Catalytic cracking system and method
By setting a contact mixing space in the feed pipe of the catalytic cracking system, the raw materials and high-temperature catalyst are fully mixed before entering the bed reactor, the problems of rising yields of dry gas, diesel, coke and light oil yields in the existing system are solved, and better product distribution and full vaporization of raw materials are achieved.
Patent Information
- Application Number
- CN202311666126.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2023-12-06
- Publication Date
- 2025-06-06
AI Technical Summary
In the existing catalytic cracking system, the yields of dry gas, diesel and coke have increased, and the yields of target products such as light oils have decreased.
A catalytic cracking system is designed, by providing a first feed port on the side wall of the feed tube, allowing the raw material to contact and mix with the high-temperature catalyst before entering the bed reactor, ensuring that the contact time is within 0.1-0.6 s, thereby achieving sufficient vaporization of the raw material.
By fully vaporizing the raw materials, some raw materials are avoided from entering the reactor in liquid phase or incomplete vaporization state, reducing the generation of by-products and poor product distribution, and improving the yield of the target product and the quality of product distribution.
Smart Images
Figure CN120098668A_ABST
Abstract
Description
Technical Field
[0001] The present invention relates to the technical field of petrochemical industry, and in particular to a catalytic cracking system and method. Background Art
[0002] Catalytic cracking is one of the petroleum refining processes. It is a process in which heavy oil undergoes cracking reaction under the action of heat and catalyst to convert it into cracked gas, gasoline and diesel.
[0003] In an existing type of catalytic cracking system, a raw material nozzle is provided at the bottom of the reactor or below the bottom distributor. The raw material is sprayed into the raw material nozzle after being atomized by steam, mixed with a high-temperature catalyst, and then enters the reactor for cracking reaction to obtain reaction oil gas and catalyst to be regenerated. The reaction oil gas and the catalyst to be regenerated are separated by a cyclone separator at the reactor outlet. The separated catalyst to be regenerated enters a settler and enters a regenerator for regeneration after steam stripping. After the reaction oil gas is separated, dry gas, liquefied gas, cracked gasoline, cracked diesel, and cracked heavy oil can be obtained. However, the inventor of the present application has found that the existing catalytic cracking system often has the problem of increased yields of dry gas, diesel, and coke, and decreased yields of target products such as light oil. Summary of the invention
[0004] The purpose of the present invention is to overcome the problem that the yield of dry gas, diesel and coke often increases while the yield of target products decreases in existing catalytic cracking systems, and to provide a catalytic cracking system and method. The catalytic cracking system can fully vaporize high-boiling point components such as heavy oil in the feedstock, so that the high-boiling point components such as heavy oil can better undergo catalytic cracking reactions in the reactor, thereby obtaining better product distribution.
[0005] In order to achieve the above-mentioned purpose, the first aspect of the present invention provides a catalytic cracking system, including a bed reactor and a feed pipe connected to the bottom of the bed reactor, the feed pipe is used to feed a high-temperature catalyst capable of causing a raw material to undergo a catalytic cracking reaction into the bed reactor, a first feed port is provided on the side wall of the feed pipe for feeding the raw material into the tube cavity of the feed pipe, and the first feed port is spaced apart from the bed reactor.
[0006] Optionally, the distance between the first feed port and the bed reactor is set to enable the raw material and the high-temperature catalyst to contact and mix for 0.1-0.6 seconds before entering the bed reactor.
[0007] Optionally, the catalytic cracking system further comprises a separation device and a regenerator, wherein the separation device is used to separate the reaction oil gas generated by the bed reactor from the catalyst to be regenerated, and the regenerator is used to char and regenerate the catalyst to be regenerated;
[0008] A second feed port is provided on the side wall of the feed pipe, and the first feed port and the second feed port are arranged in sequence on the side wall of the feed pipe in a direction away from the bed reactor, and the regenerator is connected to the second feed port for feeding the regenerated catalyst obtained by charring and regenerating the regenerator into the feed pipe.
[0009] Optionally, a nozzle is provided at the first feed port for spraying the raw material into the feed pipe.
