2. The first chemical product, the second chemical product, the deactivated heavy particulate catalyst, and the deactivated light particulate catalyst in the reaction device enter the settling tank 3 under the action of the lifting gas. After being separated by the settling tank 3, the deactivated heavy particulate catalyst and the light particulate catalyst are mixed and enter the regeneration unit. The regeneration unit is used to regenerate the deactivated heavy particulate catalyst and the deactivated light particulate catalyst, and sends the regenerated heavy particulate catalyst and the light particulate catalyst into the first reactor 1 to realize the circulation of the heavy particulate catalyst and the light particulate catalyst.

[0047] The regenerator unit includes a first regenerator 5 and a second regenerator 6 located on the left side of the first reactor 1 and connected to each other, with the second regenerator 6 located above the first regenerator 5; the first regenerator 5 is connected to the settling tank 3, and both the first regenerator 5 and the second regenerator 6 are connected to the inclined pipe 14; the bottom of the first regenerator 5 is provided with an air inlet 12 for introducing the main air, so that the light particulate catalyst enters the second regenerator 6 and the heavy particulate catalyst remains in the first regenerator 5. The deactivated heavy and light particulate catalysts separated from the settling tank 3 enter the first regenerator 5. Under the action of the main airflow, the deactivated heavy and light particulate catalysts are regenerated. At the same time, the heavy particulate catalyst remains in the first regenerator 5, while the deactivated light particulate catalyst and part of the regenerated light particulate catalyst enter the second regenerator 6, thus achieving the separation of the heavy and light particulate catalysts. Then, the heavy particulate catalyst enters the inclined tube 14 through the first regenerator 5 in the amount required by the reaction device, and the light particulate catalyst enters the inclined tube 14 through the second regenerator 6 in the amount required by the reaction device. After mixing in the inclined tube 14, they enter the mixing buffer 103, thus achieving the quantitative circulation of the heavy and light particulate catalysts in the reaction system.

[0048] Specifically, such as Figure 2 As shown, the first regenerator 5 is connected to the inclined tube 14 via the first inclined tube 7, and the second regenerator 6 is connected to the inclined tube 14 via the second inclined tube 8. The first inclined tube 7 and the second inclined tube 8 are equipped with flow control valves. The flow control valve of the first inclined tube 7 is used to control the amount of heavy particulate catalyst entering the inclined tube 14, and the flow control valve of the second inclined tube 8 is used to control the amount of light particulate catalyst entering the inclined tube 14, thereby controlling the ratio of heavy particulate catalyst and light particulate catalyst entering the first reactor 1. The inclined tube 14 is equipped with a control valve.

[0049] The settling tank 3 and the first regenerator 5 are connected by a waiting-to-regenerate inclined tube 4, and a waiting-to-regenerate valve is provided on the waiting-to-regenerate inclined tube 4. The deactivated heavy particulate catalyst and light particulate catalyst in the settling tank 3 enter the first regenerator 5 through the waiting-to-regenerate inclined tube 4.

[0050] The bottom of the first regenerator 5 is provided with a feed port for replenishing heavy particulate catalyst, and the bottom of the second regenerator 6 is provided with a feed port for replenishing light particulate catalyst. During the reaction, the heavy particulate catalyst and light particulate catalyst that need to be replenished due to loss are replenished through the feed ports of the first regenerator 5 and the second regenerator 6, respectively.

[0051] The bottom of the second regenerator 6 is recessed towards its center to form a cone-shaped area. The bottom of the cone-shaped area is connected to the upper port of the first regenerator 5, meaning that the speed of the main air in the second regenerator 6 is less than the speed of the main air in the first regenerator 5.

