Low-carbon catalytic reforming system and process

Abstract

The invention discloses a low-carbon catalytic reforming system and process, the low-carbon catalytic reforming system comprises a heating reaction module and a separation module, the heating reaction module comprises a reactor, a heater and a first heat exchanger, and a shock wave heating channel is formed in the heater and used for carrying out shock wave heating on a heat exchange medium; the tube pass of the first heat exchanger is communicated with the reactor, the shell pass of the first heat exchanger is communicated with the heater, the raw oil is subjected to a catalytic reforming reaction in the reactor, the separation module comprises an oil-gas separation tower and a stabilization tower, and the oil-gas separation tower is communicated with the reactor for separating hydrogen from a first material flow flowing out of the reactor; the stabilization tower is communicated with the oil-gas separation tower and used for separating gas hydrocarbon, pentane and reformate from the second material flow flowing out of the oil-gas separation tower, compared with an existing catalytic reforming system, fuel such as methane does not need to be used, and emission of carbon dioxide is reduced.

Description

Technical Field

[0001] The present application belongs to the field of petrochemical technology, and specifically relates to a low-carbon catalytic reforming system and process. Background Art

[0002] Diesel hydrofining refers to the process of improving the quality of oil products by converting non-hydrocarbon compounds such as sulfur, nitrogen, and oxygen contained in oil products into corresponding hydrocarbons and easily removable hydrogen sulfide, ammonia, and water under the action of hydrofining catalysts under certain temperature, pressure, hydrogen-to-oil ratio, and air velocity conditions. The raw oil used for diesel hydrofining needs to be preheated before the hydrogenation reaction. In the prior art, the heating of the raw oil is usually carried out by thermal radiation. The raw oil passes through the furnace tube of the heating furnace, and the combustible gas is continuously introduced into the radiation chamber of the heating furnace. The thermal radiation generated by the gas combustion continuously flushes the furnace tube to achieve the purpose of heating the raw oil. However, a large amount of carbon dioxide and some sulfides will be generated during the combustion process, which is not conducive to environmental protection. Summary of the invention

[0003] In view of the above-mentioned defects or shortcomings, the present application provides a low-carbon catalytic reforming system and process, aiming to solve the technical problem of carbon dioxide and sulfide emissions caused by existing catalytic reforming systems based on combustion heating.

[0004] To achieve the above-mentioned purpose, the present application provides a low-carbon catalytic reforming system, comprising a heating reaction module and a separation module;

[0005] The heating reaction module includes a reactor, a heater and a first heat exchanger. The heater is formed with a shock wave heating channel for shock wave heating of the heat exchange medium. The tube side of the first heat exchanger is connected to the reactor, and the shell side of the first heat exchanger is connected to the heater. The crude oil undergoes catalytic reforming reaction in the reactor.

[0006] The separation module includes an oil-gas separation tower and a stabilization tower. The oil-gas separation tower is connected to the reactor to separate hydrogen from the first material flow flowing out of the reactor. The stabilization tower is connected to the oil-gas separation tower to separate gaseous hydrocarbons, pentane and reforming products from the third material flow flowing out of the oil-gas separation tower.

[0007] In an embodiment of the present application, the heating reaction module includes a plurality of heating reaction units connected in sequence, each heating reaction unit includes a reactor, a first heat exchanger and at least one heater, and the reactor of the last heating reaction unit is connected to an oil-gas separation tower.

[0008] In an embodiment of the present application, the system further includes a second heat exchanger, which is disposed upstream of the first heating reaction unit, and the shell side of the second heat exchanger is connected to the reactor of the last heating reaction unit.

[0009] In an embodiment of the present application, the separation module also includes a third heat exchanger, the tube side of the third heat exchanger corresponds to the outlet of the oil and gas separation tower and the inlet of the stabilization tower, and the shell side of the third heat exchanger is connected to the outlet of the stabilization tower for cooling the reforming product.

[0010] In an embodiment of the present application, the separation module also includes a fourth heat exchanger, the tube side of the fourth heat exchanger corresponds to the outlet and inlet of the stabilization tower, and the shell side of the third heat exchanger is connected to the outlet of the reactor of the last heating reaction unit and the inlet of the oil and gas separation tower.

[0011] In an embodiment of the present application, the heater includes an outer shell, a first fixed blade grid, a rotating blade grid, a second fixed blade grid and a rotor. The outer shell forms a shock wave heating channel. The cross-section of the shock wave heating channel is annular. The first fixed blade grid, the rotating blade grid and the second fixed blade grid are sequentially arranged in the shock wave heating channel from front to back. The rotor is arranged on the outer shell to drive the rotating blade grid to rotate in the shock wave heating channel.