[0010] Optionally, a side pipeline is connected to the bed reactor for adding catalyst to the bed reactor.
[0011] A second aspect of the present invention provides a catalytic cracking method, the catalytic cracking method comprising:
[0012] The raw material and the high temperature catalyst for catalyzing the raw material to undergo catalytic cracking reaction are contacted and mixed in advance, and then sent into the bed reactor to undergo the catalytic cracking reaction.
[0013] Optionally, the feedstock and the high-temperature catalyst are contacted and mixed for 0.1-0.6 seconds before entering the bed reactor.
[0014] Optionally, the catalytic cracking method also includes: using a separation device to separate the reaction oil and gas generated by the catalytic cracking reaction and the catalyst to be regenerated, using a regenerator to char and regenerate the catalyst to be regenerated to obtain a regenerated catalyst, and then using the regenerated catalyst as the high-temperature catalyst to contact and mix with the raw material for 0.1-0.6s, and then sending it into the bed reactor again to carry out the catalytic cracking reaction.
[0015] Optionally, the catalytic cracking method further comprises: adding catalyst to the bed reactor.
[0016] Optionally, the amount of catalyst added to the bed reactor accounts for 5-30 weight % of the catalyst circulation amount in the bed reactor.
[0017] According to the technical solution provided by the present invention, by setting the first feed port and the bed reactor at a distance, a certain contact and mixing space is provided for the high-temperature catalyst and the raw material before entering the bed reactor. On the one hand, it can promote the high-temperature catalyst and the raw material to be fully mixed, and on the other hand, it can meet the contact time between the raw material and the high-temperature catalyst to achieve sufficient vaporization of the raw material, effectively avoiding the problem that part of the raw material enters the bed reactor in a liquid phase or in an incompletely vaporized state, and the by-products increase and the product distribution deteriorate due to the prolonged vaporization time.
[0018] The catalytic cracking system provided by the present invention ensures that the raw materials to be cracked enter the bed reactor in a full gas phase state, which not only makes fuller use of the functions of the bed reactor, but also solves the problem of target product distribution. At the same time, it can better adapt to the raw material composition of different refineries and has good applicability. BRIEF DESCRIPTION OF THE DRAWINGS
[0019] Figure 1 It is a schematic diagram of a catalytic cracking system provided by the present invention.
[0020] Description of Reference Numerals
[0021] 10. Bed reactor; 11. Side pipeline; 20. Feed pipe; 21. First feed inlet; 22. Second feed inlet; 30. Separation device; 40. Regenerator. DETAILED DESCRIPTION
[0022] The specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.
[0023] The catalytic cracking reaction of hydrocarbons takes place on the surface of the catalyst. Under general cracking conditions, catalytic cracking can be considered a gas-solid heterogeneous catalytic reaction, which includes seven main steps: (1) the raw material molecules diffuse from the main gas flow to the catalyst surface; (2) the raw material molecules diffuse along the catalyst micropores to the inside of the catalyst; (3) the raw material molecules are adsorbed by the inner surface of the catalyst; (4) the adsorbed raw material molecules undergo a chemical reaction on the inner surface of the catalyst; (5) the product molecules desorb from the inner surface of the catalyst; (6) the product molecules diffuse outward along the catalyst micropores; (7) the product molecules diffuse into the main gas flow. The speed of the entire catalytic cracking depends on the speed of the above seven steps, and the slowest step plays a decisive role in the overall reaction speed and thus becomes the controlling factor.
[0024] The inventors of the present application have found that in the existing catalytic cracking system, as the proportion of high-boiling-point components such as hydrogenated heavy oil in the raw material gradually increases, the yield of dry gas, diesel, and coke increases, and the yield of target products such as light oil decreases. Furthermore, the inventors have found that due to the high proportion of high-boiling-point components such as hydrogenated heavy oil in the raw material, the raw material vaporization is not sufficient, and some raw materials enter the reactor in liquid phase or incompletely vaporized state, and some raw materials need to continue to vaporize in the reactor. The long vaporization time leads to rapid development of thermal cracking reaction and increase of by-products. At the same time, the reactor space velocity is low, the residence time is long, the yield of coke and dry gas increases, and the product distribution becomes worse.
