A continuous catalytic cracking regeneration operation simulation evaluation system and method

Abstract

The present disclosure relates to a continuous catalytic cracking regeneration operation simulation evaluation system and method, the system includes a spent catalyst storage and feeding unit and a regenerator (2-1); wherein the regenerator includes a shell, a spent catalyst inlet, a heat exchange medium internal component (2-5), a charred gas inlet and a regenerated agent outlet; wherein the heat exchange medium internal component is formed as a variable diameter spiral coil and is arranged inside the shell around the axial direction of the regenerator; the heat exchange medium internal component includes a heat exchange medium inlet and a heat exchange medium outlet; the heat exchange medium inlet and the heat exchange medium outlet are respectively extended to the outside of the regenerator shell through pipelines, so that the heat exchange medium in the heat exchange medium internal component pipe exchanges heat with the material inside the regenerator shell only through the tube wall. Continuous steady-state operation can be achieved, and the device is smaller in scale and suitable for construction in small and medium-sized laboratories, and can more accurately and conveniently simulate and evaluate the catalytic cracking regeneration charring effect under different conditions.

Description

Technical Field

[0001] The present disclosure relates to the field of petrochemical technology, and in particular to a continuous catalytic cracking regeneration operation simulation evaluation system and method. Background Art

[0002] Petroleum, the lifeblood of industry, is used as fuel for over 80% of its products, providing energy and power for industry, agriculture, and transportation. The remainder serves as crucial chemical raw materials, driving the development of industries such as food, agriculture, pharmaceuticals, and household chemicals. Catalytic cracking plays a pivotal role in petroleum refining. Over 90% of refineries worldwide have catalytic cracking units, and 80% of gasoline and 30% of diesel in my country come from catalytic cracking units. The catalytic cracking process primarily consists of a reaction phase and a regeneration phase. The reaction phase primarily produces the various products, while the regeneration phase burns off the deactivated catalyst to regenerate it and provides the heat required to maintain the reaction temperature. As a crucial component of the catalytic cracking process, the performance of the regeneration phase impacts the overall unit's output. Despite significant recent advancements in catalytic cracking technology, the conventional single-stage regeneration process, with its relatively simple process and minimal equipment, remains widely used by refineries.

[0003] At present, most of the research and evaluation devices for catalytic cracking regeneration processes in laboratories are small-scale intermittent fluidized bed devices, and another small part of the research uses catalytic cracking pilot plants.

[0004] A problem with small-scale devices is that they operate intermittently. For example, CN104845661A discloses an intermittent evaluation device. Before each test, a small amount of reagent is weighed and placed in the reactor, but the reactor is not continuously replenished or discharged. This results in the reactants and products in the reactor changing over time. For example, the carbon content in the reactor decreases, while the carbon dioxide concentration in the flue gas first increases, then decreases, and finally disappears. This clearly makes it impossible to simulate and evaluate the continuous stable state in actual industrial production and conduct in-depth mechanism research.

[0005] The pilot plant also has problems in the laboratory regeneration operation simulation evaluation. CN104140843A discloses a fluidized bed catalytic cracking test device, which includes a reactor and a regenerator, forming a continuous cycle process. In the experiment, the raw oil is atomized and mixed with the regeneration agent, reacting to generate reaction oil gas, which is then received and analyzed by external detection instruments, thereby achieving evaluation of the raw oil, catalyst, and reaction conditions. However, the device in this technical solution is large in size, uses a lot of materials, and has a long operation time (requiring several days), which is not suitable for routine scientific research and evaluation in the laboratory; secondly, the pilot plant design is mainly based on the simulation reaction section, and the design purpose of the regeneration section is to burn off the coke on the spent agent transported by the reaction section, so its regeneration space velocity is generally large, and the gas and solid residence time is also different from that of the industrial regeneration device; and because the pilot plant is a reverse regeneration system, there are problems with material balance, pressure balance, and heat balance. If the regeneration process is studied and evaluated on the pilot plant and a single operating parameter is changed, the entire reverse regeneration system will be affected, and it is very complicated to adjust to the new operating point, and other operating parameters may also change.

[0006] If the regenerator structure of an industrial regenerator or a pilot plant is taken out and reduced in size, in order to ensure the catalyst storage and the average residence time of the solids, the resulting regenerator must either have a wide bed diameter and a shallow bed layer, resulting in a short gas residence time; or reduce the bed diameter and increase the bed height, which will lead to poor fluidization conditions such as slugging in the bed layer; if a wide bed diameter and a high bed layer are used at the same time, a single evaluation will require dozens of kilograms of catalyst to be regenerated and a high flow rate of reaction gas, and will also face the problem of large-scale flue gas treatment. Whether it is refinery procurement or actual operation, it is not suitable for small-scale evaluation in the laboratory.

[0007] Furthermore, after the regenerator is reduced in size, some components of the original industrial installation, such as heat exchangers and slide valves, become difficult to manufacture and install in a smaller size, and may even fail to achieve their original performance. Even if some structures, such as cyclone separators, can be manufactured to meet the specific operating conditions of a small regenerator, the operating conditions of laboratory-level simulation evaluation equipment are very wide. A cyclone separator that is feasible under certain gas flow conditions will have a significant impact on separation efficiency when the gas flow rate is increased or decreased.

[0008] At the same time, the regeneration process itself is primarily a chemical reaction involving carbon combustion and heat release. When the experimental volume reaches a certain level, the heat release increases, and relying solely on the reactor's natural heat dissipation will make it difficult to maintain thermal equilibrium, potentially leading to dangerous temperature fluctuations. Therefore, heat extraction components are required. However, in industrial plants, internal heat extraction equipment is bulky when installed vertically, and excessive cross-sectional area is occupied when installed horizontally. External heat extraction equipment is complex and difficult to implement in small-scale plants. Furthermore, the removal and return of the catalyst can significantly affect the fluidization state of the small bed, leading to problems such as uneven heat distribution and flow field interference.

[0009] When used alone, the regenerator structure requires specialized equipment to simulate the regeneration process of an actual industrial unit. A key challenge is achieving continuous and stable feeding of spent reactant particles. Current methods for feeding particles primarily include pneumatic and mechanical feeding. Pneumatic feeding requires large amounts of gas to transport the material, which can affect the reactant concentration and flow pattern within the regenerator. Furthermore, pneumatic feeding is typically used in applications with high mass flow rates, resulting in low feeding accuracy and significant control difficulties.

[0010] The spent catalyst in the catalytic cracking process enters the regenerator in the form of hot particles. However, small devices do not have enough vertical space to heat the spent catalyst. If the particles are heated in the hopper above the feeder, there are problems involving the heating method, insulation and heating effect such as the thermal uniformity of the particles, and whether the subsequent mechanical and sealing structures can withstand high temperatures. Summary of the Invention

[0011] The purpose of the present disclosure is to provide a continuous catalytic cracking regeneration operation simulation evaluation system and method, which can achieve continuous steady-state operation, and the device is smaller in scale and suitable for construction in small and medium-sized laboratories, and can simulate and evaluate the catalytic cracking regeneration coking effect more accurately and conveniently.

[0012] To achieve the above-mentioned objectives, the present disclosure provides, in a first aspect, a continuous catalytic cracking regeneration operation simulation and evaluation system, comprising a spent catalyst storage and feeding unit and a regenerator; wherein the regenerator comprises a shell, a spent catalyst inlet, a heat exchange medium internal component, a charred gas inlet, and a regenerated catalyst outlet; wherein the heat exchange medium internal component is formed as a variable diameter spiral coil and is arranged inside the shell by being coiled around the axial direction of the regenerator; the heat exchange medium internal component comprises a heat exchange medium inlet and a heat exchange medium outlet; the heat exchange medium inlet and the heat exchange medium outlet respectively extend to the outside of the regenerator shell through pipelines, so that the heat exchange medium in the heat exchange medium internal component tube exchanges heat with the material inside the regenerator shell only through the tube wall.

[0013] Optionally, the variable diameter spiral coil is formed by winding a through hollow tube in a conical spiral line; and along the axial direction of the regenerator shell, the winding diameter of the variable diameter spiral coil gradually increases from top to bottom to form a cone in an upright shape, or the winding diameter gradually decreases from top to bottom to form an inverted cone, or a plurality of the variable diameter spiral coils are installed in combination, and the combined installation method includes: the conical top end of a variable diameter spiral coil is connected to the conical top end of another variable diameter spiral coil, or the conical bottom end of a variable diameter spiral coil is connected to the conical top end of another variable diameter spiral coil. Connect to the conical bottom end of another reducing spiral coil; optionally, the inner diameter of the reducing spiral coil is 3 to 8 mm, and the centerline thread pitch of each layer of coil is 3 to 15 mm; the wall thickness of the reducing threaded coil is 0.75 to 2 mm; the maximum coiling diameter of the reducing threaded coil is 80 to 95% of the inner diameter of the regenerator shell, wherein the maximum coiling diameter refers to the maximum diameter of the conical shape of the reducing threaded coil; optionally, the hollow tube is a seamless steel tube; optionally, the shape of the hollow tube is a round tube or a square tube.

[0014] Optionally, the shell of the regenerator is a constant diameter cylinder or a variable diameter cylinder; the cross-section of the shell of the regenerator is circular; preferably, the shell of the regenerator is a variable diameter cylinder, and the variable diameter cylinder is composed of an upper cylindrical shell and a lower conical shell coaxially sealed and connected; the heat exchange medium internal component is arranged in the upper cylindrical shell of the regenerator and is coaxially arranged with the upper cylindrical shell; the regeneration agent outlet is arranged at the bottom of the lower conical shell, and the regeneration agent outlet is connected to the regeneration agent recovery unit; optionally, the inner diameter of the upper cylindrical shell is 30 to 100 mm; the height-to-diameter ratio is 1 to 50:1, preferably 4 to 30:1; the bottom cone angle of the lower conical shell is 60 to 150°, preferably 90 to 120°.

