Device and method for direct catalytic cracking of electric heating crude oil

Abstract

The invention discloses a device and a method for direct catalytic cracking of electric heating crude oil. A plurality of nozzles are arranged in the circumferential direction of the side wall of the fluidized bed and are close to the bottom of the fluidized bed; a slag discharge port and a first gas inlet are formed in the bottom of the fluidized bed; a plurality of output ends of the raw material and catalyst mixer are respectively connected to the plurality of corresponding nozzles; the second heating assembly extends into the fluidized bed; the annular heating area is located above the nozzle, and the first air inlet corresponds to the annular heating area; one end of the reaction tube is connected to the top of the fluidized bed, and the other end is connected to the input end of the cyclone separator; the first heating assembly is arranged on the outer wall of the vertical part of the reaction tube; the first output end of the cyclone separator is connected to the fine coke particle storage area, and the second output end of the cyclone separator is connected to the input end of the cooling separator. An electric heating heat supply mode is adopted, a cheap catalyst does not need to be burnt and regenerated, a regenerator-free device is adopted, carbon emission is low, the structure is simple, and operation is convenient.

Description

Technical Field

[0001] The present application relates to the field of petrochemical technology, and in particular to a device and method for direct catalytic cracking of crude oil by electric heating. Background Art

[0002] The rapid development of new energy vehicles has continuously squeezed the market space of traditional fuel vehicles, which has had a direct impact on the refined oil market. In order to adapt to this development trend, the transformation of the oil refining industry to the chemical industry has become a general trend.

[0003] Although the existing crude / heavy oil catalytic cracking technology is an important technology in the process of maximizing crude oil production into chemicals, this technology currently faces two major challenges:

[0004] On the one hand, it needs to regenerate the catalyst through burning and provide the required heat for the reaction. However, providing heat through burning inevitably produces a large amount of flue gas containing low-concentration carbon dioxide, which has a high carbon emission intensity and high subsequent capture and treatment costs.

[0005] On the other hand, in addition to the reactor, a regenerator is also required. The catalyst particles are recycled between the two devices, making the entire process relatively complicated and difficult to operate. Summary of the invention

[0006] The embodiments of the present application provide a device and method for direct catalytic cracking of crude oil by electric heating, which solves two major problems in the prior art: first, the carbon emission intensity of catalyst coke regeneration heating is high and carbon emission reduction is difficult; second, the catalyst particles need to circulate between the reactor and the regenerator, resulting in the whole process being complicated and difficult to operate. In addition, a reaction tube similar to light hydrocarbon steam cracking is set on the upper part of the fluidized bed, and the light hydrocarbons generated by the primary cracking of crude oil are subjected to secondary cracking to improve the overall cracking efficiency.

[0007] In the first aspect, an embodiment of the present application provides an apparatus for direct catalytic cracking of electrically heated crude oil, comprising a feedstock and catalyst mixer, a fluidized bed, a reaction tube, a cyclone separator, a cooling separator, a first heating component and a second heating component; the first input end of the feedstock and catalyst mixer is connected to the feedstock output end, and the second input end thereof is connected to the catalyst output end; a plurality of nozzles are arranged circumferentially on the side wall of the fluidized bed, and the plurality of nozzles are all close to the bottom of the fluidized bed, and the nozzles are configured to atomize crude oil, recycled oil and water vapor; a slag discharge port and a first air inlet are arranged at the bottom of the fluidized bed; the plurality of output ends of the feedstock and catalyst mixer are respectively connected to the corresponding plurality of nozzles; the second heating component extends into the interior of the fluidized bed and is configured to atomize crude oil, recycled oil and water vapor in the fluidized bed An annular heating area is formed in the bed so that the temperature in the annular heating area is higher than the temperature outside the annular heating area; the annular heating area is located above the nozzle, and the first air inlet corresponds to the annular heating area; one end of the reaction tube is connected to the top of the fluidized bed, and the other end thereof is connected to the input end of the cyclone separator; the first heating assembly is arranged on the outer wall of the vertical part of the reaction tube; the first output end of the cyclone separator is connected to the fine coke particle storage area, and the second output end thereof is connected to the input end of the cooling separator; the first output end of the cooling separator is connected to the chemical storage area, the second output end thereof is connected to the raw material output end, and the third output end thereof is connected to the first air inlet; the fluidized bed and the reaction tube are both made of metal.

[0008] In combination with the first aspect, in a possible implementation, the fluidized bed includes a reduced diameter section and a constant diameter section; a slag discharge port and a first air inlet are provided at the bottom of the constant diameter section, and a plurality of nozzles are provided circumferentially on the outer wall thereof, and the plurality of nozzles are close to the bottom of the constant diameter section; one end of the reduced diameter section is connected to an end of the reaction tube away from the cyclone separator and the top of the constant diameter section.

[0009] In combination with the first aspect, in a possible implementation, a plurality of second air inlets are arranged circumferentially on the outer wall of the reaction tube and are located below the second heating assembly; the plurality of second air inlets are all connected to the third output end of the cooling separator.