[0025] Based on this, the first aspect of the present invention provides a catalytic cracking system, which includes a bed reactor 10 and a feed pipe 20 connected to the bottom of the bed reactor 10, the feed pipe 20 is used to feed a high-temperature catalyst that can cause the raw material to undergo catalytic cracking reaction into the bed reactor 10, and a first feed port 21 is provided on the side wall of the feed pipe 20 for feeding the raw material into the tube cavity of the feed pipe 20, and the first feed port 21 is spaced apart from the bed reactor 10.
[0026] In the technical solution provided by the present invention, by setting the first feed port 21 and the bed reactor 10 at a distance, a certain contact and mixing space is provided for the high-temperature catalyst and the raw material before entering the bed reactor 10. On the one hand, it can promote the high-temperature catalyst and the raw material to be fully mixed, and on the other hand, it can meet the contact time between the raw material and the high-temperature catalyst to achieve sufficient vaporization of the raw material, effectively avoiding the problem that part of the raw material enters the bed reactor 10 in the liquid phase or in an incompletely vaporized state, and the by-products increase and the product distribution deteriorate due to the prolonged vaporization time.
[0027] It should be noted that, in the present invention, the “full vaporization” means that all components in the raw material have been vaporized. More precisely, the raw material has been completely vaporized before entering the bed reactor 10, rather than the traditional partial liquid phase raw material that is vaporized only after entering the bed reactor 10.
[0028] Based on the catalytic cracking system provided by the present invention, since the high-temperature catalyst and the raw material to be cracked are fully mixed before entering the bed reactor 10, the high-boiling point components such as hydrogenated heavy oil in the raw material can be better cracked in the bed reactor 10, thereby enhancing the cracking reaction effect and obtaining a better target product distribution; in addition, since the catalytic cracking system provided by the present invention realizes the full vaporization of the raw material to be cracked, the raw material to be cracked enters the bed reactor 10 in a full gas phase state, so that a higher space velocity is formed in the bed reactor 10, and the goals of short-time high-temperature vaporization and high space velocity bed reaction are achieved. It has been proved in practice that based on the catalytic cracking system provided by the present invention, the residence time of the high-temperature catalyst and the raw material in the bed reactor 10 is 2-6s; compared with the design idea of vaporizing part of the liquid phase raw material at the bottom of the bed reactor 10 in the traditional scheme, the catalytic cracking system provided by the present invention can make the raw material enter the bed reactor 10 in a full gas phase state, which not only makes the function of the bed reactor 10 more fully utilized, but also solves the problem of target product distribution, and can better adapt to the raw material composition of different refineries, and has good applicability.
[0029] In the present invention, the feed pipe 20 is used to feed the reaction material into the bed reactor 10, more precisely, to feed the raw material and the high-temperature catalyst capable of catalytic cracking reaction of the raw material into the bed reactor 10 at the same time. In a specific embodiment of the invention, one end of the feed pipe 20 is set as an open end for connecting to the feed port of the bed reactor 10, and the other end of the feed pipe 20 is set as a closed end. A corresponding feed port is set on the side wall of the feed pipe 20 for feeding the raw material and the high-temperature catalyst into the tube cavity of the feed pipe 20.
[0030] It should be noted that, in the present invention, the raw material entering the feed pipe 20 through the first feed port 21 is contacted and mixed with the high-temperature catalyst in the feed pipe 20, and the raw material obtains the heat of the high-temperature catalyst to achieve vaporization, so the contact and mixing time of the raw material and the high-temperature catalyst determines the vaporization degree of the raw material before entering the bed reactor 10. In order to ensure that the raw material is fully vaporized before entering the bed reactor 10, the distance between the first feed port 21 and the bed reactor 10 is set to enable the raw material and the high-temperature catalyst to contact and mix for 0.1-0.6s before entering the bed reactor 10.
[0031] It can be understood that the contact and mixing time of the raw material and the high-temperature catalyst before entering the bed reactor 10 depends on the feed rate of the two. If the feed rate of the raw material and the high-temperature catalyst is increased, the distance between the first feed port 21 and the bed reactor 10 needs to be increased accordingly to meet the contact and mixing time of the raw material and the high-temperature catalyst.