[0015] Optionally, the raw material storage and feeding unit includes a raw material silo, a feeding screw, an external pressure protective gas structure and a raw material standpipe; the feeding includes an idle section, a feeding section and a transmission section; the external pressure protective gas structure includes an external pressure protective gas shell, a pressing end cover and a particle feeder shell, the external pressure protective gas shell is sleeved on the outside of the idle section of the feeding screw, the pressing end cover is arranged at the end of the idle section, and the pressing end cover and the first end face of the external pressure protective gas shell are sealed by a protective gas shaft seal; there is a gap between the inner wall of the external pressure protective gas shell and the outer wall of the feeding screw to form an annular cavity around the feeding screw, and the external pressure protective gas shell is provided with a through hole inside and outside. an air inlet pipe and an air outlet pipe, so that the annular cavity is connected with the air source through the air inlet pipe, and is connected with the outside of the external pressure protective gas shell through the air outlet pipe; optionally, the transverse length of the annular cavity is 0.5 to 8 mm; optionally, a pressure sensor and a first control valve are provided on the protective gas inlet pipe; a back pressure valve is provided on the protective gas outlet pipe; the particle feeder shell is sleeved on the outside of the feeding section of the feeding screw, and the first end face of the particle feeder shell is sealed with the second end face of the external pressure protective gas shell by a feeding shaft seal; the inlet end of the riser to be generated is connected with the conveying section of the feeding screw, and the outlet end extends to the inside of the shell of the regenerator.

[0016] Optionally, the idle section length of the feeding screw is 50 to 300 mm; the total length of the conveying section is 200 to 1000 mm. Preferably, a solid preheater is provided on the outside of the conveying section of the feeding screw; preferably, the feeding screw has an inclination angle from the idle section to the conveying section, preferably any inclination angle between -30 and 30°; the outlet end of the standpipe to be generated is located above the heat exchange medium internal component and is spaced from the top of the heat exchange medium internal component, and the inlet end of the standpipe to be generated is located below the static bed layer of the regenerator's regenerator; optionally, the system further includes a heating furnace, which is arranged outside the regenerator; optionally, the number of the heating furnaces is one or more.

[0017] Optionally, the system also includes a charred gas supply unit, which includes a pressure-stabilizing valve, a gas flowmeter, a gas preheater and a gas distributor; the gas preheater is provided with a gas preheating inlet and a gas preheating outlet, and the gas preheating inlet is connected to the charred gas source. The gas source introduction pipeline of the gas preheating inlet is provided with the pressure-stabilizing valve and the gas flowmeter in sequence along the gas flow direction; the gas distributor is provided with a charred gas inlet and distribution air holes, and the charred gas inlet is connected to the preheating gas outlet of the gas preheater; the gas distributor extends from the lower part of the shell of the regenerator into the regenerator, and the outlets of the distribution air holes of the gas distributor face the bottom of the shell; preferably, the gas distributor extends from the bottom of the upper cylindrical shell of the regenerator into the regenerator, and the outlets of the distribution air holes of the gas distributor face the bottom of the lower conical shell of the regenerator.

[0018] Optionally, the system also includes an analysis unit; the analysis unit includes a flue gas sampling device and an exhaust gas flue gas analyzer; the regenerator also includes a flue gas filtering device, and the flue gas filtering device is arranged at the upper part of the regenerator shell; the flue gas inlet of the exhaust gas flue gas analyzer is connected to the flue gas outlet of the flue gas filtering device; a flue gas collection port is provided on the side wall of the regenerator shell, and the flue gas collection port is connected to the flue gas sampling device. Preferably, a plurality of flue gas collection ports are provided at different heights on the side wall of the shell along the axial direction of the regenerator.

[0019] Optionally, the system also includes a regeneration agent recovery unit, which includes a discharge valve, a discharge bin, a discharge bin air inlet valve, a discharge bin back pressure valve, a pressure sensor and a discharge valve; the discharge bin is provided with a regeneration agent inlet, a discharge outlet, a discharge bin air inlet and a discharge bin gas outlet; the regeneration agent inlet is connected with the regeneration agent outlet of the regenerator; the discharge bin air inlet is provided at the upper part of the discharge bin, and the discharge bin air inlet valve is provided on the connecting pipeline between the discharge bin air inlet and the gas source; the discharge bin gas outlet is provided at the top of the discharge bin and is connected to the external environment through the air outlet pipeline, the discharge bin back pressure valve is provided on the gas pipeline, and the pressure sensor is provided between the discharge bin gas outlet and the discharge bin back pressure valve.

[0020] A second aspect of the present disclosure provides a method for simulating and evaluating a continuous catalytic cracking regeneration operation, using the system described in the first aspect of the present disclosure. The method comprises the following steps:

[0021] The regenerated agent is allowed to enter the regenerator through the feeding outlet of the regenerated agent feeding unit; the charred gas is introduced into the regenerator through the charred gas supply unit, and the regenerated agent is subjected to charred regeneration treatment in the regenerator to obtain regenerated flue gas and regenerated agent; the heat exchange medium is introduced into the tube space of the variable diameter spiral coil inner component through the heat exchange medium inlet of the variable diameter coil heat exchange medium inner component, so that the heat exchange medium exchanges heat with the material in the regenerator; the regenerated flue gas enters the analysis unit for analysis; and the regenerated agent enters the regenerated agent recovery unit for regenerated agent recovery treatment.

[0022] Optionally, the reaction conditions in the regenerator include: temperature of 500-800°C, pressure of 0-0.5 MPa; temperature of the charred gas of 20-500°C, preferably 150-300°C; volume space velocity of the charred gas of 6-50000h -1 , preferably 200 to 3000 hours -1 , the superficial velocity of the charred gas is 0.01 to 1.2 m / s, preferably 0.1 to 0.6 m / s; the residence time of the spent agent is 1 to 240 min, preferably 2 to 60 min; optionally, the volume content of oxygen in the charred gas composition is 10 to 40 volume %; optionally, the spent agent comes from a catalytic cracking process in a factory or a spent agent obtained by carbonizing in a pilot plant reaction, preferably, the carbon content of the spent agent is 0.5 to 3 wt%; preferably, the carbon content of the regenerated agent is 0.01 to 1 wt%.

[0023] Optionally, the method further includes preheating the spent catalyst entering the spent catalyst feeding unit; and then allowing the preheated spent catalyst to enter the regenerator; preferably, the temperature of the preheated spent catalyst is 10 to 550° C.; optionally, the feeding speed of the feeding screw in the spent catalyst feeding unit to the regenerator is 0.1 to 20 g / s, and the working pressure of the feeding screw in the spent catalyst feeding unit is 0 to 0.5 MPa.

[0024] Through the above technical solution, the present disclosure provides a continuous catalytic cracking regeneration operation simulation evaluation system and method, the system is provided with a heat exchange medium internal component in the shape of a variable diameter spiral coil in the regenerator, on the one hand, the spiral heat exchange medium internal component has a large heat exchange area, and by introducing the heat exchange medium into the tube, the excess heat of the regeneration and burning process can be removed, the temperature inside the regenerator can be adjusted, and the temperature field can be maintained stable; on the other hand, the variable diameter spiral coil can also regulate the flow field inside the regenerator, break up bubbles, prevent bubbles from agglomerating into larger bubbles, avoid the throttling problem caused by the increase in the bed height in the regenerator, and maintain the flow field stability; and the variable diameter coiling is performed along the axis of the regenerator, which increases the vertical height of the internal component, and the coil presents a multi-layer structure, which can also increase the effective flow area. The system provided by the present disclosure can achieve continuous steady-state operation and is suitable for construction in small and medium-sized laboratories, simulating a complete catalytic cracking regeneration process that is closer to an actual industrial device, and is easy to operate, so that the catalytic cracking regeneration and burning effect under different regeneration conditions can be evaluated more accurately and conveniently.

[0025] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] 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:

[0027] Figure 1 It is a structural schematic diagram of a specific embodiment of the continuous catalytic cracking regeneration operation simulation evaluation system disclosed in the present invention.

[0028] Figure 2 It is a structural diagram of a specific implementation of the external pressure protective gas structure in the evaluation system disclosed in the present invention.

[0029] Figure 3 It is a structural diagram of a specific implementation of the heat exchange medium internal components in the evaluation system disclosed in the present invention.

[0030] Figure 4 It is a structural diagram of a specific implementation of the heat exchange medium internal components in the evaluation system disclosed in the present invention.

[0031] Figure 5 It is a structural diagram of a specific implementation of the heat exchange medium internal components in the evaluation system disclosed in the present invention.

[0032] Figure 6 It is a structural diagram of a specific implementation of the flue gas sampling tube in the evaluation system disclosed in the present invention.

[0033] Figure 7This is a graph showing the changes in flue gas CO2 and CO concentrations over experimental time during the experiment of Example 1.

[0034] Figure 8 It is a structural schematic diagram of a specific embodiment of the continuous catalytic cracking regeneration operation simulation evaluation system disclosed in the present invention.

[0035] Figure 9 This is a graph showing the changes in flue gas CO2 and CO concentrations over experimental time during the experimental process of Comparative Example 1.

[0036] Description of Reference Numerals

[0037] 1-1, raw material silo; 1-2, external pressure shielding gas structure; 1-3, solid preheater; 1-4, feeding screw; 1-5, raw material standpipe; 1-2-1, particle feeder housing; 1-2-2, feeding shaft seal; 1-2-3, O-ring; 1-2-4, bolt fasteners; 1-2-5, external pressure shielding gas housing; 1-2-6, air inlet pipe; 1-2-7, pressing end cover; 1-2-8, shielding gas shaft seal; 1-2-9, air outlet pipe; 2-1, reactor; 2-2, heating furnace; 2-3, flue gas filter; 2-4, heat extractor inlet valve; 2-5, heat exchange medium internal components; 2-6, gas distributor; 2 -7, heat extractor outlet valve; 3-1, discharge valve; 3-2, discharge silo; 3-3, discharge silo air inlet valve; 3-4, discharge silo back pressure valve; 3-5, pressure sensor; 3-6, discharge valve; 4-1, pressure regulating valve; 4-2, gas flow meter; 4-3, gas preheater; 5-1, reactor back pressure valve; 5-2, gas flow meter; 5-3, three-way valve; 5-4, exhaust gas analyzer; 5-5, flue gas sampling equipment; 5-5-1, flue gas sampling tube; 5-5-2, temperature sensor; 5-5-3, filter; 5-5-4, pressure sensor; 5-5-5, flue gas sampling valve; 5-5-6, flue gas sampling bag DETAILED DESCRIPTION

[0038] 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.