[0012] In an embodiment of the present application, the heater also includes a plurality of partitions arranged in the shock wave heating channel, the plurality of partitions are used to separate a plurality of heating spaces, each heating space is provided with a plurality of first fixed blades for forming a first fixed blade grid, and a plurality of second fixed blades for forming a second fixed blade grid.

[0013] In the embodiment of the present application, both the first stationary blade and the second stationary blade have a curved streamline profile.

[0014] In an embodiment of the present application, the installation angle of the first fixed blade is between 35° and 75°, the inlet angle of the first fixed blade is between 0° and 45°, and the outlet angle of the first fixed blade is between 35° and 75°; the installation angle of the second fixed blade is between 45° and 85°, the inlet angle of the second fixed blade is between 25° and 65°, and the outlet angle of the second fixed blade is between 25° and 65°.

[0015] In the embodiment of the present application, the rotating blade grid includes a plurality of rotating blades, and each rotating blade has a curved profile toward its rotation direction.

[0016] In the embodiment of the present application, the installation angle of the rotating blade is between 10° and 80°, the inlet angle of the rotating blade is between 35° and 75°, and the outlet angle of the rotating blade is between 35° and 75°.

[0017] To achieve the above objectives, the present application also provides a low-carbon catalytic reforming process, comprising:

[0018] S1: The heat exchange medium enters the shell side of the first heat exchanger after being heated to a preset temperature by shock wave;

[0019] S2: The feedstock oil and hydrogen are sequentially passed through multiple heating reaction units for catalytic reforming;

[0020] S3: heating the reaction unit to separate the first material flow and the second material flow;

[0021] S4: the first material flows through the shell side of the second heat exchanger into the oil-gas separation tower, and the second material flows through the shell side of the fourth heat exchanger into the oil-gas separation tower;

[0022] S5: an oil-gas separation tower separates hydrogen and a third stream;

[0023] S6: the third material flows through the shell side of the third heat exchanger and enters the stabilization tower;

[0024] S7: The stabilization tower separates the fourth material stream and the fifth material stream. The fourth material stream re-enters the stabilization tower only through the shell side of the fourth heat exchanger, and the fifth material stream is discharged through the shell side of the third heat exchanger.

[0025] In the embodiment of the present application, step S2 also includes: the crude oil passes through the second heat exchanger and the first heat exchanger of the first heating reaction unit in sequence and enters the first mixer to mix with hydrogen, and then enters the reactor of the first heating reaction unit after mixing.

[0026] In the embodiment of the present application, step S5 also includes: separating the unreacted feedstock oil and reintroducing it into the first mixer.

[0027] In the embodiment of the present application, in step S1, the preset temperature is between 600-1200°C.

[0028] Through the above technical solution, the low-carbon catalytic reforming system provided in the embodiment of the present application has the following beneficial effects:

[0029] When using the above-mentioned low-carbon catalytic reforming system, in the system, the crude oil passes through the first heat exchanger, the reactor, the oil-gas separation tower and the stabilization tower in sequence. In the first heat exchanger, the crude oil and the heated heat exchange medium undergo convection heat exchange to reach the temperature required for catalytic reforming. The heating method of the heat exchange medium is shock wave heating. A shock wave heating channel is formed in the heater. The heat exchange medium is decelerated from sonic or supersonic speed to subsonic speed in the shock wave heating channel. In this process, the kinetic energy of the heat exchange medium is converted into thermal energy. Compared with the prior art that uses fuel combustion, this process does not involve chemical changes, does not produce carbon dioxide or sulfide, and is beneficial to environmental protection. After the crude oil and hydrogen react in the reactor, the unreacted hydrogen is separated out by the oil-gas separation tower, and the qualified reforming product is separated out by the stabilization tower.

[0030] Other features and advantages of the present application will be described in detail in the subsequent specific embodiments. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] The accompanying drawings are used to provide an understanding of the present application and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present application but do not constitute a limitation to the present application. In the accompanying drawings:

[0032] Figure 1 is a schematic diagram of a low-carbon catalytic reforming system according to an embodiment of the present application;

[0033] Figure 2 is a horizontal cross-sectional schematic diagram of a heater according to an embodiment of the present application;

[0034] Figure 3 is a front schematic diagram of a heater according to an embodiment of the present application;

[0035] Figure 4 is a schematic diagram of a blade at a certain location in a shock wave heating channel according to an embodiment of the present application;

[0036] Figure 5 It is a flow chart of a low-carbon catalytic reforming process according to one embodiment of the present application.

