Lift pipe reactor for catalytic cracking reaction and catalytic cracking equipment
By using a ring nozzle assembly in the riser reactor to prevent catalyst backmixing, the problem of excessively long contact time between the catalyst and emulsified oil was solved, achieving a highly efficient catalytic cracking reaction and improving product yield and unit operating efficiency.
Patent Information
- Application Number
- CN202422477227.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-10-12
- Publication Date
- 2025-11-07
- Estimated Expiration
- 2034-10-12
AI Technical Summary
Backmixing of the catalyst occurs in the riser reactor, resulting in excessive contact time between the catalyst and the emulsified oil, leading to over-cracking and coking, which affects product yield and unit operation.
The system employs a ring nozzle assembly, which includes a ring and multiple high-pressure nozzles. The nozzle orifices face the top of the reaction tube, spraying an emulsified oil mixture that drives the catalyst upward, preventing backmixing and improving the reaction rate.
It effectively prevents catalyst backmixing, avoids excessive cracking and coking, improves catalytic cracking reaction rate, reduces steam consumption, simplifies process flow, and improves light oil yield and economic benefits.
Smart Images
Figure CN223517489U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model belongs to the technical field of petroleum chemical industry, concretely relates to a riser reactor for catalytic cracking reaction and catalytic cracking equipment. BACKGROUND
[0002] Catalytic cracking is a very important petroleum processing technology in the field of petroleum chemical industry, and the riser reactor is one of the key equipment of the catalytic cracking device. Generally, the riser reactor can be divided into four parts from bottom to top according to the role of different parts: pre-lifting section, feed mixing section, reaction section and outlet rapid separation section. In the pre-lifting section, the pre-lifting gas enters from the bottom of the riser, mixes with the catalyst particles entering from the regenerated inclined pipe, and then carries the catalyst upward. When moving to the feed mixing section, the catalyst particles mix with the raw oil sprayed by the atomizing nozzle, and then continue to move upward into the reaction section. In the reaction section, the oil and catalyst mixture moves upward and rapidly cracks to generate gasoline, diesel, liquefied gas and other target products. When reaching the outlet rapid separation section at the end of the riser, the diesel, gasoline and other products and catalyst are rapidly separated to prevent excessive cracking.
[0003] In the feed mixing section of the riser device, the catalyst particles are relatively dense and there is a backmixing phenomenon, especially in the riser wall area, which makes the catalyst residence time longer and greatly increases the probability of repeated contact between oil and catalyst. Prolonged contact between oil and catalyst can lead to excessive cracking and coking, thereby affecting the yield of products and the operation of the device. UTILITY MODEL CONTENT
[0004] The utility model aims to provide a riser reactor for catalytic cracking reaction and catalytic cracking equipment to prevent the backmixing phenomenon of catalyst and improve the catalytic cracking reaction rate of emulsified oil.
[0005] In order to achieve the above-mentioned purpose, the utility model provides a riser reactor for catalytic cracking reaction, which comprises:
[0006] A reaction tube, the bottom of which can spray water vapor to the top, and the top of the reaction tube is provided with a material discharge port;
[0007] A catalyst feed pipe, which communicates with the reaction tube and is used for feeding catalyst into the reaction tube;
[0008] An emulsified oil feed pipe, which communicates with the reaction tube and is used for conveying emulsified oil mixture into the reaction tube, and the outlet end of the emulsified oil feed pipe is located above the outlet end of the catalyst feed pipe;
[0009] The annular nozzle assembly is arranged in the outlet end of the emulsified oil feeding pipe and in the lumen of the reaction pipe, and comprises an annular pipe and a plurality of high-pressure nozzles.
[0010] In some embodiments, the plurality of high-pressure nozzles are arranged with their nozzles inclined, and the emulsified oil mixture sprayed from the nozzles of the plurality of high-pressure nozzles is located in the same rotating vortex, and the centers of the nozzles of the plurality of high-pressure nozzles are located on the same circle.
[0011] In some embodiments, the center of the annular pipe coincides with the axis of the reaction pipe, and there is a gap between the outer wall of the annular pipe and the inner wall of the reaction pipe.
[0012] In some embodiments, the outer ring of the annular pipe, the inner ring of the annular pipe and the central axis of the reaction pipe coincide.