[0039] like Figure 1 As shown, the first aspect of the present disclosure provides a continuous catalytic cracking regeneration operation simulation evaluation system, the system comprising a spent catalyst storage and feeding unit and a regenerator 2-1;

[0040] The regenerator 2-1 includes a shell, a spent catalyst inlet, a heat exchange medium internal component 2-5, a burnt gas inlet, and a regenerated catalyst outlet; the heat exchange medium internal component 2-5 is formed as a variable diameter spiral coil and is arranged inside the shell around the axial direction of the regenerator 2-1;

[0041] The heat exchange medium internal component 2-5 includes a heat exchange medium inlet and a heat exchange medium outlet; the heat exchange medium inlet and the heat exchange medium outlet are respectively extended to the outside of the regenerator 2-1 shell through pipelines, so that the heat exchange medium in the heat exchange medium internal component 2-5 tube only exchanges heat with the material inside the regenerator 2-1 shell through the tube wall.

[0042] The present disclosure provides a continuous catalytic cracking regeneration operation simulation evaluation system, which is provided with a heat exchange medium internal component in the shape of a variable diameter spiral coil in the regenerator. On the one hand, the spiral heat exchange medium internal component has a large heat exchange area. By introducing the heat exchange medium into the tube, the excess heat of the regeneration and burning process can be taken out and the temperature inside the regenerator can be adjusted. On the other hand, the variable diameter spiral coil can also adjust the flow field inside the regenerator, break up bubbles, prevent bubbles from agglomerating into larger bubbles, and avoid the throttling problem caused by the increase in the bed height in the regenerator. The variable diameter coil is wound upward along the axis of the regenerator, which increases the vertical height of the internal component. The coil presents a multi-layer structure and can also increase the effective flow area. The system provided by the present disclosure can achieve continuous steady-state operation and is suitable for construction in small and medium-sized laboratories. It simulates the complete regeneration process of catalytic cracking that is closer to the actual industrial device and is easy to operate, so that the catalytic cracking regeneration and burning effect under different regeneration conditions can be evaluated more accurately and conveniently.

[0043] In the present disclosure, "variable diameter spiral coil" refers to a spiral coil having different coil diameters during the spiral coiling process.

[0044] In one embodiment, the variable diameter spiral coil is formed by winding a through hollow tube in a conical spiral line; and along the axial direction of the regenerator 2-1 shell, the winding diameter of the variable diameter spiral coil gradually increases from top to bottom to form a cone in an upright shape, or the winding diameter gradually decreases from top to bottom to form an inverted cone.

[0045] In the present disclosure, “a cone in an upright shape” means that the top of the cone is at the top and the base of the cone is at the bottom; and “a cone in an inverted shape” means that the top of the cone is at the bottom and the base of the cone is at the top.

[0046] In a specific embodiment, Figure 3 and Figure 4 The schematic diagram of the structure of a variable diameter spiral coil is shown in the figure, wherein the coil can be regarded as a hollow tube that is wound from top to bottom with a gradually decreasing diameter along the central axis to obtain an "inverted cone"; in a further embodiment, as Figure 3 As shown, the openings of the two spiral coils are arranged at 180° horizontally to balance the uneven flow distribution caused by the asymmetry of the spiral line. Furthermore, the "upright cone" coiling method is opposite to the "inverted cone" coiling method, and this disclosure will not be repeated here.

[0047] In the present disclosure, during the fluidization process, the gas-solid two-phase flows through the variable diameter spiral coil, and the large bubble can be regarded as a tiny cylindrical flow in each differential section perpendicular to the coil axis. The wake formed by the cylindrical flow in each differential section is itself non-ideally axially symmetrical, and the flow directions of the wakes at different interfaces are also different. The vortices formed in the wake interfere with each other to enhance the gas disturbance and break up the bubbles. The shape of larger at the top and smaller at the bottom makes it easier for the upward two-phase fluid below to rise from the side wall, and there are more downward-moving particles in the middle. The downward-moving particles contact and mix with the flowing gas wake, further enhancing the mass transfer and heat transfer effects.

[0048] In a further embodiment, one or more heat exchange medium internal components can be provided in the regenerator 2-1, preferably an even number of components according to the internal space of the regenerator; specifically, during installation, the same winding diameters are connected into one piece, that is, multiple variable diameter spiral coils are installed in combination, and the combined installation method includes: the conical top end of a variable diameter spiral coil is connected to the conical top end of another variable diameter spiral coil, or the conical bottom end of a variable diameter spiral coil is connected to the conical bottom end of another variable diameter spiral coil. A specific embodiment, such as Figure 5 As shown, it is preferred that multiple heat exchange media (multiple variable diameter spiral coils) are connected into one piece in the axial direction of the regenerator 2-1, and the internal components of the multiple heat exchange media use the same heat exchange medium inlet and heat exchange medium outlet as a whole. Therefore, the multiple heat exchange medium internal components can also be regarded as being wound along the same central axis through the same coil.

[0049] Specifically, the arrangement of two heat exchange medium internal components is used as an example for schematic description: Figure 5 As shown, the winding diameter gradually decreases and then gradually increases from top to bottom, so the upper and lower variable diameter spiral parts share a minimum winding diameter (considered as two cones arranged "cone angle to cone angle"); or the winding diameter gradually increases and then gradually decreases from bottom to top, so the upper and lower variable diameter spiral parts share a maximum winding diameter (considered as two cones arranged "base to base"); when the above method is used to set two heat exchange medium internal components 2-5 arranged in the upper and lower parts of the regenerator 2-1, the heat exchange medium follows the "bottom in and top out" principle, and the heat exchange medium inlet flow direction of the lower heat exchange medium internal component is 180 degrees opposite to the outlet flow direction of the upper heat exchange medium internal component. Furthermore, when it is necessary to arrange multiple heat exchange medium internal components, the coil can continue to be coiled in a conical spiral manner. Taking four heat exchange medium internal components as an example, the connection between two adjacent internal components from bottom to top includes the following two methods:

[0050] Method 1: Cone angle against cone angle (1st and 2nd internal components) - base against base (2nd and 3rd internal components) - cone angle against cone angle (3rd and 4th internal components). In this method, the winding diameter of the first internal component at the bottom gradually decreases from bottom to top.

[0051] Method 2: bottom edge to bottom edge (the first and second inner components) - cone angle to cone angle (the second and third inner components) - bottom edge to bottom edge (the third and fourth inner components). In this method, the winding diameter of the first inner component at the bottom gradually increases from bottom to top.

[0052] In the present disclosure, the mass and heat transfer effects can be further improved by providing multiple heat exchange medium internal components.

[0053] In a specific embodiment, optionally, the inner diameter of the variable diameter spiral coil is 3 to 8 mm, the centerline thread pitch of each layer of the coil is 3 to 15 mm, preferably 5 to 10 mm; the wall thickness of the variable diameter spiral coil is 0.75 to 2 mm;

[0054] The maximum coiling diameter obtained by the outer diameter of the variable diameter threaded coil is 80 to 95% of the inner diameter of the regenerator 2-1 shell, preferably 85 to 92%; the maximum coiling diameter refers to the maximum diameter of the conical shape of the variable diameter threaded coil, and the maximum diameter is calculated according to the distance between the outermost pipe walls of the coil in this disclosure; the heat exchange medium internal components are set according to the ratio between the maximum coiling diameter provided in this disclosure and the inner diameter of the regenerator 2-1 shell, which can better improve the heat and mass transfer effect and maintain steady-state operation inside the regenerator.

[0055] Optionally, the hollow tube is a seamless steel tube; optionally, the shape of the hollow tube is a round tube or a square tube, or a hollow tube of other materials and other shapes known in the art can also be used.

[0056] In one embodiment, the shell of the regenerator 2-1 is a cylinder of constant diameter or a cylinder of variable diameter, and the cross section of the shell of the regenerator 2-1 is circular. Figure 1 As shown, the housing of regenerator 2-1 is a variable diameter cylinder, consisting of an upper cylindrical shell and a lower conical shell coaxially and sealed together. The heat exchange medium internal component 2-5 is disposed within the upper cylindrical shell of regenerator 2-1 and is coaxially arranged with the upper cylindrical shell. The regenerant outlet is located at the bottom of the lower conical shell and is connected to the regenerant recovery unit. The variable diameter cylinder preferably used in this disclosure allows the sidewalls of the lower conical shell to reflect the charred gas at the bottom of the cone when the gas is introduced, which helps to fluidize the solid particles within the regenerator.

[0057] In a specific embodiment, the inner diameter of the upper cylindrical shell is 30-100 mm; the height-to-diameter ratio is 1-50:1, preferably 4-30:1; the height-to-diameter ratio refers to the ratio of the height of the upper cylindrical shell to the inner diameter of the upper cylindrical shell.

[0058] The bottom cone angle of the lower conical shell is 60 to 150 degrees, preferably 90 to 120 degrees.

[0059] In the present disclosure, the regenerator 2-1 also includes a feed pipe and a discharge pipe. The feed pipe is located at the top of the bed in the regenerator 2-1, and the discharge pipe is at the bottom of the regenerator 2-1. The inner diameters of the feed pipe and the discharge pipe of the regenerator 2-1 are 4 to 30 mm, preferably 6 to 10 mm.

[0060] The present invention discloses a discharge pipe equipped with a discharge valve connected to the cone bottom of the regenerator. During the evaluation process, the discharge speed and the bed storage capacity and bed height in the regenerator can be adjusted by controlling the opening of the discharge valve; after the evaluation is completed, it serves as a discharge outlet to empty the material.