[0052] Example 5

[0053] A dual-flow catalyst coupling method is provided, based on a dual-flow catalyst reaction system described in Example 4 above. In this example, the density of the heavy and light particulate catalysts is similar, the particle size of the heavy particulate catalyst is larger than that of the light particulate catalyst, the first chemical reaction is an endothermic reaction, and the temperature of the light particulate catalyst is higher than the temperature in the first reactor 1. The method includes the following steps:

[0054] S1, the heavy particulate catalyst and the light particulate catalyst enter the first reactor 1 through the regeneration unit. After catalyzing the first chemical reaction, the heavy particulate catalyst is deactivated, converting the first reaction feedstock into the first reaction product. The light particulate catalyst provides heat for the first chemical reaction, ensuring a stable temperature within the first reactor 1. The temperature of the light particulate catalyst decreases to the temperature required for the second chemical reaction. The cooled light particulate catalyst, the deactivated heavy particulate catalyst, and the first chemical product enter the second reactor 2 under the action of the lifting gas. The second chemical feedstock enters the second reactor 2 through the feedstock inlet 11. After participating in the second chemical reaction, the light particulate catalyst is deactivated, converting the second reaction feedstock into the second reaction product. In this embodiment, part of the heavy particulate catalyst flows out of the first reactor 1 through the inner conveying pipe 13, and part of the heavy particulate catalyst flows out through the gap between the inner conveying pipe 13 and the sidewall of the carry-out control zone 101.

[0055] In S1, the acute angle formed between the flow direction of the heavy and light particulate catalysts entering the mixing buffer 103 and the axis of the first reactor 1 is 20-70°, and the inflow velocity is 0.5-3 m / s. The flow velocity of the lift gas entering the first reactor 1 through the air inlet 9 is 0.1-1 m / s. In this embodiment, the acute angle formed between the flow direction of the heavy and light particulate catalysts entering the mixing buffer 103 and the axis of the first reactor 1 is 20°, and the inflow velocity is 0.5 m / s. The flow velocity of the lift gas entering the first reactor 1 through the air inlet 9 is 0.1 m / s. This avoids the formation of a deposition zone at the bottom of the first reactor 1 by the heavy particulate catalyst, and also prevents the light particulate catalyst that has just entered the mixing buffer 103 and has not yet had time to transfer heat from being carried away. This would result in low heat transfer efficiency, and because the light particulate catalyst has not transferred heat, it has not reached the temperature required for the second chemical reaction, thus affecting the conversion of the second chemical raw material.

[0056] In S1, the supplementary air pipe 1011 introduces lifting gas into the carry-out control zone 101 to ensure that the carried-out heavy particulate catalyst enters the settling tank 3. The lifting gas velocity in the supplementary air pipe 1011 is 1-10 m / s, and the direction is vertically upward. The main air velocity introduced into the bottom of the first regenerator 5 is 0.5-2 m / s, and the direction is vertically upward. In this embodiment, the lifting gas velocity in the supplementary air pipe 1011 is 1 m / s, and the direction is vertically upward; the main air velocity introduced into the bottom of the first regenerator 5 is 0.5 m / s, and the direction is vertically upward, further ensuring that the heavy particulate catalyst can flow out of the first reactor 1 and finally enter the first regenerator 5 for regeneration, so that it can be circulated in this invention.

[0057] S2, the deactivated heavy particulate catalyst, the deactivated light particulate catalyst, the first chemical product, and the second chemical product enter the settling tank 3 under the action of the lifting gas. After passing through the settling tank 3, the deactivated heavy particulate catalyst and the light particulate catalyst are transported to the regeneration unit for regeneration. The heavy particulate catalyst is regenerated in the first regenerator 5, and part of the light particulate catalyst is regenerated in the first regenerator 5, while the other part is regenerated in the second regenerator 6.

[0058] S3, the regenerated heavy particulate catalyst and light particulate catalyst enter the first reactor 1.