[0010] In combination with the first aspect, in a possible implementation, the first heating assembly includes a first electromagnetic coil and a first electromagnetic heating power supply; the first electromagnetic coil is wound around the outer wall of the vertical part of the reaction tube; both ends of the first electromagnetic coil are connected to the first electromagnetic heating power supply.

[0011] In combination with the first aspect, in a possible implementation, the second heating assembly includes a second electromagnetic coil, a second electromagnetic heating power supply, a circulation tube and a heating rod; the second electromagnetic coil is wound around the circumference of the outer wall of the fluidized bed, and both ends of the second electromagnetic coil are connected to the second electromagnetic heating power supply; the circulation tube and the heating rod are both located in the fluidized bed and are both made of metal; one end of the heating rod is connected to the bottom wall of the fluidized bed, and the other end is a free end; the circulation tube is arranged on the outside of the heating rod and is connected to the inner wall of the fluidized bed; the vertical part of the reaction tube, the circulation tube, the heating rod and the fluidized bed are coaxial, and the circulation tube and the second electromagnetic coil are both located above the nozzle.

[0012] In combination with the first aspect, in a possible implementation, the second heating assembly includes a resistance heating power supply, a heating tube and a heating rod; the heating tube and the heating rod are both located in the fluidized bed and are provided with resistance wires therein; one end of the heating rod is connected to the bottom wall of the fluidized bed, and the other end is a free end; the heating tube is arranged on the outside of the heating rod and is connected to the inner wall of the fluidized bed; the resistance heating power supply is arranged outside the fluidized bed, and the two ends of the resistance wires in the heating tube and the heating rod are respectively connected to the resistance heating power supply; the heating tube is located above the nozzle.

[0013] In combination with the first aspect, in a possible implementation, the device for direct catalytic cracking of electrically heated crude oil also includes an internal component; the internal component is disposed in the vertical portion of the reaction tube and is configured to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube.

[0014] In combination with the first aspect, in a possible implementation, the internal structure includes sleeves of equal diameters arranged in a plurality of the reaction tubes; the plurality of sleeves are coaxial with the vertical portion of the reaction tube, and the material resistivity gradually decreases from the innermost sleeve to the outermost sleeve, so as to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube.

[0015] In combination with the first aspect, in a possible implementation, the internal structure includes a sleeve with a variable diameter distribution arranged in a plurality of the reaction tubes; the vertical portion in the reaction tube and the plurality of the sleeves are coaxial, and the material resistivity of the plurality of the sleeves is equal to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube.

[0016] In a second aspect, an embodiment of the present application provides a method for direct catalytic cracking of crude oil by electric heating, the method comprising:

[0017] The crude oil and the catalyst are uniformly mixed in a raw material and catalyst mixer to form a mixed material, wherein the catalyst comprises at least one of red mud, pyrite, calcium hydroxide, calcium oxide, sodium hydroxide, potassium hydroxide, biomass ash, biomass charcoal, potassium acetate, sodium acetate, potassium carbonate, sodium carbonate, fatty acid potassium, fatty acid sodium, ferroferric oxide, and ferric oxide;

[0018] Adding first petroleum coke particles as bed particles into the fluidized bed, introducing preheated gas through the air inlet of the fluidized bed to fluidize the bed particles, the temperature of the preheated gas being 200-500° C.;

[0019] The second heating assembly is started to make the interior of the fluidized bed reach a preset cracking temperature, and the temperature in the annular heating area is higher than the temperature outside the annular heating area, and the preset cracking temperature is 600-900°C;

[0020] The first heating component is started, and the metal wall of the reaction tube is heated to a predetermined cracking temperature of 700-1000° C. by adjusting the current magnitude and the current frequency;

[0021] The mixed flow and water vapor are sprayed into the fluidized bed through a nozzle to cause evaporation, vaporization and cracking reactions. The gaseous hydrocarbons and fine coke particles produced after the cracking reaction are sent to the reaction tube for further cracking, and the second petroleum coke particles produced after the cracking reaction are coated on the surface of the first petroleum coke particles, and part of the second petroleum coke particles with catalysts and the first coarse coke particles are discharged through a slag discharge port;

[0022] The gaseous hydrocarbons in the reaction tube undergo further cracking reactions and are separated into fine coke particles and oil and gas by a cyclone separator;

[0023] The oil and gas enter the cooling separator, and the separated small molecule alkanes and low-value olefins are circulated and sent to the first air inlet of the fluidized bed and the second air inlet of the reaction tube as fluidizing gas and cracking raw materials to continue to participate in the cracking reaction;

[0024] The chemicals separated by the cooling separator are transported to the chemical area, while the separated recycled oil is returned to the raw material output end to continue to participate in the cracking reaction.