[0013] In some embodiments, the annular nozzle assembly further comprises a pressurizing member arranged between the annular pipe and the high-pressure nozzles and used for pressurizing the emulsified oil mixture.
[0014] In some embodiments, the reaction pipe comprises a reaction pipe section, a feed mixing pipe section and a riser section in sequence from top to bottom, the catalyst feeding pipe is in communication with the riser section, the emulsified oil feeding pipe is in communication with the feed mixing pipe section, the annular nozzle assembly is arranged in the feed mixing pipe section, and the pipe diameter of the feed mixing pipe section is greater than that of the reaction pipe section and the riser section.
[0015] In some embodiments, the inner diameter of the reaction pipe section gradually increases in the direction close to the feed mixing pipe section, and the inner diameter of the riser section gradually increases in the direction close to the feed mixing pipe section.
[0016] In some embodiments, the gas pressure at the bottom gas injection port of the reaction pipe is 1.2 MPa±0.2 MPa, and the pressure of the nozzles of the high-pressure nozzles is 0.5 MPa-4.5 MPa.
[0017] The utility model discloses a second aspect provides a kind of catalytic cracking equipment, including above-mentioned for catalytic cracking reaction riser reactor.
[0018] In some embodiments, the catalytic cracking equipment further comprises: a raw material tank storing raw oil; a raw material pump having one end in communication with the raw material tank and configured to deliver the raw oil; and a pretreatment mechanism installed on a pipeline between the raw material pump and the emulsified oil feeding pipe and configured to pretreat the raw oil and obtain the emulsified oil mixture.
[0019] In the technical scheme, the riser reactor comprises a reaction tube, a catalyst feeding tube, an emulsified oil feeding tube and a loop nozzle assembly. The reaction tube is used for catalytic cracking reaction of the emulsified oil in the tube cavity. The catalyst feeding tube is communicated with the reaction tube and used for feeding catalyst into the reaction tube. The emulsified oil feeding tube is used for feeding emulsified oil mixture into the reaction tube. The outlet end of the emulsified oil feeding tube is located above the outlet end of the catalyst. Water vapor is sprayed from the bottom to the top of the reaction tube to transport the catalyst at the bottom to the top to catalyze the emulsified oil to react. The loop nozzle assembly is installed at the outlet end of the emulsified oil feeding tube and located in the tube cavity of the reaction tube. The loop nozzle assembly comprises a loop and a plurality of high-pressure nozzles. The plurality of high-pressure nozzles are installed on the loop and arranged at intervals along the circumference of the loop. The nozzles of the plurality of high-pressure nozzles are arranged towards the top end of the reaction tube. When the emulsified oil mixture is transported to the outlet end of the emulsified oil feeding tube, the emulsified oil mixture passes through the loop and the high-pressure nozzles in sequence and is then sprayed into the reaction tube to mix with the catalyst to perform catalytic cracking reaction. The nozzles spray the emulsified oil mixture and drive the catalyst to move upwards at the same time, which reduces the back mixing of the catalyst, improves the reaction rate of the catalytic cracking and prevents the back mixed catalyst from contacting with the emulsified oil for a long time to cause excessive cracking and coking.
[0020] Other features and advantages of the embodiments of the present application will be described in detail in the following specific embodiments. BRIEF DESCRIPTION OF DRAWINGS
[0021] The accompanying drawings are included to provide a further understanding of the embodiments of the present application, and constitute a part of the specification, and are used to explain the embodiments of the present application together with the following detailed description, but do not limit the embodiments of the present application. For those skilled in the art, other drawings can be obtained from the structures shown in the drawings without creative labor. In the drawings:
[0022] Figure 1 A front view cross-sectional schematic view of the riser reactor for catalytic cracking reaction according to the embodiments of the present application is provided.
[0023] Figure 2 A top view cross-sectional schematic view of the riser reactor for catalytic cracking reaction according to the embodiments of the present application is provided.
[0024] Figure 3 An installation angle schematic view of the high-pressure nozzle according to the embodiments of the present application is provided.
[0025] Figure 4 A partial structure schematic view of the catalytic cracking equipment according to the embodiments of the present application is provided.