[0061] In one embodiment, Figure 2 As shown, the spent charge storage and feeding unit includes a spent charge silo 1-1, a feeding screw 1-4, an external pressure protection gas structure 1-2 and a spent charge riser 1-5;

[0062] The feeding screws 1-4 are divided into a feeding section and a conveying section in sequence along the material flow direction. Preferably, the feeding screw further includes an idle section arranged upstream of the feeding section, that is, an idle section of the screw area is arranged between the feeding port of the feeding screw and the motor end of the screw, rather than directly feeding at the motor end of the screw;

[0063] Among them, the external pressure shielding gas structure 1-2 includes an external pressure shielding gas housing 1-2-5, a compacting end cover 1-2-7 and a particle feeder housing 1-2-1. The external pressure shielding gas housing 1-2-5 is sleeved on the outside of the idle section of the feeding screw 1-4, and the compacting end cover 1-2-7 is arranged at the end of the idle section. The compacting end cover 1-2-7 and the first end face of the external pressure shielding gas housing 1-2-5 are sealed by a shielding gas shaft seal 1-2-8.

[0064] A gap is defined between the inner wall of the external-pressure shielding gas housing 1-2-5 and the outer wall of the feeding screw 1-4, forming an annular cavity around the feeding screw 1-4. An air inlet pipe 1-2-6 and an air outlet pipe 1-2-9 are provided on the external-pressure shielding gas housing 1-2-5, extending therethrough. The annular cavity is connected to the gas source via the air inlet pipe 1-2-6 and to the exterior of the external-pressure shielding gas housing 1-2-5 via the air outlet pipe 1-2-9. Optionally, the transverse length of the annular cavity is 0.5 to 8 mm. In this disclosure, the transverse length of the annular cavity refers to the length of the annular cavity along the length of the screw.

[0065] In one embodiment, Figure 2 As shown, a pressure sensor and a first control valve are provided on the shielding gas inlet pipe 1-2-6; a back pressure valve is provided on the shielding gas outlet pipe 1-2-9 to adjust the pressure in the cavity;

[0066] The particle feeder housing 1-2-1 is sleeved on the outside of the feeding section of the feeding screw 1-4, and the first end surface of the particle feeder housing 1-2-1 and the second end surface of the external pressure protection gas housing 1-2-5 are sealed by a feeding shaft seal 1-2-2;

[0067] The inlet end of the standpipe 1-5 to be regenerated is communicated with the conveying section of the feeding screw 1-4, and the outlet end extends to the interior of the shell of the regenerator 2-1.

[0068] The present invention sets an external pressure protective gas structure in the feeding screw. The principle of the external pressure protective gas structure is: a small volume cavity is used to match a trace gas to obtain a higher pressure, and the high-pressure gas micro-group is used to block the tiny gaps that appear in the rotating shaft of the automatic particle feeder (feeding screw) during operation from the outside, so that the reaction system will not leak from the inside to the outside through these tiny pores. This device can not only prevent the leakage of reaction gas, but also prevent the dry hot fine powder from entering the tiny pores of the sealing surface to expand the pores and cause aging and failure of the sealing material. At the same time, due to the lengthening of the conveying section, problems such as arching and bridging, increased resistance loss along the way, particle extrusion, and increased particle wear occur during the particle conveying process. The present invention uses the trace gas flowing into the system through the external pressure protective gas structure to expand the distance between particles, increase material fluidity, improve the conveying effect, and effectively solve the above-mentioned problems caused by the growth of the conveying end. The trace gas in the external pressure shielding gas structure will not cause significant interference to the flow field and reactant concentration inside the regenerator, and the impact of the external pressure shielding gas structure can be ignored. The external pressure shielding gas uses nitrogen or inert gas to ensure that the solid material will not be contaminated or reacted by the gas components diffused or backflowed from downstream during the transportation and heating process.

[0069] The feeding screw in the present disclosure cooperates with the external pressure protection gas structure installed at the coupling end, thereby achieving the effect of the feeder stably conveying materials into the regenerator.

[0070] In one embodiment, Figure 1 As shown, the feeding screw 1-4 also includes a feeding inlet and a feeding outlet, which are arranged in the particle feeder housing 1-2-1; the feeding inlet is connected to the outlet of the spent agent silo 1-1, and the feeding outlet is connected to the spent agent inlet of the regenerator 2-1; along the material transmission direction of the feeding screw 1-4, the feeding inlet is located downstream of the shaft seal 1-2-2 and is spaced from the shaft seal 1-2-2 to form an idle section; preferably, the idle section length of the feeding screw 1-4 is 50 to 300 mm.

[0071] The present invention leaves an empty section in front of the feeding area, which can reduce the temperature increase of the rotating shaft caused by the preheating of the conveying section and protect the flexible sealing material at the shaft seal; at the same time, the empty area can also play a buffering role in special circumstances of the device, such as when the balance pipe is blocked or the external pressure protection gas pressure is insufficient or other reasons cause the regenerator pressure to be much greater than the particle automatic feeder pressure, to prevent the backflow gas carrying a large amount of particles from directly impacting the shaft seal and destroying the sealing structure.

[0072] In one embodiment, Figure 1 As shown, a solid preheater 1-3 is mounted externally on the conveying section of the feeding screw 1-4, forming a spent catalyst preheating section on the feeding screw 1-4. A gap exists between the preheating inlet of the solid preheater 1-3 and the feeding inlet of the feeding screw 1-4, and the feeding outlet of the feeding screw 1-4 is located within the spent catalyst preheating section. The installation of a solid preheater external to the feeding screw heats the spent catalyst to the target temperature before entering the regenerator, improving subsequent reaction efficiency within the regenerator and preventing large temperature fluctuations within the regenerator, facilitating steady-state simulation operation.

[0073] In one embodiment, the total length of the conveying section of the feeding screws 1-4 is 200 to 1000 mm. In the present disclosure, the total length of the conveying section between the feeding inlet and the feeding outlet is relatively long. The specific length can also be adjusted according to the pellet preheating requirements and the heating furnace power to maintain the final pellet discharge temperature between 10 and 550°C.

[0074] In a preferred embodiment, Figure 8 As shown, the idle sections and conveying sections of the feeding screws 1-4 have an inclination angle, preferably any inclination angle between -30° and 30°. In this disclosure, the inclination angle when the feeding outlet is higher than the feeding inlet is considered positive.

[0075] The automatic feeding device (feeding screw) used in the present invention is set with an inclination angle. When conveying particles with good fluidity, the conveying section is installed with an appropriate upward inclination (0 to 30 degrees) to increase feeding stability; when conveying particles with poor fluidity, it needs to be appropriately tilted downward (-30 to 0 degrees) to increase fluidity.

[0076] In one embodiment, Figure 1 As shown, the outlet end of the standpipe 1-5 to be produced is located above the heat exchange medium internal component 2-5 and is spaced apart from the top of the heat exchange medium internal component 2-5. Figure 1As shown, the height of the spent catalyst bed within the regenerator 2-1 is higher than the top of the heat exchange medium internals 2-5, so that the heat exchange medium internals 2-5 are completely placed in the spent catalyst bed. The outlet end of the spent catalyst riser 1-5 is located below the spent catalyst bed within the regenerator 2-1. Optionally, the outlet end of the spent catalyst riser 1-5 is located 10 to 50 mm below the spent catalyst bed within the regenerator 2-1 and is spaced apart from the top of the heat exchange medium internals 2-5. In the present disclosure, positioning the outlet end of the spent catalyst riser 1-5 below the spent catalyst bed within the regenerator 2-1 can provide a sealing effect.

[0077] In a specific embodiment, Figure 1 As shown, the system further includes a heating furnace 2-2, which is disposed outside the regenerator 2-1; optionally, there are one or more heating furnaces 2-2. During the evaluation test, the regenerator can be heated by the heating furnace to maintain a stable temperature inside the regenerator.

[0078] In one embodiment, Figure 1 As shown, the system further includes a char gas supply unit, which includes a pressure regulating valve 4-1, a gas flow meter 4-2, a gas preheater 4-3 and a gas distributor 2-6;

[0079] The gas preheater 4-3 is provided with a gas preheating inlet and a gas preheating outlet. The gas preheating inlet is connected to the charring gas source. The gas source introduction pipeline of the gas preheating inlet is provided with a pressure regulating valve 4-1 and a gas flow meter 4-2 in sequence along the gas flow direction. The present disclosure monitors the charring gas introduction flow rate by the gas flow meter 4-2 and controls the charring gas flow rate by adjusting the opening of the pressure regulating valve 4-1.

[0080] The gas distributor 2-6 is provided with a charred gas inlet and distribution holes, and the charred gas inlet is connected to the preheating gas outlet of the gas preheater 4-3; the gas distributor 2-6 extends from the lower part of the shell of the regenerator 2-1 into the regenerator 2-1, and the outlet of the distribution holes of the gas distributor 2-6 is toward the bottom of the shell of the regenerator 2-1.

[0081] In a preferred embodiment, the gas distributor 2-6 extends from the bottom of the upper cylindrical shell of the regenerator 2-1 into the regenerator 2-1, and the outlet of the distribution holes of the gas distributor 2-6 faces the bottom of the lower conical shell of the regenerator 2-1.

[0082] In the system provided by the present invention, the charred gas is controlled by a pressure-stabilizing valve and a gas flow meter to reach a target flow rate, is heated by a gas preheater, and is evenly sprayed downward into the regenerator through a gas distributor. Under the combined action of the cone bottom reflection and the pressure gradient, the flow direction is changed to from bottom to top. During the upward flow, the charred gas comes into contact with solid particles, which can make the solid particles fluidized under the action of the charred gas and undergo charred regeneration.

[0083] The gas distributor 2-6 used in the present disclosure can adopt a conventional structure in the art. In a specific embodiment, the gas distributor 2-6 is an annular hollow tube structure.

[0084] In one embodiment, Figure 1 As shown, the system further includes an analysis unit; the analysis unit includes a flue gas sampling device 5-5 and an exhaust gas analyzer 5-4; the regenerator 2-1 further includes a flue gas filter device 2-3, and the flue gas filter device 2-3 is arranged at the upper part of the regenerator 2-1 housing; the flue gas inlet of the exhaust gas analyzer 5-4 is connected to the flue gas outlet of the flue gas filter device 2-3;

[0085] A flue gas collection port is provided on the shell side wall of the regenerator 2-1, and the flue gas collection port is connected to the flue gas sampling device 5-5. Preferably, a plurality of flue gas collection ports are provided at different heights on the shell side wall along the axial direction of the regenerator 2-1.