[0025] One or more technical solutions provided in the embodiments of the present application have at least the following technical effects:

[0026] The device for direct catalytic cracking of electric heating crude oil provided in the embodiment of the present application includes a raw material and catalyst mixer, a fluidized bed, a reaction tube, a cyclone separator, a cooling separator, a first heating component and a second heating component. Crude oil enters the raw material and catalyst mixer from the raw material output end, and the catalyst enters from the catalyst output end. The two are fully mixed in the mixer to form a uniform mixture, thereby ensuring the uniformity and efficiency of the catalytic cracking reaction. The mixture is atomized into fine droplets through multiple nozzles, accompanied by the addition of water vapor to enhance its fluidity and reactivity. The first air inlet provides gas to maintain the fluidized state of the fluidized bed, ensuring that the mixture is fully in contact with the particles in the bed and reacts. The second heating component forms an annular heating area in the fluidized bed, the temperature in the area is higher, and the temperature outside the area is lower. This design not only alleviates the coking problem of the nozzle, but also forms a circulation from the inside to the top and the outside to the bottom. This circulation allows the mixture to quickly mix with the bed particles and undergo a cracking reaction, accelerating the process of the reaction. The second petroleum coke generated by the cracking reaction is deposited on the surface of the bed particles and is discharged through the slag discharge port along with part of the second petroleum coke particles and the first petroleum coke particles carrying the catalyst. The gaseous hydrocarbons and fine coke particles generated by the cracking reaction are sent to the reaction tube for further cracking. After passing through the cyclone separator, the fine coke particles and the oil and gas are effectively separated. After the oil and gas enter the cooling separator, the separated small molecule alkanes and low-value olefins are circulated into the first air inlet of the fluidized bed and continue to participate in the reaction as fluidizing gas and cracking raw materials, thereby realizing the recycling of resources and reducing production costs. The cooling separator also separates chemicals, which are transported to the chemical area to provide raw materials for subsequent chemical production. At the same time, the separated recycled oil is returned to the raw material output end to continue to participate in the cracking reaction, thereby improving the utilization rate of the raw materials and the overall efficiency of the device. The catalyst of the present application has the functions of catalyzing the cracking of hydrocarbons, reducing the generation of coke, and accelerating the gasification of coke, and does not require a complex regeneration system. A fluidized bed is used as the primary cracking reactor for crude oil, and most of the second petroleum coke generated is wrapped on the surface of the bed particles, which is convenient for discharge from the reactor through the slag discharge port, thereby solving the coking problem in the existing steam cracking technology. In addition, the device can also process medium and heavy crude oils, and can achieve long-term continuous operation. The reaction tubes arranged on the upper part of the fluidized bed promote the in-depth progress of the secondary cracking reaction and improve the conversion rate. In summary, the present application adopts an electric heating heating method, does not require a cheap catalyst for burning and regeneration, and does not require a regenerator-free device, has low carbon emissions, a simple structure, and is easy to operate. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] In order to more clearly illustrate the technical solutions in the embodiments of the present application, the following is a brief introduction to the drawings required for use in the description of the embodiments of the present application. Obviously, the drawings described below are some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0028] Figure 1 Schematic diagram of the structure of the device for direct catalytic cracking of crude oil by electric heating provided in the embodiment of the present application Figure 1 ;

[0029] Figure 2 Schematic diagram of the structure of the device for direct catalytic cracking of crude oil by electric heating provided in the embodiment of the present application Figure 2 ;

[0030] Figure 3 A sleeve with variable diameter distribution provided in an embodiment of the present application;

[0031] Figure 4 The casing with equal diameter distribution provided in the embodiment of the present application;

[0032] Figure 5 This is a process flow chart of the method for direct catalytic cracking of crude oil by electrical heating provided in an embodiment of the present application.

[0033] Icons: 1-raw material and catalyst mixer; 2-fluidized bed; 21-reduced diameter section; 22-equal diameter section; 23-nozzle; 24-first air inlet; 25-slag discharge port; 3-reaction tube; 31-second air inlet; 4-cyclone separator; 5-cooling separator; 6-first heating component; 61-first electromagnetic coil; 62-first electromagnetic heating power supply; 7-second heating component; 71-second electromagnetic coil; 72-second electromagnetic heating power supply; 73-circulation tube; 74-resistance heating power supply; 75-heating tube; 8-internal structure component; 81-sleeve; 9-raw material output end; 10-catalyst output end; 11-heating rod. DETAILED DESCRIPTION

[0034] The following will be combined with the drawings in the embodiments of the present application to clearly and completely describe the technical solutions in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of this application.

[0035] In the description of the embodiments of the present application, it should be noted that the orientation or positional relationship indicated by the terms "center", "up", "down", "left", "right", "vertical", "horizontal", "inside", "outside", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the embodiments of the present application and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present application. The terms "first", "second", and "third" are used for descriptive purposes only and cannot be understood as indicating or implying relative importance. In addition, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be a connection between the two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the embodiments of the present application can be understood according to the specific circumstances.