[0026] REFERENCE SIGNS
[0027] 10 reaction tube
[0028] 11 Reaction Section
[0029] 12 Feed mixing pipe section
[0030] 13. Uplift pipe section
[0031] 20 Catalyst feed pipe
[0032] 30 Emulsified oil feed pipe
[0033] 40 Ring nozzle assembly
[0034] 41. Ring pipe
[0035] 42 High-pressure nozzle
[0036] 50 Raw material tanks
[0037] 60 Raw material pump
[0038] 70 Pre-processing unit Detailed Implementation
[0039] The specific embodiments of this utility model will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit the scope of this utility model.
[0040] The riser reactor and catalytic cracking equipment for catalytic cracking reactions provided according to embodiments of the present invention are described below with reference to the accompanying drawings. Figure 1 The image shown is a front cross-sectional schematic diagram of a riser reactor for catalytic cracking according to an embodiment of the present invention; as shown... Figure 2 The image shown is a top cross-sectional view of a riser reactor for catalytic cracking according to an embodiment of the present invention. The riser reactor for catalytic cracking includes:
[0041] The reaction tube 10 has a bottom that can spray water vapor to the top, and the top of the reaction tube 10 is provided with a material outlet (not shown in the figure);
[0042] The catalyst feed pipe 20 is connected to the reaction pipe 10 and is used to feed the catalyst into the reaction pipe 10.
[0043] The emulsified oil feed pipe 30 is connected to the reaction pipe 10 and is used to feed the emulsified oil mixture into the reaction pipe 10. The outlet end of the emulsified oil feed pipe 30 is located above the outlet end of the catalyst feed pipe 20.
[0044] The ring pipe nozzle assembly 40 is installed at the outlet end of the emulsified oil feeding pipe 30 and located in the pipe cavity of the reaction pipe 10, and the ring pipe nozzle assembly 40 comprises a ring pipe 41 and a plurality of high-pressure nozzles 42, the ring pipe 41 is arranged along the inner wall of the reaction pipe 10 in the circumferential direction, the plurality of high-pressure nozzles 42 are all installed on the ring pipe 41 and arranged in the circumferential direction of the ring pipe 41, and the spray nozzles of the plurality of high-pressure nozzles 42 are all arranged towards the material discharge port.
[0045] In the process of catalytic cracking of emulsified oil, it is necessary to mix the emulsified oil mixture with the catalyst in a high-temperature environment, and the contact time and contact amount of the emulsified oil mixture and the catalyst have relatively stringent range requirements. When the catalyst is excessive or the contact time of the emulsified oil mixture and the catalyst is too long, it is easy to cause excessive cracking or coking of the emulsified oil, and to cause the reaction rate to decrease due to excessive reaction; when the catalyst is insufficient or the contact time of the emulsified oil mixture and the catalyst is too short, it will cause incomplete cracking reaction and low reaction rate.
[0046] In the embodiment of the utility model, the riser reactor comprises a reaction pipe 10, a catalyst feeding pipe 20, an emulsified oil feeding pipe 30 and a ring pipe nozzle assembly 40. The reaction pipe 10 can accommodate the emulsified oil mixture and the catalyst for reaction, and the reaction pipe 10 can also provide a high-temperature environment suitable for catalytic cracking of emulsified oil. The catalyst feeding pipe 20 is in communication with the reaction pipe 10, and the catalyst can enter the reaction pipe 10 through the catalyst feeding pipe 20 to catalyze the emulsified oil mixture for reaction. The emulsified oil feeding pipe 30 is in communication with the reaction pipe 10, and the emulsified oil mixture can enter the reaction pipe 10 through the emulsified oil feeding pipe 30 for catalytic cracking reaction. The outlet end of the catalyst feeding pipe 20 is located below the outlet end of the emulsified oil feeding pipe 30, in order to make the catalyst fully contact with the emulsified oil mixture, a water vapor outlet (not shown in the figure) for spraying water vapor to the top is arranged at the bottom of the reaction pipe 10, and the water vapor can drive the catalyst to move upward and contact with the emulsified oil mixture. The catalyst and the cracking product are discharged from the material discharge port. The emulsified oil mixture is a mixture obtained by emulsifying and pretreating raw oil, and the emulsified oil mixture comprises emulsified oil and water vapor. The catalyst can be selected as catalase, and of course, other catalysts can be used according to the type of catalytic cracking, which is not limited here.