[0086] In one embodiment, two or more sampling ports are provided at different heights in the dense phase section of the regenerator; and two or more sampling ports are provided in the dilute phase section. Figure 6 As shown, a sampling port is provided on the side wall of the regenerator 2-1 (taking one sampling port as an example), and the sampling inlet of the flue gas sampling tube 5-5-1 enters the interior of the regenerator 2-1 through the sampling port of the regenerator 2-1. A filter 5-5-3 is provided at the head of the flue gas sampling tube 5-5-1, and a temperature sensor 5-5-2 is provided inside. The flue gas sampling tube 5-5-1 is also connected to a pressure sensor 5-5-4 and a gas sampling bag 5-5-6. The pressure sensor and temperature sensor connected to the flue gas sampling tube 5-5-1 can also monitor the pressure and temperature at different bed heights in the regenerator, making it easier to control the steady-state environment in the regenerator. The flue gas sampling tube 5-5-1 is also provided with a flue gas sampling valve 5-5-5 to facilitate the control of flue gas sampling.

[0087] In one embodiment, Figure 1As shown, the system also includes a regenerant recovery unit; the regenerant recovery unit includes a discharge valve 3-1, a discharge bin 3-2, a discharge bin air inlet valve 3-3, a discharge bin back pressure valve 3-4, a pressure sensor 3-5 and a discharge valve 3-6; the discharge bin 3-2 is provided with a regenerant inlet, a discharge outlet, a discharge bin air inlet and a discharge bin gas outlet; the regenerant inlet is connected to the regenerant outlet of the regenerator 2-1; the discharge bin air inlet is provided at the upper part of the discharge bin 3-2, and a discharge bin air inlet valve 3-3 is provided on the connecting pipeline between the discharge bin air inlet and the gas source;

[0088] The discharge silo gas outlet is located at the top of the discharge silo 3-2 and communicates with the external environment via a gas outlet pipeline. A discharge silo backpressure valve 3-4 is installed on the gas pipeline, and a pressure sensor 3-5 is installed between the discharge silo gas outlet and the discharge silo backpressure valve 3-4. The discharge rate, bed capacity, and bed height are adjusted by controlling the difference between the internal pressure of the discharge silo and the internal pressure of the regenerator.

[0089] When using the system provided by the present invention for evaluation, the specific process parameters in the evaluation reaction can be set according to the specific parameters of the target industrial device, such as feed rate, char gas velocity, pressure in the regenerator, temperature in the regenerator and other parameters; the specific process parameters can also be calculated and determined using methods known in the art.

[0090] In one exemplary embodiment, Figure 1 The specific process flow of the continuous catalytic cracking regeneration operation simulation evaluation system shown includes:

[0091] The spent charge in the spent charge silo 1-1 enters the feeding screw 1-4 through the feeding inlet and is automatically fed to the feeding outlet under the action of the screw. During the automatic feeding of the spent charge, protective gas is introduced into the cavity of the outward pressure protective gas structure. The spent charge is preheated in the spent charge preheating section of the feeding screw 1-4 and then enters the regenerator 2-1 through the spent charge riser 1-5.

[0092] The charred gas passes through the pressure regulating valve 4-1, the gas flow meter 4-2, and the gas preheater 4-3 in sequence. The preheated charred gas at the target flow rate is ejected through the distribution holes on the gas distributor 2-6 toward the bottom of the lower conical shell of the regenerator 2-1. The flow direction is changed from bottom to top due to the combined effects of the cone bottom reflection and the pressure gradient of the lower conical shell. During the upward flow, the charred gas comes into contact with the solid particles (regenerated agent), causing the regenerated agent to be charred and regenerated, forming regenerated flue gas and regenerated agent. During the charred regeneration process, heat exchange medium is introduced into the heat exchange medium inlet of the heat exchange medium internal component 2-5 in the form of a variable diameter spiral coil in the regenerator 2-1, and the heat exchanged heat exchange medium is discharged through the heat exchange medium outlet.

[0093] The flue gas is sampled through the sampling port on the side wall of the regenerator, and the pressure, temperature and other parameters at different bed heights can also be monitored. After a part of the regenerated flue gas rises to the upper part of the regenerator 2-1, it is filtered by the flue gas filter device 2-3 and then enters the exhaust gas analyzer 5-4 for flue gas composition analysis;

[0094] The discharge amount of the regenerated agent in the regenerator 2-1 is controlled by adjusting the opening and closing degree of the discharge valve 3-1 on the regenerator discharge pipe. The regenerated agent enters the discharge bin 3-2, and the pressure in the discharge bin and the discharge of the regenerated agent are detected and controlled by the discharge bin air inlet valve 3-3, the discharge bin back pressure valve 3-4 and the pressure sensor 3-5. The regenerated agent is drawn out through the discharge valve 3-6, and the carbon content and other parameters of the regenerated agent are detected as needed to evaluate the regeneration situation.

[0095] A second aspect of the present disclosure provides a method for simulating and evaluating a continuous catalytic cracking regeneration operation, using the system described in the first aspect of the present disclosure. The method comprises the following steps:

[0096] The spent catalyst is fed into the regenerator 2-1 through the feed outlet of the spent catalyst feeding unit; and the charred gas is introduced into the regenerator 2-1 through the charred gas supply unit, and the spent catalyst is subjected to charred regeneration treatment in the regeneration gasifier 2-1 to obtain regenerated flue gas and regenerated catalyst;

[0097] Introducing heat exchange medium into the variable diameter spiral coil tube through the heat exchange medium inlet of the heat exchange medium internal component 2-5, so that the heat exchange medium exchanges heat with the material in the regenerator 2-1;

[0098] The regeneration flue gas is allowed to enter the analysis unit for analysis; and the regeneration agent is allowed to enter the regeneration agent recovery unit for regeneration agent recovery treatment.

[0099] The method provided by the present invention can maintain a continuous regeneration reaction for a period of time, and is conducive to maintaining the steady state in the system during the simulation evaluation process. It can simulate the reaction conditions that are closer to those in the actual industrial regeneration device. The parameters such as temperature, operating pressure, inlet and outlet gas composition, inlet and outlet catalyst carbon content, particle residence time, interphase mass transfer resistance, char intensity, and temperature field distribution in the bed can be simulated on the industrial catalytic cracking regeneration device through continuous and stable material inlet and outlet, hot feed, optimization of bed fluidization quality, and bed heat extraction.

[0100] In a specific embodiment, the spent catalyst used in the present disclosure can be selected from a spent catalyst obtained by a catalytic cracking process in a factory or a carbonization reaction in a pilot plant; preferably, the spent catalyst has a carbon content of 0.5 to 3% by weight; and an average particle size of 60 to 90 μm.

[0101] In one specific embodiment, the carbon content of the regeneration agent flowing out of the regenerator 2-1 is 0.01 to 1% by weight.

[0102] In one embodiment, the reaction conditions in the regenerator include: a temperature of 500-800°C, preferably 650-750°C, a pressure of 0-0.5 MPa, preferably 0.15-0.25 MPa; a temperature of the charred gas of 20-500°C, preferably 150-300°C; a volume space velocity of 6-50,000 h -1 , preferably 200 to 3000 hours -1 The residence time of the spent agent is 1 to 240 minutes, preferably 2 to 60 minutes. The heat exchange medium can be any one of air, deionized water and molten salt. The molten salt can be a binary nitrate, for example, the binary nitrate includes 50 to 70 weight percent KNO3 and 30 to 50 weight percent NaNO3. When the heat exchange medium is air, the inlet temperature is 5 to 30°C and the pressure is 0 to 0.2 MPa. When the heat exchange medium is deionized water, the inlet temperature is 40 to 150°C and the pressure is 0 to 4 MPa. When the heat exchange medium is molten salt, the inlet temperature is 250 to 350°C and the pressure is 0 to 0.2 MPa.

[0103] Optionally, the volume content of oxygen in the charring gas composition is 10 to 40 volume %.

[0104] In one embodiment, the method further comprises preheating the spent catalyst entering the spent catalyst feeding unit; and then allowing the preheated spent catalyst to enter the regenerator 2-1; preferably, the temperature of the preheated spent catalyst is 10-550°C;

[0105] Optionally, the feed screw 1-4 in the spent catalyst feeding unit feeds the regenerator 2-1 at a rate of 0.1 to 20 g / s, preferably 0.5 to 8 g / s. The working pressure of the feed screw 1-4 in the spent catalyst feeding unit is 0 to 0.5 MPa, preferably 0.15 to 0.25 MPa. In this disclosure, the working pressure of the feed screw 1-4 refers to the air pressure within the screw housing during screw transmission.

[0106] By adopting the above process parameters provided by the present disclosure, it is possible to further maintain the steady state within the system during the simulation evaluation process.

[0107] The present disclosure will be further described below with reference to specific embodiments.

[0108] In the following examples and comparative examples, the carbon content of the regeneration agent is measured by drying the regeneration agent sample and then feeding it into a carbon and sulfur element analyzer or an organic element analyzer.

[0109] The concentrations of CO2 and CO in the flue gas are detected in real time by a 5-4 tail gas analyzer, and the test results are displayed on a computer in real time.