[0036] The present application provides a device for direct catalytic cracking of crude oil by electric heating, such as Figures 1 to 4 As shown. The device for direct catalytic cracking of electric heating crude oil includes a raw material and catalyst mixer 1, a fluidized bed 2, a reaction tube 3, a cyclone separator 4, a cooling separator 5, a first heating component 6 and a second heating component 7. The first input end of the raw material and catalyst mixer 1 is connected to the raw material output end 9, and the second input end thereof is connected to the catalyst output end 10. A plurality of nozzles 23 are arranged in the circumference of the side wall of the fluidized bed 2, and the plurality of nozzles 23 are all close to the bottom of the fluidized bed 2, and the nozzles 23 are configured to atomize crude oil, recycled oil and water vapor. A slag discharge port 25 and a first air inlet 24 are arranged at the bottom of the fluidized bed 2. The plurality of output ends of the raw material and catalyst mixer 1 are respectively connected to the corresponding plurality of nozzles 23. The second heating component 7 extends into the interior of the fluidized bed 2, and is configured to form an annular heating area in the fluidized bed 2, so that the temperature in the annular heating area is higher than the temperature outside the annular heating area. The annular heating area is located above the nozzle 23, and the first air inlet 24 corresponds to the annular heating area. One end of the reaction tube 3 is connected to the top of the fluidized bed 2, and the other end thereof is connected to the input end of the cyclone separator 4. The first heating assembly 6 is arranged on the outer wall of the vertical portion of the reaction tube 3. The first output end of the cyclone separator 4 is connected to the fine coke particle storage area, and the second output end thereof is connected to the input end of the cooling separator 5. Specifically, the oil and gas separated by the cyclone separator 4 is transported to the cooling separator 5 through the second output end, and the separated fine coke particles are transported to the fine coke particle storage area. The fine coke particles in the fine coke particle storage area can also be added to the fluidized bed 2 to absorb heat as bed particles.

[0037] The first output end of the cooling separator 5 is connected to the chemical storage area, the second output end thereof is connected to the raw material output end 9, and the third output end thereof is connected to the first air inlet 24. The fluidized bed 2 and the reaction tube 3 are both made of metal. Specifically, the olefins, aromatics and other chemicals separated by the cooling separator 5 are transported to the chemical storage area.

[0038] First petroleum coke particles are added as bed particles in the fluidized bed 2. The particle size of the first petroleum coke particles is 0.05-5 mm.

[0039] It should be noted that crude oil enters the raw material and catalyst mixer 1 from the raw material output end 9, and the catalyst enters from the catalyst output end 10. The two are fully mixed in the raw material and catalyst mixer 1 to form a uniform mixture, thereby ensuring the uniformity and efficiency of the catalytic cracking reaction. The mixture is atomized into fine droplets through multiple nozzles 23, accompanied by the addition of water vapor to enhance its fluidity and reaction activity. The first air inlet 24 provides gas to maintain the fluidized state of the fluidized bed 2, ensuring that the mixture is fully in contact with the particles in the bed and reacts. The second heating component 7 forms an annular heating area in the fluidized bed 2, where the temperature is higher and the temperature outside the area is lower. This design not only alleviates the coking problem of the nozzle 23, but also forms a circulation from the inside to the top and the outside to the bottom. This circulation allows the mixture to quickly mix with the bed particles and undergo a cracking reaction, accelerating the reaction process. The second petroleum coke generated by the cracking reaction is deposited on the surface of the bed particles and is discharged through the slag discharge port 25 along with the second petroleum coke particles and the first petroleum coke particles with the catalyst. The gaseous hydrocarbons and fine coke particles generated by the cracking reaction are sent to the reaction tube 3 for further cracking. After the cyclone separator 4, the fine coke particles and oil and gas are effectively separated. After the oil and gas enter the cooling separator 5, the separated small molecule alkanes and low-value olefins are circulated into the first air inlet 24 of the fluidized bed 2, and continue to participate in the reaction as fluidized gas and cracking raw materials, thereby realizing the recycling of resources and reducing production costs. The cooling separator 5 also separates chemicals, which are transported to the chemical area to provide raw materials for subsequent chemical production. At the same time, the separated recycled oil is returned to the raw material output end 9 to continue to participate in the cracking reaction, thereby improving the utilization rate of raw materials and the overall efficiency of the device. The catalyst of the present application has the functions of catalyzing hydrocarbon cracking, reducing coke generation, and accelerating coke gasification, and does not require a complex regeneration system. The fluidized bed 2 is used as a primary cracking reactor for crude oil, and most of the second petroleum coke generated is wrapped on the surface of the bed particles, which is convenient for discharge from the reactor through the slag discharge port 25, thereby solving the coking problem in the existing steam cracking technology. In addition, the device can also process medium and heavy crude oils, and can achieve long-term continuous operation. The reaction tube 3 disposed on the upper part of the fluidized bed 2 promotes the further progress of the secondary cracking reaction and improves the conversion rate.

[0040] Specifically, the second petroleum coke particles with catalyst and the first petroleum coke particles discharged from the slag discharge port 25 have high gasification activity and are good gasification raw materials.