[0047] The riser reactor provided by the embodiment of the utility model includes a loop nozzle assembly 40, the loop nozzle assembly 40 is installed at the outlet end of the emulsified oil feed pipe 30 and is located in the lumen of the reaction tube 10, the loop nozzle assembly 40 includes a loop 41 and a plurality of high-pressure nozzles 42, the emulsified oil mixture sequentially passes through the emulsified oil feed pipe 30, the loop 41 and the high-pressure nozzles 42 and enters the reaction tube 10, the nozzles of the high-pressure nozzles 42 are all arranged towards the top end of the reaction tube 10, the emulsified oil mixture is forced to be sprayed upwards and drives the catalyst to move upwards together, so that the emulsified oil mixture and the catalyst are fully contacted and reacted, and the top of the reaction tube 10 is discharged after the reaction is completed.
[0048] The riser reactor is adopted, the catalyst and the emulsified oil mixture can be fully contacted, the emulsified oil mixture of high pressure is sprayed upwards through the loop nozzle assembly 40, the catalyst can be driven to move together with the emulsified oil mixture towards the material discharge port, catalyst back mixing in the middle of movement is prevented, when the emulsified oil is contacted with the catalyst for a long time or contacted with excessive catalyst, the phenomenon of excessive cracking and coking is avoided, and the reaction rate of catalytic cracking is effectively improved. In the embodiment of the utility model, the spraying position and the emulsified oil discharge position are the same, compared with the technical scheme that the inner member is additionally increased in the reaction tube 10 to spray water vapor, the structure provided by the embodiment of the utility model has less coking adhesion points and low steam consumption.
[0049] In one embodiment, as shown in Figure 3 The installation angle of the high-pressure nozzle 42 provided by the embodiment of the utility model is shown, wherein the position reference of the coordinate system is Figure 2 The nozzles of the plurality of high-pressure nozzles 42 are all arranged obliquely, the emulsified oil mixture sprayed by the nozzles of the plurality of high-pressure nozzles 42 is located in the same rotating vortex, and the centers of the nozzles of the plurality of high-pressure nozzles 42 are located on the same circumference. The obliquely arranged high-pressure nozzles 42 can make the emulsified oil mixture sprayed by the nozzles located in the same rotating vortex, so that the emulsified oil mixture can drive the catalyst to form a "flat flow" above the loop nozzle assembly 40, in the "flat flow", the catalyst and the emulsified oil mixture move upwards along the inner circumference of the reaction tube 10 at the same speed. The structure of the high-pressure nozzle 42 is adopted, and the catalyst backflow can be further prevented.
[0050] In one specific embodiment, a three-dimensional rectangular coordinate system is established with the connection center of the high-pressure nozzle 42 and the ring pipe 41 as the origin, the tangent direction of the ring pipe 41 as the Y-axis, the direction of the center of the ring pipe 41 toward the center of the ring pipe 41 as the X-axis, and the height direction of the reaction pipe 10 as the Z-axis. The angle between the high-pressure nozzle 42 and the Z-axis is γ, the angle between the horizontal projection of the high-pressure nozzle 42 on the horizontal plane formed by the X-axis and the Y-axis is α, and the angle between the horizontal projection of the high-pressure nozzle 42 and the Y-axis is β. The angle α is in the range of 5° to 15°, the angle β is (90-α) degrees, and the angle γ is in the range of 5° to 30°. The use of the above angle range has the following beneficial effects: the emulsified oil mixture sprayed by the high-pressure nozzle 42 forms an upward rotating flow, the gas flow and catalyst flow in the reaction pipe 10 from the bottom to the top change from straight flow to rotating flow, catalyst backmixing is reduced, the flow in the reaction pipe 10 is uniform and stable, the light oil yield of the riser reactor is improved, the coke yield of the riser reactor is reduced, and the economic benefit of the riser reactor is improved.
[0051] In one specific embodiment, the plurality of high-pressure nozzles 42 are uniformly spaced in the circumferential direction, and the angular interval between any two adjacent high-pressure nozzles 42 is in the range of the central angle 360° / n (n is the number of high-pressure nozzles 42). The use of the above structure is beneficial to ensuring that the fluid sprayed by the high-pressure nozzle 42 is uniform and stable, and forms a rotating gas flow.