[0110] Example 1

[0111] use Figure 1 The continuous catalytic cracking regeneration operation simulation evaluation system shown in the figure includes the following specific device structures:

[0112] The volume of the raw agent silo 1-1 is 20L, and the feeding screw 1-4 is arranged in the horizontal direction without an inclination angle; the screw thread is a rectangular thread made of steel plate with a thread thickness of 1.5mm, a thread pitch of 20mm, a major diameter of the screw of 40mm, and a minor diameter of the screw of 20mm. The feeding shaft seal and the protective gas shaft seal are made of polytetrafluoroethylene material. The horizontal length of the idle section of the feeding screw 1-4 is 100mm, and the length of the conveying section is 600mm; the inner diameter of the air inlet pipe 1-2-6 of the external pressure protective gas structure 1-2 is 4mm, and the outer diameter is 6mm. The air inlet pipe 1-2-6 is externally connected to an argon cylinder and a gas quality controller. The air outlet pipe of the external pressure protective gas structure is connected to an electrically controlled needle valve. The horizontal length of the annular cavity of the external pressure protective gas structure is 4mm. A solid preheater 1-3 is arranged outside the conveying section of the feeding screw 1-4, and the outlet of the conveying section is connected to a standpipe 1-5 to be produced with an outer diameter of 12 mm and a wall thickness of 1.5 mm. The standpipe 1-5 to be produced is vertically inserted into the regenerator 2-1 along the axis of the regenerator 2-1, and the outlet of the standpipe 1-5 to be produced is arranged 30 mm below the bed layer of the experimental static bed, where the height of the experimental static bed is 240 mm.The shell of the regenerator 2-1 consists of an upper cylindrical shell and a lower conical shell. The inner diameter of the upper cylindrical shell of the regenerator 2-1 is 60mm, the height of the upper cylindrical shell is 1500mm, and the height-to-diameter ratio is 25:1; the cone angle of the lower conical shell is 120°, and the total height of the regenerator 2-1 shell is 1518mm. A heating furnace is arranged outside the regenerator 2-1. The dense phase section of the regenerator 2-1 is arranged with two sampling ports on the side wall along the axial direction to connect to the flue gas sampling equipment 5-5; the dilute phase section is arranged with a sampling port on the side wall along the axial direction. The configuration is the same as that of the dense phase sampling port; the flue gas filter device 2-3 uses a 316 material metal powder filter with a filtration accuracy of 3μm; the flue gas filter device 2-3 is externally connected to the regenerator back pressure valve and gas mass flow meter, and finally sent to the flue gas analyzer and exhaust treatment; the middle of the regenerator 2-1 is 130mm away from the upper surface of the gas distributor 2-6, and a heat exchange medium internal component 2-5 made of a seamless steel pipe with a reducing plate is installed. The internal hollow of the heat exchange medium internal component 2-5 is filled with cooling water in a bottom-in and top-out manner, wherein the heat exchange medium internal component The maximum coil diameter of 2-5 is 54mm (the maximum coil diameter is 90% of the inner diameter of the regenerator 2-1 shell), the vertical height is 47mm, the centerline thread pitch of each layer of coil is 10.5mm, the inner diameter of the steel pipe is 4.5mm, and the wall thickness is 2mm; the gas distributor 2-6 at the bottom of the regenerator uses a gas distribution ring made of a seamless steel pipe with an outer diameter of 8mm and a wall thickness of 1mm, with 10 holes with an aperture of 1mm evenly distributed along the ring; the regenerant outlet at the bottom of the regenerator 2-1 is connected to a gas distribution ring with an outer diameter of 12mm and a wall thickness of 1.5mm. seamless steel pipe, then connected to the discharge valve 3-1 and then to the discharge silo 3-2; one side of the discharge silo 3-2 is connected to the air inlet pipe with an outer diameter of 8mm and a wall thickness of 1mm, the discharge silo air inlet valve 3-3, and is connected to the nitrogen gas source, and one side of the discharge silo 3-2 is connected to the air outlet pipe with an outer diameter of 8mm and a wall thickness of 1mm, the pressure sensor 3-5 and the discharge silo back pressure valve 3-4; the charred gas inlet of the gas distributor 2-6 of the regenerator 2-1 is connected to the gas preheater 4-3, the gas flow meter 4-2, the pressure regulating valve 4-1 and the charred gas source in sequence.

[0113] During the regeneration process, the spent agent is stored in the spent agent silo 1-1 and is driven by the screw rotation of the feeding screw 1-4 and the protective gas of the external pressure protective gas structure 1-2 (the ventilation volume of the protective gas is 0.03m 3 / h, the pressure of the external pressure protection gas structure 1-2 is 0.15MPa), and then heated to the target temperature (350℃) by the solid preheater 1-3, and flows into the regenerator 2-1 along the standpipe 1-5. The feeding speed into the regenerator 2-1 is 2g / s, and the working pressure of the feeding screw is 0.15MPa. And the charred gas (the composition of the charred gas includes: 21% by volume of oxygen and 79% by volume of nitrogen) is controlled by the pressure regulating valve 4-1 and the gas flow meter 4-2 to reach the target flow rate (0.992m 3 / h), is heated to 130°C by gas preheater 4-3, and is uniformly sprayed downward into regenerator 2-1 through gas distributor 2-6. The flow direction changes from bottom to top due to the combined effects of reflection at the cone bottom and the pressure gradient. During the upward flow, it comes into contact with solid particles (spent catalyst, carbon content 1.145 wt%), fluidizing the solid particles and initiating char regeneration. The reaction conditions in regenerator 2-1 include: temperature 700°C, pressure 0.15 MPa, superficial velocity of the char gas 0.13 m / s, volume space velocity 1488 h / s. -1 The residence time of the regenerated agent is 5 minutes. The variable diameter spiral coil-shaped heat exchange medium component 2-5 within regenerator 2-1 breaks large bubbles into small ones, enhancing gas-solid contact and preventing surges. The regenerated flue gas passes upward through a flue gas filter to remove any entrained fines, then flows through a back pressure valve and a gas flow meter for analysis and processing by flue gas analyzer 5-4. During the experiment, a flue gas sampling device continuously samples and collects the reaction gases while also monitoring the bed pressure and temperature. The heat medium flow rate is adjusted based on the feedback from temperature sensor 5-5-2 to maintain a temperature of 700°C within regenerator 2-1. The regenerated agent particles flow from the bottom of regenerator 2-1 through the discharge hopper 3-2, controlled by the pressure differential between regenerator 2-1 and the discharge hopper 3-2 and the opening of discharge valve 3-1.

[0114] Testing revealed that the carbon contents of the regenerated agent obtained at reaction times of 10 minutes, 20 minutes, 30 minutes, and 40 minutes were 0.082%, 0.086%, 0.084%, and 0.085% by weight, respectively. Furthermore, in the petroleum refinery that provided this regenerated agent, the carbon content of the regenerated agent for the catalytic cracking unit was 0.08-0.09% by weight. These data demonstrate that the experimental results using the evaluation device disclosed herein are consistent with industrial data, demonstrating good simulation results. Furthermore, the carbon content of the regenerated agent obtained at different reaction times in the disclosed embodiment exhibited minimal variation, enabling continuous steady-state operation.

[0115] in addition, Figure 7 The curve of the flue gas CO2 and CO concentration changes with experimental time during the experiment of this embodiment shows that the flue gas CO2 and CO concentrations first increase and then reach a stable state during the experiment of this embodiment, which also represents that the internal state of the reactor 2-1 has reached dynamic equilibrium (after dynamic equilibrium, CO2 in the flue gas accounts for 9.5-10% of the total volume of the flue gas, and CO in the flue gas accounts for 6.8-7.3% of the total volume of the flue gas). In the industrial regeneration flue gas data provided by the oil refinery, CO and CO2 account for 7% and 10% of the total volume of the flue gas, respectively. Figure 7 The results show that the evaluation device results have a good correspondence with the industrial data, which also illustrates that the device and method provided by the present disclosure can achieve continuous steady-state operation and good simulation effects.

[0116] Example 2

[0117] use Figure 8 The continuous catalytic cracking regeneration operation simulation evaluation system shown in the figure has a specific device structure similar to that of Example 1. The only difference from the system structure in Example 1 is that the spent catalyst particles added in this example (the spent catalyst has a carbon content of 1.363% by weight) have strong adhesion. In this embodiment, the motor, screw, and solid preheater 1-3 in the feeding screw 1-4 are installed downward at an angle of 5° to the horizontal plane, and the gas volume and pressure of the external pressure shielding gas are increased (the shielding gas ventilation volume is 0.036m 3 / h, pressure is 0.152MPa), the heat exchange medium internal components in the reactor are selected to connect two internal components at the small diameter according to the "cone angle to cone angle", such as Figure 5 As shown (the specific structure of the single-piece internal component is the same as that in Example 1), its ability to improve the fluidization effect is increased and the imbalance is reduced.

[0118] The curve of flue gas CO2 and CO concentration changing with experimental time during the experiment of this embodiment is similar to that of Example 1. Figure 7 Similarly, it is shown that in the experiment of this embodiment, the concentrations of CO2 and CO in the flue gas first increase and then reach a stable state, which also means that the internal state of the reactor 2-1 reaches a dynamic equilibrium, indicating that the device and method provided by the present disclosure can achieve continuous steady-state operation.

[0119] Testing showed that the carbon contents of the regenerated agent obtained at reaction times of 10, 20, 30, and 40 minutes were 0.092, 0.091, 0.09, and 0.092 weight percent, respectively. This is close to the 0.09 weight percent carbon content of the industrial regenerated agent provided by the manufacturer of the regenerated agent, demonstrating good simulation results. Furthermore, the carbon content of the regenerated agent obtained at different reaction times in the present disclosure varies little, enabling continuous steady-state operation.

[0120] Example 3

[0121] A system and method similar to that of Example 1 are used, but the differences from Example 1 are as follows:

[0122] The feeding screw 1-4 is not provided with an idle section, nor is an external pressure protection gas structure 1-2 provided. The feeding screw only includes a feeding section and a transmission section. The length of the transmission section is the same as that of Example 1; the remaining parts and operating parameters are the same as those of Example 1.

[0123] The experimental results of this example show that the carbon content of the regenerated agent obtained at reaction times of 10 min, 20 min, 30 min, and 40 min was 0.088 wt%, 0.089 wt%, 0.063 wt%, and 0.047 wt%, respectively. The carbon content of the regenerated agent began to decline significantly after 30 min. Simultaneously, data from the bed pressure sensor indicated that at 26 min into the experiment, the pressure at each monitoring point within the bed suddenly dropped, and the bed pressure drop also decreased. However, the screw speed and the charred gas flow rate remained unchanged during operation, indicating a feed blockage. Analysis revealed that this phenomenon was caused by gas leakage at the dynamic seal, which caused catalyst particles to flow back through the screw conveying section and the standpipe to be regenerated, resulting in a feed blockage, a reduction in bed storage, an increase in particle residence time and oxygen-carbon ratio, and ultimately a decrease in the carbon content of the regenerated agent. During a shutdown inspection, it was discovered that the device, which had successfully passed the airtightness test before the experiment, had begun to leak significantly from the feeder shaft seal. This shows that the device that does not adopt the idle section and external pressure protection gas structure is prone to problems such as poor feeding and poor evaluation effect.