[0032] In some embodiments, the catalytic cracking system also includes a separation device 30 and a regenerator 40, wherein the separation device 30 is used to separate the reaction oil gas and the catalyst to be regenerated generated by the bed reactor 10, and the regenerator 40 is used to burn and regenerate the catalyst to be regenerated; a second feed port 22 is provided on the side wall of the feed pipe 20, and the first feed port 21 and the second feed port 22 are arranged in sequence on the side wall of the feed pipe 20 in a direction away from the bed reactor 10, and the regenerator 40 is connected to the second feed port 22 for feeding the regenerated catalyst obtained by burning and regenerating the regenerator 40 into the feed pipe 20.
[0033] In the present invention, the vaporized raw material is uniformly mixed with the high-temperature catalyst and enters the bed reactor 10. The raw material undergoes a catalytic cracking reaction under the catalytic action of the high-temperature catalyst to form reaction oil gas and the catalyst to be regenerated. The reaction oil gas and the catalyst to be regenerated are separated by means of a separation device 30. The regenerator 40 is further used to char and regenerate the catalyst to be regenerated. The regenerated catalyst obtained by sintering and regenerating can be transported back to the feed pipe 20 through a pipeline for reuse.
[0034] In the present invention, the separation device 30 can adopt any appropriate structure, as long as it can separate the reaction oil gas from the catalyst to be produced. In a specific embodiment of the present invention, the separation device 30 is a cyclone separator. In addition, the method of further separating the reaction oil gas to obtain dry gas, liquefied gas, pyrolysis gasoline, pyrolysis diesel and pyrolysis heavy oil is also well known to those skilled in the art. The dry gas and liquefied gas can be further separated by conventional separation means in the art to obtain target products such as ethylene and propylene. The present invention will not be described in detail here.
[0035] In the present invention, the method of sintering and regenerating the regenerated catalyst using the regenerator 40 can be well known to those skilled in the art. For example, oxygen-containing gas such as air can be introduced into the regenerator 40 to contact the regenerated catalyst. After the flue gas obtained by charring and regeneration is separated from the regenerated catalyst in the regenerator 40, it can be sent to a subsequent energy recovery system for recycling.
[0036] It can be understood that the first feed port 21 and the second feed port 22 are arranged in sequence on the side wall of the feed pipe 20 in a direction away from the bed reactor 10, so that the regenerated catalyst entering through the second feed port 22 has a certain rectification space, and then fully contacts with the raw material entering through the first feed port 21, transfers heat to the raw material, and fully vaporizes it.
[0037] In some embodiments, a nozzle is provided at the first feed port 21 for spraying the raw material into the feed pipe 20. By providing the nozzle, the raw material is sprayed into the tube cavity of the feed pipe 20 to contact and mix with the high-temperature catalyst, which is beneficial to the contact and mixing effect of the raw material and the high-temperature catalyst.
[0038] In some embodiments, a side pipeline 11 is connected to the bed reactor 10 for adding catalyst to the bed reactor 10 .
[0039] It should be noted that in the catalytic cracking system provided by the present invention, by adding catalyst to the bed reactor 10, the catalyst-oil ratio can be adjusted within a larger range, providing more active centers for the catalytic cracking reaction, while increasing the flexibility of adjusting the reaction temperature, and effectively adjusting the gradient of the temperature and catalyst activity in the bed reactor 10; moreover, by adding catalyst to the bed reactor 10, the density uniformity of the catalyst in the bed reactor 10 can be maintained as much as possible, and the effective adjustment of the catalyst density distribution can be achieved, ensuring that the catalytic cracking reaction is fully and effectively carried out, and improving the selectivity of the target product. Preferably, the distance between the connection position of the side pipeline 11 on the bed reactor 10 and the bottom of the bed reactor 10 is 1 / 4 to 2 / 3 of the total height of the bed reactor 10.