[0052] In one embodiment, as shown in Figure 1 the center of the ring of the ring pipe 41 coincides with the pipe axis of the reaction pipe 10, and there is a gap between the outer wall of the ring pipe 41 and the inner wall of the reaction pipe 10. The distance of the gap can be selected within a suitable range according to actual conditions, and cannot be too large or too small. The center of the ring of the ring pipe 41 coincides with the pipe axis of the reaction pipe 10, which can make the emulsified oil mixture sprayed by the high-pressure nozzle 42 be uniformly stressed in all directions, and is more conducive to forming a "flat push flow" above the nozzle to prevent catalyst backmixing. There is a gap between the outer wall of the ring pipe 41 and the inner wall of the reaction pipe 10, and the catalyst flows from the gap or the center of the ring pipe 41 to the upper part of the ring pipe 41 during the upward flow from the lower part of the ring pipe 41, which prevents the installation ring from forming a card slot that blocks the upward flow of the catalyst, effectively improving the utilization rate of the catalyst and the reaction rate of the catalytic cracking reaction.
[0053] In one embodiment, as shown in Figure 2As shown, the outer ring of the ring pipe 41, the inner ring of the ring pipe 41 and the central axis of the reaction pipe 10 coincide. With the above structure, the spacing between the outer peripheral wall of the ring pipe 41 and the inner peripheral wall of the reaction pipe 10 is equal everywhere, and the catalyst is uniformly mixed with the emulsified oil mixture during the upward flow of the catalyst, the catalytic cracking reaction is highly consistent, and the product quality at the material outlet is higher.
[0054] In one embodiment, the ring pipe nozzle assembly 40 further comprises a pressurizing member (not shown in the figure) installed between the ring pipe 41 and the high-pressure nozzle 42 for pressurizing the emulsified oil mixture. The pressurizing member is arranged in the ring pipe nozzle assembly 40, which can pressurize the emulsified oil mixture, and the pressurized emulsified oil mixture is sprayed from the nozzle of the high-pressure nozzle 42, which can make the emulsified oil mixture move upward with a larger initial speed, so as to prevent the catalyst from moving downward due to gravity and causing back mixing phenomenon, which affects the reaction.
[0055] In one embodiment, as shown, Figure 1 The reaction pipe 10 comprises a reaction pipe section 11, a feed mixing pipe section 12 and a lift pipe section 13 connected in sequence from top to bottom, the emulsified oil feed pipe 30 is connected to the feed mixing pipe section 12, the ring pipe nozzle assembly 40 is located in the feed mixing pipe section 12, the catalyst feed pipe 20 is connected to the lift pipe section 13, and the pipe diameter of the feed mixing pipe section 12 is larger than that of the reaction pipe section 11 and the lift pipe section 13. The reaction pipe 10 comprises a reaction pipe section 11, a feed mixing pipe section 12 and a lift pipe section 13 connected in sequence from top to bottom, the ring pipe nozzle assembly 40 is installed in the feed mixing pipe section 12, which occupies a large volume in the feed mixing pipe section 12. Therefore, in order to keep the fluid velocity in the reaction pipe 10 relatively stable, the inner diameter of the feed mixing pipe section 12 is larger than that of the reaction pipe section 11 and the lift pipe section 13, so that a more stable "plug flow" can be formed above the ring pipe nozzle assembly 40, which helps to optimize the reaction process, improve the reaction rate and fully utilize the catalyst and the emulsified oil mixture.
[0056] In one embodiment, the reaction pipe 10 further comprises a discharge pipe section (not shown in the figure) at the top end of the reaction pipe 10 and an air inlet pipe section (not shown in the figure) at the bottom end of the reaction pipe 10, the inner diameter of the reaction pipe section 11 gradually increases along the direction close to the feed mixing pipe section 12, and the inner diameter of the lift pipe section 13 gradually increases along the direction close to the feed mixing pipe section 12. The inner diameters of the reaction pipe section 11 and the lift pipe section 13 are not fixed values, the inner diameter of the reaction pipe section 11 gradually increases along the direction close to the feed mixing pipe section 12, and the inner diameter of the lift pipe section 13 gradually increases along the direction close to the feed mixing pipe section 12. With the structure of gradually increasing inner diameters, it can prevent the local fluid velocity from suddenly changing and causing the formation of turbulent flow in the reaction pipe 10, which affects the "plug flow" movement above the ring pipe nozzle assembly 40.