[0124] Example 4

[0125] The same system and similar method as in Example 1 are used, but the difference from Example 1 is that:

[0126] The reaction conditions in the regenerator were adjusted to: temperature 400°C, pressure 1.0 MPa; volume space velocity of the charred gas was 22880 h -1 , the superficial velocity of the charred gas is 1.5m / s; the residence time of the spent agent is 0.8min;

[0127] The feeding conditions were adjusted as follows: the feeding speed of the feeding screw 1-4 to the regenerator 2-1 was 13.9 g / s, and the working pressure of the feeding screw 1-4 was 1.0 MPa.

[0128] The experimental results of this example show that the carbon contents of the regenerated agent obtained at reaction times of 10, 20, 30, and 40 minutes were 0.854, 0.862, 0.866, and 0.858 weight percent, respectively. These carbon contents are significantly higher than the 0.1 weight percent carbon content required for catalytic cracking, indicating poor regeneration. Furthermore, data from the bed pressure sensor indicates that during the experiment, the internal bed pressure gradually increased and then suddenly decreased, with the increase exceeding 2000 Pa. In the experiment of Example 1 using the same apparatus, this value was less than 500 Pa. This phenomenon occurs because the operating parameters, including excessively low temperature, result in a low carbonization reaction rate, and excessively high gas volumetric space velocity and superficial gas velocity, lead to throttling. This demonstrates that the process conditions employed in Example 1 achieve superior spent agent regeneration, with minimal bed fluctuations and the ability to maintain a steady state.

[0129] Comparative Example 1

[0130] When evaluating regeneration using a common fixed fluidized bed, an intermittent operation is used regardless of the form and size of the regenerator, the composition of the gas received, or the principle and accuracy of the post-processing instrument.

[0131] Comparative Example 1 uses the same regenerator and reaction materials as Example 1. The difference is that intermittent operation is used: that is, a certain amount of spent catalyst as in Example 1 is weighed before the reaction and placed in the regenerator, without continuous feeding and withdrawing of spent catalyst.

[0132] The temperature and pressure in the regenerator are first raised to the same temperature and pressure as in Example 1 under a nitrogen or inert gas atmosphere. At this time, the same charred gas as in Example 1 is switched to react and the flue gas components are detected.

[0133] The curve results of the flue gas CO2 and CO concentration changes with the experimental time during the comparative experiment are as follows: Figure 9 As shown in the figure, the CO2 and CO concentrations in the flue gas fluctuate continuously as the reaction proceeds, first increasing and then decreasing, unable to reach a steady state. This differs from the continuous and stable state observed during actual catalytic cracking regeneration, resulting in poor simulation results. Therefore, the device and method provided in Comparative Example 1 cannot achieve continuous steady-state simulation, operational preview, and optimization guidance for industrial regeneration equipment. Using data corresponding to peak values clearly does not conform to general chemical reaction patterns and is difficult to represent in practice.

[0134] Furthermore, testing revealed that the carbon contents of the regenerated agent obtained at reaction times of 10, 20, 30, and 40 minutes were 0.653, 0.107, 0.015, and 0.009 weight percent, respectively. This indicates that at the initial stage of the reaction, the carbon content of the regenerated agent was far higher than the 0.1 weight percent carbon content required by the catalytic cracking process, indicating poor regeneration effectiveness. Furthermore, the carbon content of the regenerated agent obtained at different reaction times varied significantly, making continuous steady-state operation impossible.

[0135] Comparative Example 2

[0136] Comparative Example 2 differs from Example 1 in that the device structure uses a design proportionally scaled down from the industrial regenerator, with a dense phase section of 60 mm; the particle conveying method uses a traditional screw or twin-screw feeder. Due to device size limitations, the currently commonly used fluidized bed external heat extraction device requires additional design. The external heat extraction structure also needs to consider the layout of the heat extraction device body and the supporting pumps and valves. During operation, it is also necessary to take into account the precise control of the circulation volume and residence time distribution of the particles in a small device, which will lead to an increase in workload. Therefore, an external heat extraction structure is not used, and an axial vertical heat extraction device from top to bottom is adopted. At the same time, due to space limitations within the bed, it is impossible to lay complex internal components within the bed, so traditional porous plate internal components are used. However, the internal components cannot affect the fluidization effect of the vertical heat extraction section extending from the top.

[0137] In actual use, the feeder shaft seal is very susceptible to aging due to the high temperature and pressure conditions inside. At the same time, the presence of fine particles will exacerbate this aging process. When gas leakage begins, the fine powder carried by the gas will expand the shaft seal gap and cannot recover on its own. The leakage phenomenon will become more and more obvious. When the leakage volume is too high, a significant updraft will appear in the standpipe to be produced. When the drag force is equal to the gravity of the particles, the particles cannot fall. If the problem is not discovered and stopped in time, and the screw is allowed to continue working, the entire standpipe to be produced and the screw conveying space will be filled. Then, as the screw rotates, the solid particles that have already filled the conveying space will be squeezed. The axial reaction force acting on the screw will damage the coupling, and the circumferential torque will burn out the motor. If the gas supply is not discovered and stopped in time, a large amount of carbon-containing solids in the conveying space will come into contact with a small amount of oxygen that flows back from the gaps between the particles. Incomplete combustion will produce a large amount of carbon monoxide. When the shaft end structure of the feeder is damaged, the gas inside the system will be ejected with high-temperature particles. During the ejection process, the high temperature will come into contact with the air and burn to release heat. If the carbon monoxide concentration is too high, it may even cause an explosion.

[0138] Because the reactor bed is filled with horizontal plate-like internals with openings and vertical heat pipes are placed in the upper middle portion, the vertical heat exchange area is related to the pipe diameter, height, and number of pipes arranged. The height is affected by the bed height, while the pipe diameter and number of pipes arranged are limited by the internal space. Excessive vertical pipes can lead to channeling and slugging, and occupying too much bed space can affect the distribution of reactants within the reactor.

[0139] Therefore, from the perspective of the device, the service life of the device in Comparative Example 2 is short, and it may cause fire and explosion if not paid attention to. At the same time, the flow field distribution inside the reactor and the product during operation are somewhat different from those of industrial devices.

[0140] Comparative Example 3

[0141] A method and system similar to Example 1 are used, but the difference from Example 1 is that:

[0142] No heat exchange medium internal components are provided in the shell of regenerator 2-1. The remaining operating parameters are the same as those in Example 1.

[0143] After testing, it was found that when the reaction time was 10 min, 20 min, 30 min and 40 min, the carbon content of the obtained regeneration agent was 0.086 wt%, 0.077 wt%, 0.075 wt% and 0.063 wt%, respectively.

[0144] The results of this comparative experiment show that due to the slow heat dissipation from the bed, the bed temperature increased excessively as the experiment progressed (temperature sensors showed temperatures exceeding 810°C), resulting in a higher rate of charring than in actual industrial processes. Consequently, the carbon content of the regenerated agent obtained in this comparative experiment was also lower than the 0.08-0.09 wt% range found in industrial processes, indicating that this comparative example cannot accurately simulate and evaluate the regeneration process. This operation also carries certain risks; the experiment should be terminated immediately if the temperature shows signs of exceeding the limit.

[0145] Comparative Example 4

[0146] A method and system similar to Example 1 are used, but the difference from Example 1 is that:

[0147] An equal-diameter spiral coil is set in the shell of regenerator 2-1, with a coil diameter of 54 mm. The vertical height, layer coil centerline thread pitch and other parameters are the same as those in Example 1; the same bottom-in and top-out method is adopted for the heat exchange medium; the other operating parameters are the same as those in Example 1.

[0148] After testing, it was found that when the reaction time was 10 min, 20 min, 30 min and 40 min, the carbon content of the obtained regeneration agent was 0.129 wt%, 0.133 wt%, 0.128 wt% and 0.13 wt%, respectively.

[0149] The experimental results of this comparative example show that the regeneration effect is not good. The carbon content of the regeneration agent is higher than the 0.1 weight% carbon content required by the catalytic cracking process, and the regeneration effect is poor. The reason is that the equal-diameter spiral coil only has the function of heat exchange and basically has no effect on improving the fluidization quality. Therefore, there are problems such as poor gas-solid contact and too wide distribution of particle residence time in the bed. The poor regeneration charcoal burning effect and the excessively high carbon content of the regeneration agent are manifestations of the above problems. Therefore, this comparative example cannot accurately simulate and evaluate the regeneration process.

[0150] 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.

[0151] 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.

[0152] 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 continuous catalytic cracking regeneration operation simulation evaluation system, characterized in that: The system comprises a spent catalyst storage and feeding unit and a regenerator (2-1); The regenerator (2-1) comprises a shell, a spent agent inlet, a heat exchange medium internal component (2-5), a burnt gas inlet, and a regenerated agent outlet; the heat exchange medium internal component (2-5) is formed as a variable diameter spiral coil and is arranged inside the shell in an axial direction of the regenerator (2-1); The heat exchange medium internal component (2-5) includes a heat exchange medium inlet and a heat exchange medium outlet; the heat exchange medium inlet and the heat exchange medium outlet are respectively extended to the outside of the regenerator (2-1) shell through pipelines, so that the heat exchange medium in the heat exchange medium internal component (2-5) tube exchanges heat with the material inside the regenerator (2-1) shell only through the tube wall; The variable diameter spiral coil is formed by winding a through hollow tube along a conical spiral line; and along the axial direction of the regenerator (2-1) shell, the winding diameter of the variable diameter spiral coil gradually increases from top to bottom to form a cone in an upright shape, or the winding diameter gradually decreases from top to bottom to form an inverted cone, or a plurality of the variable diameter spiral coils are combined and installed, and the combined installation method includes: the conical top end of one variable diameter spiral coil is connected to the conical top end of another variable diameter spiral coil, or the conical bottom end of one variable diameter spiral coil is connected to the conical bottom end of another variable diameter spiral coil.