[0041] In the embodiment of the present application, the fluidized bed 2 includes a reduced diameter section 21 and a constant diameter section 22. A slag discharge port 25 and a first air inlet 24 are provided at the bottom of the constant diameter section 22, and a plurality of nozzles 23 are provided in the circumferential direction of the outer wall thereof, and the plurality of nozzles 23 are close to the bottom of the constant diameter section 22. One end of the reduced diameter section 21 is connected to one end of the reaction tube 3 away from the cyclone separator 4 and the top of the constant diameter section 22.

[0042] It should be noted that the reduced diameter section 21 allows the gaseous hydrocarbons and fine coke particles generated by the cracking reaction in the fluidized bed 2 to pass through with a faster flow rate due to the gradual reduction in the channel diameter, thereby allowing the gaseous hydrocarbons and fine coke particles to enter the reaction tube 3 more quickly, which not only improves the transmission efficiency of the gaseous hydrocarbons and fine coke particles, but also promotes the in-depth progress of the secondary cracking reaction.

[0043] In the embodiment of the present application, a plurality of second air inlets 31 are arranged on the circumference of the outer wall of the reaction tube 3 and are located below the second heating assembly 7. The plurality of second air inlets 31 are all connected to the third output end of the cooling separator 5.

[0044] It should be noted that after the oil and gas enter the cooling separator 5, the separated small molecule alkanes and low-value olefins are partially sent to the second air inlet 31 as additional cracking raw materials. These small molecule alkanes and low-value olefins directly enter the high-temperature heating area of ​​the reaction tube 3 and can quickly reach the temperature required for cracking, thereby accelerating the progress of the cracking reaction. Since the second air inlet 31 is cleverly arranged below the second heating assembly 7, the material can absorb more energy when flowing through this area, further promoting the in-depth progress of the cracking reaction.

[0045] In the embodiment of the present application, the first heating assembly 6 includes a first electromagnetic coil 61 and a first electromagnetic heating power supply 62. The first electromagnetic coil 61 is wound around the outer wall of the vertical portion of the reaction tube 3. Both ends of the first electromagnetic coil 61 are connected to the first electromagnetic heating power supply 62.

[0046] It should be noted that the reaction tube 3 adopts electromagnetic induction heating, which has no carbon dioxide emission and is environmentally friendly.

[0047] In the embodiment of the present application, the second heating assembly 7 includes a second electromagnetic coil 71, a second electromagnetic heating power supply 72, a circulation tube 73 and a heating rod 11. The second electromagnetic coil 71 is wound around the circumference of the outer wall of the fluidized bed 2, and both ends of the second electromagnetic coil 71 are connected to the second electromagnetic heating power supply 72. The circulation tube 73 and the heating rod 11 are both located in the fluidized bed 2 and are both made of metal. One end of the heating rod 11 is connected to the bottom wall of the fluidized bed 2, and the other end is a free end. The circulation tube 73 is arranged on the outside of the heating rod 11 and is connected to the inner wall of the fluidized bed 2. The vertical part of the reaction tube 3, the circulation tube 73, the heating rod 11 and the fluidized bed 2 are coaxial, and the circulation tube 73 and the second electromagnetic coil 71 are both located above the nozzle 23.

[0048] It should be noted that the second electromagnetic coil 71 is wound around the outer wall of the fluidized bed 2, and after being powered by the second electromagnetic heating power supply 72, an electromagnetic induction heating effect is generated. This heating method can quickly and evenly heat the metal wall surface of the fluidized bed 2, the bed particles inside it, the circulation tube 73 and the heating rod 11, ensuring that the cracking reaction is carried out at the required temperature. At the same time, the second heating component 7 adopts electromagnetic induction heating, which does not require the combustion of fossil fuels, so there is no carbon dioxide emission, which fully meets environmental protection requirements.

[0049] In the embodiment of the present application, the second heating assembly 7 includes a resistance heating power supply 74, a heating tube 75 and a heating rod 11. The heating tube 75 and the heating rod 11 are both located in the fluidized bed 2, and are both provided with resistance wires. One end of the heating rod 11 is connected to the bottom wall of the fluidized bed 2, and the other end is a free end. The heating tube 75 is arranged on the outside of the heating rod 11 and is connected to the inner wall of the fluidized bed 2. The resistance heating power supply 74 is arranged outside the fluidized bed 2, and both ends of the resistance wires in the heating tube 75 and the heating rod 11 are connected to the resistance heating power supply 74. The heating tube 75 is located above the nozzle 23.

[0050] Specifically, in order to reduce the heat loss in the fluidized bed 2, the outer wall of the fluidized bed 2 is also provided with heat insulation cotton. This heat insulation measure can further improve the heating efficiency and ensure that the cracking reaction is carried out at the required temperature.