[0040] The second aspect of the present invention provides a catalytic cracking method, which comprises: pre-contacting and mixing a raw material and a high-temperature catalyst for catalyzing the raw material to undergo a catalytic cracking reaction, and then feeding the mixture into a bed reactor 10 for the catalytic cracking reaction.
[0041] According to the catalytic cracking method provided by the present invention, the raw materials are fully vaporized during the process of contacting and mixing with the high-temperature catalyst, which effectively avoids the problem that part of the raw materials enter the bed reactor 10 in a liquid phase or in an incompletely vaporized state, and the increase of by-products and the deterioration of product distribution due to the prolonged vaporization time are caused.
[0042] In some embodiments, the feedstock and the high temperature catalyst are contacted and mixed for 0.1-0.6 seconds before entering the bed reactor 10 .
[0043] In some embodiments, the catalytic cracking method further includes: using a separation device 30 to separate the reaction oil gas and the catalyst to be regenerated generated by the catalytic cracking reaction, using a regenerator 40 to burn and regenerate the catalyst to be regenerated to obtain a regenerated catalyst, and then contacting and mixing the regenerated catalyst with the raw material as the high-temperature catalyst for 0.1-0.6s, and then sending it into the bed reactor 10 again to carry out the catalytic cracking reaction.
[0044] According to the catalytic cracking method provided by the present invention, the cost of raw material use is reduced by regenerating the catalyst to be spent in the bed reactor 10 and contacting and mixing it with the raw material as a high-temperature catalyst, and then sending it into the bed reactor 10 to catalyze the raw material again to carry out catalytic cracking reaction.
[0045] It should be noted that the temperature of the regenerated catalyst obtained by charring regeneration in the regenerator 40 is relatively high, and can generally be lowered to a suitable temperature by a cooler. For example, the temperature of the regenerated catalyst can be lowered to 690-760°C by a cooler, and the raw material can be fully vaporized after contact and mixing with the raw material.
[0046] In some embodiments, the weight ratio of the feedstock to the high temperature catalyst is 10-20:1.
[0047] In some embodiments, the catalytic cracking method further includes: adding catalyst to the bed reactor 10 .
[0048] According to the catalytic cracking method provided by the present invention, by adding catalyst to the bed reactor 10, the catalyst-oil ratio can be adjusted within a larger range, providing more active centers for the catalytic cracking reaction, while increasing the flexibility of the reaction temperature adjustment, and effectively adjusting the temperature and catalyst activity gradient in the bed reactor 10; moreover, by adding catalyst to the bed reactor 10, the density uniformity of the catalyst in the bed reactor 10 can be maintained as much as possible, and the effective adjustment of the catalyst density distribution can be achieved, ensuring that the catalytic cracking reaction is fully and effectively carried out, and improving the selectivity of the target product. Preferably, the carbon content in the added catalyst is 0-1% by weight.
[0049] In some embodiments, the amount of catalyst added to the bed reactor 10 accounts for 5-30% by weight of the catalyst circulation amount in the bed reactor 10. By controlling the amount of added catalyst within the above range, the ability to adjust the gradient of temperature and catalyst activity in the bed reactor 10 is ensured, and the catalytic cracking reaction in the bed reactor 10 is ensured to be fully and effectively carried out.
[0050] The catalytic cracking system and method provided by the present invention are further described below through specific examples.
[0051] Example 1
[0052] The present embodiment provides a catalytic cracking system, comprising a bed reactor 10 and a feed pipe 20 connected to the bottom of the bed reactor 10, the feed pipe 20 is used to feed a high-temperature catalyst capable of causing a raw material to undergo a catalytic cracking reaction into the bed reactor 10, the feed pipe 20 is provided with a first feed port 21 for feeding the raw material into the tube cavity of the feed pipe 20, the first feed port 21 is spaced apart from the bed reactor 10 so that the raw material enters the bed reactor 10 after being in contact with the high-temperature catalyst for 0.4 seconds.
[0053] The high-temperature catalyst is a commercial catalytic cracking catalyst with a trade name of DMMC-2; the raw material is a mixture of 50% by weight of hydrogenated heavy oil and 50% by weight of hydrogenated wax oil.