[0059] In S2, the flow velocity of the main air entering the bottom of the first regenerator 5 is 0.5-2 m / s. In this embodiment, the flow velocity of the main air entering the bottom of the first regenerator 5 is 0.5 m / s, and the direction is vertically upward. This ensures that the light particulate catalyst flows into the second regenerator 6, while the heavy particulate catalyst remains in the second regenerator 6, and that the light particulate catalyst and the heavy particulate catalyst enter the first reactor 1 through the main air.

[0060] Example 6

[0061] A dual-flow catalyst coupling method is provided, based on a dual-flow catalyst reaction system described in Example 4 above. In this example, the density of the heavy and light particulate catalysts is similar, the particle size of the heavy particulate catalyst is larger than that of the light particulate catalyst, the first chemical reaction is exothermic, and the temperature of the light particulate catalyst is lower than that in the first reactor 1. The method includes the following steps:

[0062] S1, the heavy particulate catalyst and the light particulate catalyst enter the first reactor 1 through the regeneration unit. After catalyzing the first chemical reaction, the heavy particulate catalyst is deactivated, converting the first reaction feedstock into the first reaction product. The light particulate catalyst acts as a cold source for the first chemical reaction, meaning that the heat generated by the first chemical reaction is carried away by the light particulate catalyst, ensuring a stable temperature inside the first reactor 1. The temperature of the light particulate catalyst rises to the temperature required for the second chemical reaction. The heated light particulate catalyst, the deactivated heavy particulate catalyst, and the first chemical product enter the second reactor 2 under the action of the lifting gas. The second chemical feedstock enters the second reactor 2 through the feedstock inlet 11. After participating in the second chemical reaction, the light particulate catalyst is deactivated, converting the second reaction feedstock into the second reaction product. In this embodiment, part of the heavy particulate catalyst flows out of the first reactor 1 through the inner conveying pipe 13, and part of the heavy particulate catalyst flows out through the gap between the inner conveying pipe 13 and the sidewall of the carry-out control zone 101.

[0063] In S1, the flow direction of the heavy and light particulate catalysts entering the mixing buffer 103 forms an acute angle of 70° with the axis of the first reactor 1, and the inlet velocity is 3 m / s. The flow velocity of the boost gas entering the first reactor 1 through the inlet 9 is 1 m / s. This avoids the formation of a deposition zone at the bottom of the first reactor 1 by the heavy particulate catalyst, and also prevents the light particulate catalyst that has just entered the mixing buffer 103 and has not yet had time to transfer heat from being carried away. The heat transfer efficiency is low, and because the light particulate catalyst has not transferred heat, it has not reached the temperature required for the second chemical reaction, which affects the conversion of the second chemical raw material.

[0064] In S1, the supplementary air pipe 1011 introduces lifting air into the carry-out control zone 101 to ensure that the carried-out heavy particulate catalyst enters the settling tank 3. The lifting air velocity in the supplementary air pipe 1011 is 10 m / s and the direction is vertically upward. The main air velocity introduced into the bottom of the first regenerator 5 is 2 m / s and the direction is vertically upward, further ensuring that the heavy particulate catalyst can flow out of the first reactor 1 and finally enter the first regenerator 5 for regeneration, so that it can be circulated in this invention.

[0065] S2, the deactivated heavy particulate catalyst, the deactivated light particulate catalyst, the first chemical product, and the second chemical product enter the settling tank 3 under the action of the lifting gas. After passing through the settling tank 3, the deactivated heavy particulate catalyst and the light particulate catalyst are transported to the regeneration unit for regeneration. The heavy particulate catalyst is regenerated in the first regenerator 5, and part of the light particulate catalyst is regenerated in the first regenerator 5, while the other part is regenerated in the second regenerator 6.

[0066] S3, the regenerated heavy particulate catalyst and light particulate catalyst enter the first reactor 1.

[0067] In S2, the main airflow velocity at the bottom of the first regenerator 5 is 2 m / s, and the direction is vertically upward. This ensures that the light particulate catalyst flows into the second regenerator 6, while the heavy particulate catalyst remains in the second regenerator 6, and that the main airflow causes both the light and heavy particulate catalysts to enter the first reactor 1.