[0051] It should be noted that resistance wires are provided inside the heating tube 75 and the heating rod 11. When the resistance heating power supply 74 is powered, the resistance wires can quickly generate heat. This resistance heating method not only has a fast heating speed, but also can heat the heating tube 75, the heating rod 11 and the bed particles inside the fluidized bed 2 to the required temperature in a short time. Compared with the electromagnetic induction heating method, the resistance heating method also does not need to burn fossil fuels, so there is no carbon dioxide emission, which fully meets environmental protection requirements.

[0052] Furthermore, the design of the circulation tube 73 or the heating tube 75 in the embodiment of the present application also allows the bed particles to form a circulation from the inside to the top and the outside to the bottom. This circulation helps to quickly mix the mixed material with the bed particles, thereby improving the efficiency of the cracking reaction and the quality of the product.

[0053] In the embodiment of the present application, the device for direct catalytic cracking of crude oil by electric heating further includes an internal component 8. The internal component 8 is disposed in the vertical portion of the reaction tube 3 and is configured to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube 3.

[0054] In the embodiment of the present application, the internal component 8 includes sleeves 81 of equal diameters arranged in a plurality of reaction tubes 3. The plurality of sleeves 81 are coaxial with the vertical portion of the reaction tube 3, and the material resistivity gradually decreases from the innermost sleeve 81 to the outermost sleeve 81, so as to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube 3.

[0055] In the embodiment of the present application, the internal component 8 includes sleeves 81 with variable diameters arranged in the plurality of reaction tubes 3. The vertical portion in the reaction tube 3 and the plurality of sleeves 81 are coaxial, and the material resistivity of the plurality of sleeves 81 is equal, so as to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube 3.

[0056] It should be noted that the internal component 8 can ensure that the gaseous hydrocarbons and fine coke particles are evenly and fully heated in the reaction tube 3. This even heating not only helps the in-depth cracking reaction, but also improves the overall heating efficiency, making the cracking process more efficient.

[0057] like Figure 5 As shown, the present embodiment provides a method for direct catalytic cracking of crude oil by electric heating, the method comprising steps S1-S8:

[0058] S1: Mix crude oil and catalyst in a raw material and catalyst mixer 1 to form a mixed material, wherein the catalyst includes at least one of red mud, pyrite, calcium hydroxide, calcium oxide, sodium hydroxide, potassium hydroxide, biomass ash, biomass charcoal, potassium acetate, sodium acetate, potassium carbonate, sodium carbonate, fatty acid potassium, fatty acid sodium, ferroferric oxide, and ferric oxide.

[0059] It should be noted that the catalyst used in the present application is single-use and relatively inexpensive, and can catalyze hydrocarbon cracking, reduce coke formation, and accelerate coke gasification without requiring a complex regeneration system.

[0060] S2: First petroleum coke particles are added into the fluidized bed 2 as bed particles, and preheated gas is introduced through the air inlet of the fluidized bed 2 to fluidize the bed particles. The temperature of the preheated gas is 200-500°C.

[0061] S3: Start the second heating assembly 7 to make the interior of the fluidized bed 2 reach a preset cracking temperature, and make the temperature in the annular heating area higher than the temperature outside the annular heating area. The preset cracking temperature is 600-900°C.

[0062] S4: Start the first heating component 6, and heat the metal wall of the reaction tube 3 to a predetermined cracking temperature by adjusting the current magnitude and current frequency. The predetermined cracking temperature is 700-1000°C.

[0063] It should be noted that the current frequency is 1-500kHz and the current size is 10-100A.

[0064] S5: The mixed flow and water vapor are sprayed into the fluidized bed 2 through the nozzle 23, and evaporation, vaporization and cracking reactions occur. The gaseous hydrocarbons and fine coke particles produced after the cracking reaction are sent to the reaction tube 3 for further cracking, and the second petroleum coke particles produced after the cracking reaction are coated on the surface of the first petroleum coke particles, and part of the second petroleum coke particles with the catalyst and the first coarse coke particles are discharged through the slag discharge port 25.

[0065] S6: The gaseous hydrocarbons in the reaction tube 3 undergo further cracking reaction, and fine coke particles and oil and gas are separated by the cyclone separator 4.

[0066] Specifically, an internal component 8 is disposed in the reaction tube 3 , and the internal component 8 can ensure that the gaseous hydrocarbons and fine coke particles are heated uniformly and sufficiently in the reaction tube 3 .

[0067] S7: The oil and gas enter the cooling separator 5, and the separated small molecule alkanes and low-value olefins are circulated to the first air inlet 24 of the fluidized bed 2 and the second air inlet 31 of the reaction tube 3 as fluidizing gas and cracking raw materials to continue to participate in the cracking reaction.

[0068] It should be noted that the separated small molecule alkanes and low-value olefins are circulated and sent to the first air inlet 24 of the fluidized bed 2 to continue to participate in the cracking reaction, thereby achieving maximum utilization of resources.