[0057] In one embodiment, the reaction tube 10 further comprises a gas inlet pipe section (not shown in the figure) at the bottom of the reaction tube 10 and a material outlet pipe section (not shown in the figure) at the top end of the reaction tube 10, wherein the inner diameter of the gas inlet pipe section and the inner diameter of the material outlet pipe section are fixed values. The water vapor outlet is arranged at the bottom of the gas inlet pipe section, and the material outlet is arranged at the top of the material outlet pipe section.
[0058] In one specific embodiment, the inner diameters of the gas inlet pipe section and the material outlet pipe section are A, the inner diameter of the ring pipe 41 is B, the outer diameter of the ring pipe 41 is C, and the diameter of the feed mixing pipe section 12 is D, and A, B, C and D satisfy the following relationship S D -S C +S B =(0.8-1)*S A With such a structure, the following beneficial effects are achieved: the gas flow and the catalyst flow are accelerated and preliminarily guided at the ring pipe 41, and after the emulsified oil mixture is sprayed by the high-pressure nozzle 42, the gas flow and the catalyst flow are further guided to rotate upward, so that the catalyst flow is uniform and stable, catalyst backmixing is prevented, and the flow is closer to "plug flow" movement.
[0059] In one embodiment, the gas pressure at the gas injection port of the bottom of the reaction tube 10 is 1.2 MPa±0.2 MPa, and the jet pressure of the high-pressure nozzle 42 is 0.5 MPa-4.5 MPa. With the above-mentioned gas pressure range, the pressure at the bottom of the reaction tube 10 is relatively low, and (1.2 MPa±0.2 MPa) of steam can meet the requirements. The high-pressure nozzle 42 uses a pressure of 0.5 MPa-4.5 MPa to achieve high-efficiency atomization by adjusting the pressure of the catalytic emulsified oil mixture, without the need for additional atomizing steam, which is energy-efficient and simplifies the process flow.
[0060] In one embodiment, a catalytic cracking device is provided, which comprises the riser reactor for catalytic cracking reaction described above. As shown in Figure 4 Fig. 2 is a partial structure schematic view of the catalytic cracking device according to an embodiment of the present application.
[0061] In one embodiment, the catalytic cracking device further comprises: a raw material tank 50 storing raw oil; a raw material pump 60, one end of the raw material pump 60 being communicated with the raw material tank 50 and being used for conveying the raw oil; and a pretreatment mechanism 70 installed on a pipeline between the raw material pump 60 and the emulsified oil feeding pipe 30 and used for pretreating the raw oil and obtaining the emulsified oil mixture. Before the raw oil is subjected to catalytic cracking, a series of pretreatment processes need to be performed to obtain the emulsified oil mixture. In the embodiment of the utility model, the catalytic cracking device further comprises the raw material tank 50, the raw material pump 60 and the pretreatment mechanism 70, and the pretreatment mechanism 70 can pretreat the raw material input by the raw material pump 60 to obtain the emulsified oil mixture. By using the catalytic cracking device, the raw oil can be more smoothly pretreated to obtain the emulsified oil mixture, and the cost is low and the production efficiency is high.
[0062] In one specific embodiment, the pretreatment mechanism 70 comprises a pre-dispersion pipe and a polarity adjustment pretreatment assembly.
[0063] In the description of the utility model, it is to be understood that the terms "first", "second" are only for the purpose of description, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features limited by "first", "second" can explicitly or implicitly include at least one of the features. In the description of the utility model, the meaning of "a plurality of" is at least two, for example, two, three, etc., unless otherwise specifically limited.
[0064] In the utility model, unless otherwise specifically defined and limited, the terms "installation", "connection", "connection", "fixing" and other terms should be understood in a broad sense, for example, can be fixedly connected, or can be detachably connected, or integrated; can be mechanically connected, or electrically connected or can communicate with each other; can be directly connected, or indirectly connected through an intermediate medium, can be the internal communication of two elements or the interaction relationship of two elements, unless otherwise specifically limited. For ordinary skilled in the art, the specific meaning of the above terms in the utility model can be understood according to the specific circumstances.
[0065] In the description of the present specification, the description referring to the terms "one embodiment", "some embodiments", "an example", "a specific example", or "some examples" and the like means that the specific features, structures, materials or characteristics described in connection with the embodiment or example are included in at least one embodiment or example of the present application. In the present specification, the illustrative description of the above terms does not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any appropriate manner in any one or more embodiments or examples. Furthermore, the person skilled in the art can combine and combine the different embodiments or examples described in the present specification and the features of the different embodiments or examples, without contradiction.