[0068] Application examples

[0069] The dual-particle catalyst coupling method provided in Example 6 was applied in practice. The first chemical reaction was a dehydrogenation reaction of low-carbon alkane, with propane as the first reactant and Cr2O3 / Al2O3 as the heavy particulate catalyst, the properties of which are shown in Table 2. The second chemical reaction was a catalytic cracking reaction, with hydrotreated wax oil as the second reactant, the properties of which are shown in Table 1, and a light particulate catalyst as a catalytic cracking balancer, the properties of which are shown in Table 3. The mixed flow of heavy and light particulate catalysts entered the first reactor at a velocity of 1 m / s, the booster gas flow entering the first reactor through the inlet was 0.1 m / s, the booster gas flow entering the carry-out control zone through the make-up gas pipe was 5 m / s, and the main air flow entering the first regenerator was 1 m / s. The main operating conditions and product distribution of this application example are shown in Table 4.

[0070] Table 1 shows the properties of the feedstock oil for the second reaction.

[0071] project Second reaction feedstock properties <![CDATA[Density (20 °C), kg / m 3 > 922.1 Distillation range, °C IBP 237.4 10％ 385.5 30％ 423.7 50％ 464.0 70％ 501.7 90％ 544.8 FBP 598.8 Race composition, w% Saturated hydrocarbons 85.89 Aromatics 10.82 Gum and asphalt 3.21

[0072] Table 2 shows the properties of heavy particulate catalysts.

[0073]

[0074]

[0075] Table 3 shows the properties of light particulate catalysts.

[0076] Catalyst type Catalytic cracking balancer Microreactive 64 Apparent loose density, g / ml 0.86 Carbon determination, % 0.01 <![CDATA[Surface area, m 2 / g]]> 112.4 Pore ​​volume, ml / g 0.30 Main chemical composition, w% <![CDATA[SiO2]]> 46.56 <![CDATA[Al2O3]]> 44.10 <![CDATA[Re2O3]]> 3.68 <![CDATA[P2O5]]> 0.78 Sieving composition, % <20μm 0.11 20-40μm 11.52 40-80μm 47.22 80-110μm 18.26 >110μm 22.89 Metal content, mg / kg Ni 4364 V 4112 Fe 4728 Na 1862

[0077] Comparative Example

[0078] This comparative example uses a reactor based on existing technology. The first chemical reaction is a dehydrogenation reaction of low-carbon alkanes, with propane as the feedstock and Cr2O3 / Al2O3 as the heavy particulate catalyst, the properties of which are shown in Table 2. The second chemical reaction is a catalytic cracking reaction, with hydrotreated wax oil as the feedstock, the properties of which are shown in Table 1. The light particulate catalyst is a catalytic cracking equilibrium agent, the properties of which are shown in Table 3. The mixed flow of heavy and light particulate catalysts enters the first reactor at a velocity of 1 m / s, and the booster gas flow entering the first reactor through the inlet is at a velocity of 0.1 m / s. The main operating conditions and product distribution of this comparative example are shown in Table 4.

[0079] Table 4 shows the product distribution for application examples and comparative examples.

[0080] Application examples Comparative Example Dual-particle fluidized bed reactor feedstock propane propane Mixed flow temperature, °C 690 690 The actual temperature of the first reactor was ℃. 650 630 Dehydrogenation catalyst <![CDATA[Cr2O3 / Al2O3]]> <![CDATA[Cr2O3 / Al2O3]]> carrier type Microspheres Microspheres The actual temperature of the second reactor was ℃. 510 530 Product distribution, w% dry air 2.10 2.16 Liquefied gas 22.70 22.78 propylene 9.42 7.96 Butene 4.58 4.26 gasoline 40.60 40.54 diesel fuel 24.58 24.79 Oil slurry 3.68 3.51 coke 6.34 6.22