[0069] A plurality of second air inlets 31 are arranged around the outer wall of the reaction tube 3 and are located below the second heating assembly 7. After the oil and gas enter the cooling separator 5, the separated small molecule alkanes and low-value olefins are partially sent to the second air inlet 31. These small molecule alkanes and low-value olefins directly enter the high-temperature heating area of ​​the reaction tube 3 and can quickly reach the temperature required for cracking, thereby accelerating the process of the cracking reaction.

[0070] S8: The chemicals separated by the cooling separator 5 are transported to the chemical area, while the separated recycled oil is returned to the raw material output end 9 to continue to participate in the cracking reaction.

[0071] It should be noted that the chemicals in this application are chemicals such as olefins and aromatics.

[0072] The present application embodiment provides a method for direct catalytic cracking of crude oil by electric heating, wherein the gaseous hydrocarbons in the reaction tube 3 further undergo cracking reaction, and fine coke particles and oil gas are separated by the cyclone separator 4, and further comprising:

[0073] The fine coke particles separated by the cyclone separator 4 are transported to the fluidized bed 2 as bed particles.

[0074] Specifically, fine coke particles are added into the fluidized bed 2 to recover heat.

[0075] Furthermore, the device and method for direct catalytic cracking of crude oil by electric heating provided in the embodiments of the present application show remarkable technical effects in terms of efficient cracking, energy utilization, equipment design, product separation and recycling, economic benefits and environmental benefits, etc. These technical effects jointly promote the innovation and development of crude oil cracking technology and provide strong support for the green and sustainable development of the petrochemical industry.

[0076] The various embodiments in this specification are described in a progressive manner, and the same or similar parts between the various embodiments can be referenced to each other. Each embodiment focuses on the differences from other embodiments.

[0077] The above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit the present application. Although the present application has been described in detail with reference to the aforementioned embodiments, a person of ordinary skill in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some or all of the technical features thereof may be replaced by equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the present application.

Claims

1. A device for direct catalytic cracking of crude oil by electric heating, characterized in that: It comprises a raw material and catalyst mixer (1), a fluidized bed (2), a reaction tube (3), a cyclone separator (4), a cooling separator (5), a first heating component (6) and a second heating component (7); The first input end of the raw material and catalyst mixer (1) is connected to the raw material output end (9), and the second input end is connected to the catalyst output end (10); A plurality of nozzles (23) are arranged in the circumferential direction of the side wall of the fluidized bed (2), and the plurality of nozzles (23) are all close to the bottom of the fluidized bed (2), and the nozzles (23) are configured to atomize crude oil, recycled oil and water vapor; The bottom of the fluidized bed (2) is provided with a slag discharge port (25) and a first air inlet (24); The multiple output ends of the raw material and catalyst mixer (1) are respectively connected to the corresponding multiple nozzles (23); The second heating assembly (7) extends into the interior of the fluidized bed (2) and is configured to form an annular heating area in the fluidized bed (2), so that the temperature in the annular heating area is higher than the temperature outside the annular heating area; The annular heating area is located above the nozzle (23), and the first air inlet (24) corresponds to the annular heating area; One end of the reaction tube (3) is connected to the top of the fluidized bed (2), and the other end is connected to the input end of the cyclone separator (4); The first heating component (6) is arranged on the outer wall of the vertical part of the reaction tube (3); The first output end of the cyclone separator (4) is connected to the fine coke particle storage area, and the second output end thereof is connected to the input end of the cooling separator (5); The first output end of the cooling separator (5) is connected to the chemical storage area, the second output end thereof is connected to the raw material output end (9), and the third output end thereof is connected to the first air inlet (24); The fluidized bed (2) and the reaction tube (3) are both made of metal.

2. The device for direct catalytic cracking of crude oil by electric heating according to claim 1, characterized in that: The fluidized bed (2) comprises a reduced diameter section (21) and a constant diameter section (22); The bottom of the equal-diameter section (22) is provided with a slag discharge port (25) and a first air inlet (24), and a plurality of nozzles (23) are provided in the circumferential direction of the outer wall thereof, and the plurality of nozzles (23) are close to the bottom of the equal-diameter section (22); One end of the reduced diameter section (21) is connected to one end of the reaction tube (3) away from the cyclone separator (4) and to the top of the equal diameter section (22).

3. The device for direct catalytic cracking of crude oil by electric heating according to claim 1, characterized in that: A plurality of second air inlets (31) are arranged in the circumferential direction of the outer wall of the reaction tube (3) and are located below the second heating assembly (7); The plurality of second air inlets (31) are all connected to the third output end of the cooling separator (5).

4. The device for direct catalytic cracking of crude oil by electric heating according to claim 1, characterized in that: The first heating component (6) comprises a first electromagnetic coil (61) and a first electromagnetic heating power source (62); The first electromagnetic coil (61) is wound around the outer wall of the vertical portion of the reaction tube (3); Both ends of the first electromagnetic coil (61) are connected to the first electromagnetic heating power source (62).