[0054] Specific:
[0055]
[0056]
[0057] In this embodiment, the conditions of the catalytic cracking reaction are: reaction temperature (outlet temperature) is 575° C., reaction pressure is 120 kPa, steam injection ratio is 20%, and the weight ratio of raw material to high-temperature catalyst is 11:1.
[0058] Based on the reaction oil and gas obtained in this example, the proportion of each component is summarized in Table 1.
[0059] Comparative Example 1
[0060] The raw materials and high-temperature catalyst used in the catalytic cracking reaction of this comparative example are the same as those of Example 1, except that the raw materials are directly transported to the bed reactor 10 through the raw material transport pipe, that is, the raw materials are in contact with the high-temperature catalyst for 0 seconds before entering the bed reactor 10.
[0061] Based on the reaction oil and gas obtained in this comparative example, the proportion of each component is summarized in Table 1.
[0062] Example 2
[0063] This embodiment is basically the same as the embodiment 1, except that the first feed port 21 is spaced apart from the bed reactor 10 so that the raw material enters the bed reactor 10 after being in contact with the high-temperature catalyst for 0.1 second.
[0064] Based on the reaction oil and gas obtained in this example, the proportion of each component is summarized in Table 1.
[0065] Example 3
[0066] This embodiment is basically the same as the embodiment 1, except that the first feed port 21 is spaced apart from the bed reactor 10 so that the raw material enters the bed reactor 10 after being in contact with the high-temperature catalyst for 0.6 seconds.
[0067] Based on the reaction oil and gas obtained in this example, the proportion of each component is summarized in Table 1.
[0068] Comparative Example 2
[0069] This comparative example is basically the same as Example 1, except that the first feed inlet 21 is spaced apart from the bed reactor 10 so that the raw material enters the bed reactor 10 after being in contact with the high-temperature catalyst for 0.7 seconds.
[0070] Based on the reaction oil and gas obtained in this comparative example, the proportion of each component is summarized in Table 1.
[0071] Example 4
[0072] This example is basically the same as Example 1, except that the raw material used in this example is a mixture of 36 wt % hydrogenated heavy oil and 64 wt % hydrogenated wax oil.
[0073] Specifically:
[0074]
[0075]
[0076] Based on the reaction oil and gas obtained in this example, the proportion of each component is summarized in Table 1.
[0077] Example 5
[0078] This example is basically the same as Example 1, except that the raw material used in this example is a mixture of 40 wt % hydrogenated heavy oil, 20 wt % hydrogenated wax oil and 40 wt % hydrogenated wax oil.
[0079] Specific:
[0080]
[0081]
[0082] Based on the reaction oil and gas obtained in this example, the proportion of each component is summarized in Table 1.
[0083] Table 1: Proportions of various components in the reaction oil and gas obtained in various embodiments and comparative examples
[0084]
[0085] In Table 1, dry gas refers to C1 and C2, that is, dry gas contains ethylene; liquefied petroleum gas contains propylene.
[0086] Based on the data of Example 1 and Comparative Example 1, it can be seen that the catalytic cracking system provided by the present invention can increase the liquefied gas yield (increased by 0.17%) and gasoline yield (increased by 1.46%), and reduce the dry gas yield (reduced by 0.05%), diesel yield (reduced by 1.47%) and coke yield (reduced by 0.05%).
[0087] Combining the data of Comparative Example 1, Example 2 and Example 3, it can be seen that when the raw material is in contact with the high-temperature catalyst for a certain period of time before entering the bed reactor 10, the change in the liquefied gas yield is not obvious, while the gasoline yield is still significantly improved, by 0.56% and 0.39% respectively; the diesel yield is reduced, by 0.37% and 0.45% respectively.
[0088] Combining the data of Example 1 and Comparative Example 2, it can be seen that when the contact time between the raw material and the high-temperature catalyst before entering the bed reactor 10 is extended from 0.4s to 0.7s, the dry gas yield increases by 0.11%, the liquefied gas yield decreases by 0.20%, the gasoline yield decreases by 1.09%, the diesel yield increases by 1.02%, and the coke yield decreases by 0.24%; therefore, the contact time between the raw material and the high-temperature catalyst before entering the bed reactor 10 is too long, which is not conducive to the light oil yield.