[0081] The results of comparing the comparative example and the application example are shown in Table 4. The temperature of the fluidized bed in the application example is higher than that in the comparative example. The light and heavy particulate catalysts are uniformly mixed in the first reactor, and no deposition zone of heavy particulate catalyst is formed at the bottom of the first reactor, allowing the light particulate catalyst to transfer heat fully. The heat transfer efficiency between the two is high, resulting in a higher actual temperature in the first reactor than in the comparative example, which improves the efficiency of the first chemical reaction. At the same time, after the light particulate catalyst in the application example has transferred heat fully, its temperature is lower when it enters the second reactor, which makes the reaction temperature of the second chemical reaction lower than that of the second chemical reaction in the comparative example. This reaction temperature is more conducive to improving the efficiency of the second chemical reaction.

[0082] The above description of the disclosed embodiments enables those skilled in the art to make or use the invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. Therefore, the invention is not to be limited to the embodiments shown herein, but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A dual-particle flow catalyst reaction unit, comprising a first reactor (1) having an inlet at the bottom and an outlet at the top, the inlet including an air inlet (9) for supplying booster gas into the first reactor (1) and a feed inlet (10) for supplying first reactant material into the first reactor (1), and an inclined pipe (14) for introducing heavy particle catalyst and light particle catalyst is provided on one side of the first reactor (1), characterized in that: The first reactor (1) includes a mixing buffer zone (103) located at its lower part with a longitudinal section of a cone-shaped structure with a larger upper section and a lower section of a cone-shaped structure with a smaller upper section and a lower section of a carry-out control zone (101) located at its upper part with a longitudinal section of a cone-shaped structure with a smaller upper section and a larger lower section. An inclined pipe (14) is connected to the mixing buffer zone (103) and its bottom end is inclined downward to mix and send the heavy particulate catalyst and the light particulate catalyst to the bottom of the mixing buffer zone (103). Under the action of the lifting gas, the heavy particulate catalyst and the light particulate catalyst form a uniform dense phase bed zone (102) between the mixing buffer zone (103) and the carry-out control zone (101). An inner conveying pipe (13) with open ends and extending along the height direction of the first reactor (1) is provided in the carry-out control zone (101). A supplementary gas pipe (1011) for introducing lifting gas into the carry-out control zone (101) is provided on one side of the carry-out control zone (101) near its bottom. The bottom end of the inclined pipe (14) faces the air inlet (9).

2. The dual-particle flow catalyst reaction unit as described in claim 1, characterized in that: The top of the inner delivery pipe (13) moves toward the center to form an inner contraction (1302), and the bottom of the inner delivery pipe (13) extends outward to form an outer expansion (1301), with the bottom end of the outer expansion (1301) close to the interface of the uniform dense phase bed region (102).

3. The dual-particle flow catalyst reaction unit as described in claim 1, characterized in that: The inner delivery pipe (13), outlet and air inlet (9) are coaxially arranged.

4. The dual-particle flow catalyst reaction unit as described in claim 1, characterized in that: The bottom of the hybrid buffer (103) has a spherical structure.

5. The dual-particle flow catalyst reaction unit as described in claim 1, characterized in that: The angle formed between the inclined tube (14) and the first reactor (1) is an acute angle, which is 30-60°.

6. A dual-particle-flow catalyst reaction device, comprising a reaction unit, wherein a second reactor (2) is connected above the reaction unit and open at its top, and the bottom of the second reactor (2) is provided with a raw material inlet (11) for introducing a second chemical reaction raw material into the reactor, characterized in that: The reaction unit is the reaction unit according to any one of claims 1-5, and the second reactor (2) is connected to the outlet of the first reactor (1).