5. The device for direct catalytic cracking of crude oil by electric heating according to claim 1, characterized in that: The second heating component (7) comprises a second electromagnetic coil (71), a second electromagnetic heating power supply (72), a circulating flow tube (73) and a heating rod (11); The second electromagnetic coil (71) is wound around the circumference of the outer wall of the fluidized bed (2), and both ends of the second electromagnetic coil (71) are connected to the second electromagnetic heating power source (72); The circulating cylinder (73) and the heating rod (11) are both located in the fluidized bed (2) and are both made of metal; One end of the heating rod (11) is connected to the bottom wall of the fluidized bed (2), and the other end is a free end; The circulation cylinder (73) is arranged on the outside of the heating rod (11) and connected to the inner wall of the fluidized bed (2); The vertical part of the reaction tube (3), the circulation tube (73), the heating rod (11) and the fluidized bed (2) are coaxial, and the circulation tube (73) and the second electromagnetic coil (71) are both located above the nozzle (23).

6. The device for direct catalytic cracking of crude oil by electric heating according to claim 1, characterized in that: The second heating component (7) comprises a resistance heating power supply (74), a heating tube (75) and a heating rod (11); The heating tube (75) and the heating rod (11) are both located in the fluidized bed (2), and are both provided with resistance wires; One end of the heating rod (11) is connected to the bottom wall of the fluidized bed (2), and the other end is a free end; The heating tube (75) is arranged on the outside of the heating rod (11) and connected to the inner wall of the fluidized bed (2); The resistance heating power supply (74) is arranged outside the fluidized bed (2), and both ends of the resistance wire in the heating tube (75) and the heating rod (11) are connected to the resistance heating power supply (74); The heating tube (75) is located above the nozzle (23).

7. The device for direct catalytic cracking of crude oil by electric heating according to claim 1, characterized in that: Also includes an internal structure component (8); The internal component (8) is arranged in the vertical part of the reaction tube (3) and is configured to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube (3).

8. The device for direct catalytic cracking of crude oil by electric heating according to claim 7, characterized in that: The internal component (8) comprises sleeves (81) with equal diameters arranged in the plurality of reaction tubes (3); The plurality of sleeves (81) are coaxial with the vertical portion of the reaction tube (3), and the material resistivity gradually decreases from the innermost sleeve (81) to the outermost sleeve (81) so as to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube (3).

9. The device for direct catalytic cracking of crude oil by electric heating according to claim 7, characterized in that: The internal component (8) comprises sleeves (81) with variable diameters arranged in the plurality of reaction tubes (3); The vertical portion in the reaction tube (3) and the plurality of sleeves (81) are coaxial, and the material resistivity of the plurality of sleeves (81) is equal so as to uniformly heat the gaseous hydrocarbons and fine coke particles entering the reaction tube (3).

10. A method for direct catalytic cracking of crude oil by electric heating, characterized in that: include: The crude oil and the catalyst are uniformly mixed in a raw material and catalyst mixer (1) to form a mixed material, wherein the catalyst comprises at least one of red mud, pyrite, calcium hydroxide, calcium oxide, sodium hydroxide, potassium hydroxide, biomass ash, biomass charcoal, potassium acetate, sodium acetate, potassium carbonate, sodium carbonate, fatty acid potassium, fatty acid sodium, ferroferric oxide, and ferric oxide; First petroleum coke particles are added into the fluidized bed (2) as bed particles, and preheated gas is introduced through the air inlet of the fluidized bed (2) to fluidize the bed particles, wherein the temperature of the preheated gas is 200-500° C.; Starting the second heating assembly (7) so that the interior of the fluidized bed (2) reaches a preset cracking temperature and the temperature in the annular heating area is higher than the temperature outside the annular heating area, the preset cracking temperature being 600-900° C.; Starting the first heating component (6) and heating the metal wall surface of the reaction tube (3) to a predetermined cracking temperature by adjusting the current magnitude and the current frequency thereof, wherein the predetermined cracking temperature is 700-1000° C.; The mixed flow and water vapor are sprayed into the fluidized bed (2) through a nozzle (23) to cause evaporation, vaporization and cracking reactions. The gaseous hydrocarbons and fine coke particles produced after the cracking reaction are sent to a reaction tube (3) for further cracking. The second petroleum coke particles produced after the cracking reaction are coated on the surface of the first petroleum coke particles. Part of the second petroleum coke particles with catalyst and the first coarse coke particles are discharged through a slag discharge port (25); The gaseous hydrocarbons in the reaction tube (3) further undergo cracking reactions and are separated into fine coke particles and oil and gas by a cyclone separator (4); The oil and gas enter the cooling separator (5), and the separated small molecule alkanes and low-value olefins are circulated and sent to the first air inlet (24) of the fluidized bed (2) and the second air inlet (31) of the reaction tube (3) as fluidizing gas and cracking raw materials, and continue to participate in the cracking reaction; The chemicals separated by the cooling separator (5) are transported to the chemical area, while the separated recycled oil is returned to the raw material output end (9) to continue to participate in the cracking reaction.

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