[0066] Although the embodiments of the present application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present application, and the person skilled in the art can make changes, modifications, replacements and modifications to the above embodiments within the scope of the present application.
Claims
1. A riser reactor for catalytic cracking reactions, characterized in that, The riser reactor comprises: a reaction tube (10) capable of ejecting steam from bottom to top, the top of the reaction tube (10) being provided with a material outlet; a catalyst feeding tube (20) communicating with the reaction tube (10) and used for feeding catalyst into the reaction tube (10); an emulsified oil feeding tube (30) communicating with the reaction tube (10) and used for feeding an emulsified oil mixture into the reaction tube (10), the outlet end of the emulsified oil feeding tube (30) being located above the outlet end of the catalyst feeding tube (20); a ring tube nozzle assembly (40) installed at the outlet end of the emulsified oil feeding tube (30) and located in the lumen of the reaction tube (10), the ring tube nozzle assembly (40) comprising a ring tube (41) and a plurality of high-pressure nozzles (42), the ring tube (41) being arranged circumferentially along the inner wall of the reaction tube (10), the plurality of high-pressure nozzles (42) being each installed on the ring tube (41) and arranged circumferentially at intervals along the ring tube (41), the spray nozzles of the plurality of high-pressure nozzles (42) being each arranged towards the material outlet.
2. The riser reactor for catalytic cracking reaction according to claim 1, characterized by, The spray nozzles of the plurality of high-pressure nozzles (42) are each arranged obliquely, the emulsified oil mixture sprayed from the spray nozzles of the plurality of high-pressure nozzles (42) being located in the same rotating vortex, the centers of the spray nozzles of the plurality of high-pressure nozzles (42) being located on the same circumference.
3. The riser reactor for catalytic cracking reaction according to claim 1, characterized by, The center of the ring of the ring tube (41) coincides with the axis of the reaction tube (10), and there is a gap between the outer tube wall of the ring tube (41) and the inner tube wall of the reaction tube (10).
4. The riser reactor for catalytic cracking reaction according to claim 3, characterized by, The outer ring of the ring tube (41), the inner ring of the ring tube (41) and the central axis of the reaction tube (10) coincide.
5. The riser reactor for catalytic cracking reaction according to claim 1, characterized by, The ring tube nozzle assembly (40) further comprises: a pressurizing member installed between the ring tube (41) and the high-pressure nozzles (42) and used for pressurizing the emulsified oil mixture.
6. The riser reactor for catalytic cracking reaction according to claim 1, characterized by The reaction tube (10) comprises a reaction tube section (11), a feeding mixing tube section (12) and a riser section (13) sequentially communicating from top to bottom, the catalyst feeding tube (20) communicating with the riser section (13), the emulsified oil feeding tube (30) communicating with the feeding mixing tube section (12), the ring tube nozzle assembly (40) being located in the feeding mixing tube section (12), and the tube diameter of the feeding mixing tube section (12) being greater than the tube diameters of the reaction tube section (11) and the riser section (13).
7. The riser reactor for catalytic cracking reactions according to claim 6, characterized in that, The inner diameter of the reaction tube section (11) gradually increases along the direction close to the feeding mixing tube section (12), and the inner diameter of the riser section (13) gradually increases along the direction close to the feeding mixing tube section (12).
8. The riser reactor for catalytic cracking reactions according to claim 1, characterized in that, The gas pressure at the gas ejection port of the bottom of the reaction tube (10) is 1.2 MPa±0.2 MPa, and the pressure of the spray nozzles of the high-pressure nozzles (42) is 0.5 MPa-4.5 MPa.
9. A catalytic cracking unit, characterized by The riser reactor for catalytic cracking reaction according to any one of claims 1-8 is provided.
10. Catalytic cracking apparatus according to claim 9, characterised in that The catalytic cracking device further comprises: a raw material tank (50) storing raw oil; A raw material pump (60) having one end communicated with the raw material tank (50) and used for delivering the raw material oil; A pretreatment mechanism (70) installed on a pipeline between the raw material pump (60) and the emulsified oil feed pipe (30) and used for pretreating the raw material oil and obtaining an emulsified oil mixture.