7. A dual-particle-flow catalyst reaction system, comprising a reaction device connected in series to form a closed loop, a settling tank (3) located above the reaction device, and a regenerator unit located on one side of the reaction device, characterized in that: The reaction device is the reaction device according to claim 6. The settling tank (3) is connected to the outlet of the second reactor (2). The regenerator unit includes a first regenerator (5) and a second regenerator (6) that are connected to each other. The second regenerator (6) is located above the first regenerator (5). The first regenerator (5) is connected to the settling tank (3). At the same time, the first regenerator (5) and the second regenerator (6) are both connected to the inclined pipe (14). The bottom of the first regenerator (5) is provided with an air inlet (12) for introducing the main air, so that the light particulate catalyst enters the second regenerator (6) and the heavy particulate catalyst remains in the first regenerator (5).

8. The dual-particle flow catalyst reaction system as described in claim 7, characterized in that: The first regenerator (5) is connected to the inclined tube (14) through the first inclined tube (7), and the second regenerator (6) is connected to the inclined tube (14) through the second inclined tube (8). A control valve is provided on the first inclined tube (7) and the second inclined tube (8).

9. The dual-particle flow catalyst reaction system as described in claim 7, characterized in that: The settling device (3) and the first regenerator (5) are connected by a waiting-to-regenerate inclined tube (4), and a waiting-to-regenerate valve is provided on the waiting-to-regenerate inclined tube (4). The deactivated heavy particle catalyst and light particle catalyst in the settling device (3) enter the first regenerator (5) through the waiting-to-regenerate inclined tube (4).

10. The dual-particle flow catalyst reaction system as described in claim 7, characterized in that: The bottom of the first regenerator (5) is provided with a feed port for replenishing heavy particulate catalyst, and the bottom of the second regenerator (6) is provided with a feed port for replenishing light particulate catalyst.

11. The dual-particle flow catalyst reaction system as described in claim 7, characterized in that: The bottom end of the second regenerator (6) is recessed towards its center to form a conical area, and the bottom end of the conical area is connected to the upper port of the first regenerator (5).

12. A dual-flow catalyst coupling method, the method being based on a dual-flow catalyst reaction system according to any one of claims 7-11, comprising the following steps: S1, the heavy particulate catalyst and the light particulate catalyst enter the first reactor (1) through the regeneration unit. The heavy particulate catalyst is used to catalyze the first chemical reaction, so that the first reaction raw material is converted into the first reaction product. The light particulate catalyst is used to heat or remove heat from the first chemical reaction and then enters the second reactor (2), so that the second reaction raw material is converted into the second reaction product. S2, the deactivated heavy particulate catalyst and light particulate catalyst are transported to the regeneration unit for regeneration after passing through the settler (3); S3, the regenerated heavy particulate catalyst and light particulate catalyst enter the first reactor (1). The features are as follows: In S1, the inflow velocity of the heavy particulate catalyst and the light particulate catalyst when entering the mixing buffer (103) is 0.5-3m / s, and the flow velocity of the lifting gas entering the first reactor (1) through the air inlet (9) is 0.1-1m / s; In S2, the lifting gas is introduced into the inner conveying pipe (13) through the gas supply pipe (1011) to ensure that the heavy particulate catalyst is carried out into the settling tank (3), and the flow velocity of the lifting gas in the gas supply pipe (1011) is 1-10m / s, and the direction is vertically upward; The flow velocity of the main air introduced into the bottom of the first regenerator (5) is 0.5-2m / s, and the direction is vertically upward.

13. The dual-particle flow catalyst coupling method as described in claim 12, characterized in that: The particle size of the heavy particulate catalyst is larger than that of the light particulate catalyst, and the weight of the heavy particulate catalyst is greater than that of the light particulate catalyst.

14. The dual-particle catalyst coupling method as described in claim 12, characterized in that: The heavy particulate catalyst is regenerated in the first regenerator (5), and a portion of the light particulate catalyst is regenerated in the first regenerator (5) and the other portion is regenerated in the second regenerator (6).

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