[0089] It can be seen from the data of Examples 1, 4 and 5 that the catalytic cracking system provided by the present invention can obtain liquefied gas and gasoline at a relatively high yield when facing different proportions of hydrogenated heavy oil.
[0090] The catalytic cracking system provided by the present invention optimizes the atomization effect of the raw material, strengthens the reaction characteristics, and can allow the raw material to be more fully mixed with the high-temperature catalyst, ensuring that the high-boiling point components such as hydrogenated heavy oil in the raw material are fully vaporized, so that the high-boiling point components such as hydrogenated heavy oil can be better cracked in the reactor to obtain a better product distribution. At the same time, the catalytic cracking system can also adapt to different proportions of hydrogenated heavy oil, and then adapt to the raw material composition of different refineries, and has good applicability.
[0091] The preferred embodiments of the present invention are described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.
Claims
1. A catalytic cracking system, It is characterized in that The invention comprises a bed reactor (10) and a feed pipe (20) connected to the bottom of the bed reactor (10); the feed pipe (20) is used to feed a high-temperature catalyst capable of causing a raw material to undergo a catalytic cracking reaction into the bed reactor (10); a first feed port (21) is provided on the side wall of the feed pipe (20) for feeding the raw material into the tube cavity of the feed pipe (20); and the first feed port (21) is spaced apart from the bed reactor (10).
2. The catalytic cracking system according to claim 1, It is characterized in that The distance between the first feed port (21) and the bed reactor (10) is set to enable the raw material and the high-temperature catalyst to contact and mix for 0.1-0.6 seconds before entering the bed reactor (10).
3. The catalytic cracking system according to claim 1, It is characterized in that The catalytic cracking system further comprises a separation device (30) and a regenerator (40), wherein the separation device (30) is used to separate the reaction oil gas and the catalyst to be regenerated generated by the bed reactor (10), and the regenerator (40) is used to regenerate the catalyst to be regenerated by burning. A second feed port (22) is provided on the side wall of the feed pipe (20), and the first feed port (21) and the second feed port (22) are arranged in sequence on the side wall of the feed pipe (20) in a direction away from the bed reactor (10), and the regenerator (40) is connected to the second feed port (22) for feeding the regenerated catalyst obtained by charring and regenerating the regenerator (40) into the feed pipe (20).
4. The catalytic cracking system according to claim 1, It is characterized in that The first feed port (21) is provided with a nozzle for spraying the raw material into the feed pipe (20).
5. The catalytic cracking system according to any one of claims 1 to 4, It is characterized in that The bed reactor (10) is connected to a side pipeline (11) for adding catalyst to the bed reactor (10).
6. A catalytic cracking method, It is characterized in that The catalytic cracking method comprises: The raw material and the high temperature catalyst for catalyzing the raw material to undergo catalytic cracking reaction are contacted and mixed in advance, and then fed into the bed reactor (10) to undergo the catalytic cracking reaction.
7. The catalytic cracking method according to claim 6, It is characterized in that The raw material and the high temperature catalyst are contacted and mixed for 0.1-0.6 seconds before entering the bed reactor (10).
8. The catalytic cracking method according to claim 6, It is characterized in that The catalytic cracking method further comprises: using a separation device (30) to separate the reaction oil gas and the catalyst to be regenerated generated by the catalytic cracking reaction, using a regenerator (40) to burn and regenerate the catalyst to be regenerated to obtain a regenerated catalyst, and then using the regenerated catalyst as the high-temperature catalyst to contact and mix with the raw material for 0.1-0.6 seconds, and then feeding it into the bed reactor (10) again to carry out the catalytic cracking reaction.
9. The catalytic cracking method according to any one of claims 6 to 8, It is characterized in that The catalytic cracking method further comprises: adding catalyst to the bed reactor (10).
10. The catalytic cracking method according to claim 9, It is characterized in that The amount of catalyst added to the bed reactor (10) accounts for 5-30% by weight of the catalyst circulation amount in the bed reactor (10).