2. The system according to claim 1, wherein: The inner diameter of the variable diameter spiral coil is 3-8 mm, the centerline thread pitch of each layer of the coil is 3-15 mm; the wall thickness of the variable diameter spiral coil is 0.75-2 mm; The maximum winding diameter of the variable diameter spiral coil is 80-95% of the inner diameter of the regenerator (2-1) shell, wherein the maximum winding diameter refers to the maximum diameter of the conical shape of the variable diameter spiral coil.

3. The system according to claim 1, wherein: The hollow tube is a seamless steel tube.

4. The system according to claim 3, characterized in that The shape of the hollow tube is a round tube or a square tube.

5. The system according to claim 1, wherein: The shell of the regenerator (2-1) is a cylinder with a constant diameter or a cylinder with a variable diameter; and the cross section of the shell of the regenerator (2-1) is circular.

6. The system according to claim 5, characterized in that The shell of the regenerator (2-1) is a variable diameter cylinder, which is composed of an upper cylindrical shell and a lower conical shell that are coaxially sealed and connected; the heat exchange medium internal component (2-5) is arranged in the upper cylindrical shell of the regenerator (2-1) and is coaxially arranged with the upper cylindrical shell; the regeneration agent outlet is arranged at the bottom of the lower conical shell, and the regeneration agent outlet is connected to the regeneration agent recovery unit.

7. The system according to claim 6, characterized in that The inner diameter of the upper cylindrical shell is 30-100 mm; the height-to-diameter ratio is 1-50:1; The bottom cone angle of the lower conical shell is 60-150 degrees.

8. The system according to claim 7, characterized in that The height-to-diameter ratio of the upper cylindrical shell is 4-30:1; The bottom cone angle of the lower conical shell is 90-120 degrees.

9. The system according to claim 1, wherein: The spent charge storage and feeding unit comprises a spent charge silo (1-1), a feeding screw (1-4), an external pressure protection gas structure (1-2) and a spent charge riser (1-5); The feeding screw (1-4) includes an idle section, a feeding section and a transmission section; The external pressure protection gas structure (1-2) comprises an external pressure protection gas housing (1-2-5), a pressing end cover (1-2-7) and a particle feeder housing (1-2-1); the external pressure protection gas housing (1-2-5) is sleeved on the outside of the idle section of the feeding screw (1-4); the pressing end cover (1-2-7) is arranged at the end of the idle section; the pressing end cover (1-2-7) and the first end face of the external pressure protection gas housing (1-2-5) are sealed by a protection gas shaft seal (1-2-8); A gap is provided between the inner wall of the external pressure protective gas housing (1-2-5) and the outer wall of the feeding screw (1-4) to form an annular cavity around the feeding screw (1-4); an air inlet pipe (1-2-6) and an air outlet pipe (1-2-9) that pass through the inside and outside are provided on the external pressure protective gas housing (1-2-5), so that the annular cavity is connected to the gas source through the air inlet pipe (1-2-6) and is connected to the outside of the external pressure protective gas housing (1-2-5) through the air outlet pipe (1-2-9).

10. The system according to claim 9, characterized in that The transverse length of the annular cavity is 0.5-8 mm.

11. The system according to claim 9, wherein: The air inlet pipe (1-2-6) is provided with a pressure sensor and a first control valve; the air outlet pipe (1-2-9) is provided with a back pressure valve; The particle feeder housing (1-2-1) is sleeved on the outside of the feeding section of the feeding screw (1-4), and a first end surface of the particle feeder housing (1-2-1) and a second end surface of the external pressure protection gas housing (1-2-5) are sealed via a feeding shaft seal (1-2-2); The inlet end of the standpipe (1-5) to be regenerated is communicated with the transmission section of the feeding screw (1-4), and the outlet end extends to the interior of the shell of the regenerator (2-1).

12. The system according to claim 9, wherein: The idle section length of the feeding screw (1-4) is 50-300 mm; the total length of the transmission section is 200-1000 mm.

13. The system according to claim 9, wherein: The transmission section of the feeding screw (1-4) is externally sheathed with a solid preheater (1-3).

14. The system according to claim 9, wherein: The feeding screws (1-4) have an inclination angle from the idle section to the transmission section.

15. The system according to claim 14, wherein: The feeding screws (1-4) have any inclination angle between -30° and 30° along the idle section to the transmission section.

16. The system according to claim 9, wherein: The outlet end of the standpipe (1-5) to be regenerated is located above the heat exchange medium internal component (2-5) and is spaced apart from the top of the heat exchange medium internal component (2-5), and the inlet end of the standpipe (1-5) to be regenerated is located below the static bed layer of the regenerator (2-1).

17. The system according to claim 9, wherein: The system further comprises a heating furnace (2-2), wherein the heating furnace (2-2) is arranged outside the regenerator (2-1).

18. The system according to claim 17, wherein: The number of the heating furnaces (2-2) is one or more.

19. The system according to claim 1, wherein: The system also includes a char gas supply unit, which includes a pressure regulating valve (4-1), a gas flow meter (4-2), a gas preheater (4-3) and a gas distributor (2-6); The gas preheater (4-3) is provided with a gas preheating inlet and a gas preheating outlet, the gas preheating inlet is connected to the charring gas source, and the gas source introduction pipeline of the gas preheating inlet is provided with the pressure regulating valve (4-1) and the gas flow meter (4-2) in sequence along the gas flow direction; The gas distributor (2-6) is provided with a charred gas inlet and distribution holes, and the charred gas inlet is connected to the preheating gas outlet of the gas preheater (4-3); the gas distributor (2-6) extends from the lower part of the shell of the regenerator (2-1) into the regenerator (2-1), and the outlets of the distribution holes of the gas distributor (2-6) are directed toward the bottom of the shell.

20. The system according to claim 19, wherein: The gas distributor (2-6) extends from the bottom of the upper cylindrical shell of the regenerator (2-1) into the regenerator (2-1), and the outlet of the distribution air hole of the gas distributor (2-6) faces the bottom of the lower conical shell of the regenerator (2-1).

21. The system according to claim 1, wherein: The system further comprises an analysis unit; the analysis unit comprises a flue gas sampling device (5-5) and an exhaust gas analyzer (5-4); the regenerator (2-1) further comprises a flue gas filter device (2-3), the flue gas filter device (2-3) being arranged at the upper portion of the housing of the regenerator (2-1); the flue gas inlet of the exhaust gas analyzer (5-4) is connected to the flue gas outlet of the flue gas filter device (2-3); A flue gas collection port is provided on the side wall of the shell of the regenerator (2-1), and the flue gas collection port is connected to the flue gas sampling device (5-5).

22. The system according to claim 21, wherein: A plurality of flue gas collection ports are provided at different heights on the side wall of the shell along the axial direction of the regenerator (2-1).

23. The system according to claim 1, wherein: The system also includes a regenerant recovery unit, which includes a discharge valve (3-1), a discharge bin (3-2), a discharge bin air inlet valve (3-3), a discharge bin back pressure valve (3-4), a pressure sensor (3-5) and a discharge valve (3-6); the discharge bin (3-2) is provided with a regenerant inlet, a discharge outlet, a discharge bin air inlet and a discharge bin gas outlet; the regenerant inlet is connected to the regenerant outlet of the regenerator (2-1); the discharge bin air inlet is provided at the upper part of the discharge bin (3-2), and the discharge bin air inlet valve (3-3) is provided on the connecting pipeline between the discharge bin air inlet and the gas source; The discharge bin gas outlet is arranged at the top of the discharge bin (3-2) and is connected to the external environment through a gas outlet pipeline. The discharge bin back pressure valve (3-4) is provided on the gas pipeline, and the pressure sensor (3-5) is provided between the discharge bin gas outlet and the discharge bin back pressure valve (3-4).

24. A method for simulating and evaluating the regeneration operation of a continuous catalytic cracking reactor, characterized in that: Using the system according to any one of claims 1 to 23; the method comprises the following steps: The spent agent is allowed to enter the regenerator (2-1) through the feed outlet of the spent agent feeding unit; and the charred gas is introduced into the regenerator (2-1) through the charred gas supply unit, and the spent agent is subjected to charred regeneration treatment in the regenerator (2-1) to obtain regenerated flue gas and regenerated agent; Introducing a heat exchange medium into the tube of the variable diameter spiral coil through the heat exchange medium inlet of the heat exchange medium internal component (2-5), so that the heat exchange medium exchanges heat with the material in the regenerator (2-1); The regeneration flue gas is allowed to enter the analysis unit for analysis; and the regeneration agent is allowed to enter the regeneration agent recovery unit for regeneration agent recovery treatment.

25. The method according to claim 24, characterized in that The reaction conditions in the regenerator include: temperature of 500-800°C, pressure of 0-0.5 MPa; temperature of the charred gas of 20-500°C; volume space velocity of the charred gas of 6-50000 h -1 The superficial velocity of the charred gas is 0.01~1.2m / s; the residence time of the spent agent is 1~240min.

26. The method according to claim 25, characterized in that The reaction conditions in the regenerator include: the temperature of the charred gas is 150-300°C; the volume space velocity of the charred gas is 200-3000h -1 The superficial velocity of the charred gas is 0.1~0.6m / s; the residence time of the spent agent is 2~60min.

27. The method according to claim 24, characterized in that The volume content of oxygen in the charred gas composition is 10-40 volume %.

28. The method according to claim 24, characterized in that The spent catalyst is obtained from a catalytic cracking process in a factory or a spent catalyst obtained by carbonization reaction in a pilot plant.

29. The method according to claim 28, characterized in that The spent catalyst has a carbon content of 0.5-3% by weight.

30. The method according to claim 29, wherein The carbon content of the regeneration agent is 0.01-1% by weight.

31. The method according to claim 24, wherein The method further comprises preheating the spent catalyst entering the spent catalyst feeding unit; and then allowing the preheated spent catalyst to enter the regenerator (2-1).

32. The method according to claim 31, characterized in that The temperature of the preheated spent catalyst is 10~550℃.

33. The method according to claim 31, wherein The feeding screw (1-4) in the spent catalyst feeding unit feeds the regenerator (2-1) at a speed of 0.1-20 g / s, and the working pressure of the feeding screw (1-4) in the spent catalyst feeding unit is 0-0.5 MPa.

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