[0037] Description of Reference Numerals

[0038] 10 Reactor 20 Oil and gas separation tower

[0039] 30 Stabilization tower 40 Heater

[0040] 41 outer shell 42 first fixed blade

[0041] 43 Rotating blade 44 Second fixed blade

[0042] 45 shock wave heating channel 51 first heat exchanger

[0043] 52 second heat exchanger 53 third heat exchanger

[0044] 54 Fourth heat exchanger 61 First mixer

[0045] 62 Second mixer 70 Cooler

[0046] 81 First booster pump 82 Second booster pump

[0047] 90 Buffer tank DETAILED DESCRIPTION

[0048] The specific embodiments of the present application are described in detail below in conjunction with the accompanying drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present application, and are not used to limit the present application.

[0049] The low-carbon catalytic reforming system and process of the present application will be described below with reference to the accompanying drawings.

[0050] The present application provides a novel low-carbon catalytic reforming system. Figure 1 As shown, in a specific embodiment, the low-carbon catalytic reforming system includes a low-carbon catalytic reforming system, including a heating reaction module and a separation module;

[0051] The heating reaction module includes a reactor 10, a heater 40 and a first heat exchanger 51. The heater 40 is formed with a shock wave heating channel 45 for shock wave heating of the heat exchange medium. The tube side of the first heat exchanger 51 is connected to the reactor 10, and the shell side of the first heat exchanger 51 is connected to the heater 40. The crude oil undergoes a catalytic reforming reaction in the reactor 10.

[0052] The separation module includes an oil-gas separation tower 20 and a stabilization tower 30. The oil-gas separation tower 20 is connected to the reactor 10 for separating hydrogen from the first material flow flowing out of the reactor 10. The stabilization tower 30 is connected to the oil-gas separation tower 20 for separating gaseous hydrocarbons, pentane and reforming products from the third material flow flowing out of the oil-gas separation tower 20.

[0053] When the above-mentioned low-carbon catalytic reforming system is used, in the system, the crude oil passes through the first heat exchanger 51, the reactor 10, the oil-gas separation tower 20 and the stabilization tower 30 in sequence. In the first heat exchanger 51, the crude oil and the heated heat exchange medium are subjected to convective heat exchange to reach the temperature required for catalytic reforming. The heating method of the heat exchange medium is shock wave heating. A shock wave heating channel 45 is formed in the heater 40. The heat exchange medium is decelerated from the sonic speed or supersonic speed to the subsonic speed in the shock wave heating channel 45. In this process, the kinetic energy of the heat exchange medium is converted into thermal energy. Compared with the prior art using fuel combustion, this process does not involve chemical changes, does not produce carbon dioxide or sulfide, and is beneficial to environmental protection. After the crude oil and hydrogen react in the reactor 10, the unreacted hydrogen is separated by the oil-gas separation tower 20, and the qualified reforming product is separated by the stabilization tower 30.

[0054] It should be noted that in the present application, the heater 40 utilizes the principle of shock wave heating. Shock wave is a gas dynamic phenomenon. For gas flowing at the speed of sound or supersonic speed, its speed will be faster than the conduction of its pressure, thereby superimposing to form waves, and when the rear gas passes through these waves, compression waves or expansion waves will be formed. When the gas in the sonic or supersonic state encounters an obstacle, its compression waves will be superimposed to form a shock wave, which can cause the gas temperature to rise sharply and the speed to drop. In essence, part of the kinetic energy of the gas is converted into heat energy.

[0055] In the embodiment of the present application, the heating reaction module includes a plurality of heating reaction units connected in sequence, each of which includes a reactor 10, a first heat exchanger 51 and at least one heater 40, and the reactor 10 of the last heating reaction unit is connected to the oil-gas separation tower 20. The mixture of crude oil and hydrogen is catalytically reformed through a plurality of heating reaction units to obtain as much reforming product as possible, and the mixture will be reheated in the process of entering from one reactor 10 to another reactor 10 to ensure the efficiency of the reaction.

[0056] Specifically, the low-carbon catalytic reforming system includes three heating reaction units, and a first heat exchanger 51 is arranged upstream of the reactor 10 of each heating reaction unit. A second mixer 62 for mixing crude oil and hydrogen is arranged between the first heat exchanger 51 of the first heating reaction unit and the reactor 10. The crude oil and hydrogen are mixed in the second mixer 62 and then enter the reactor 10.

[0057] Furthermore, the shell side inlet of each first heat exchanger 51 is connected to a first mixer 61 , and each first mixer 61 is connected to at least one heater 40 . The heated heat exchange medium enters the shell side of the first heat exchanger 51 after being mixed by the first mixer 61 .

[0058] More specifically, the low-carbon catalytic reforming system further includes a waste heat recovery device, which is used to reintroduce the heat exchange medium discharged from the last heating reaction unit into the heater 40 of the first heating reaction unit. By adopting the waste heat recovery device, the low-carbon catalytic reforming system can recover and utilize heat energy to the maximum extent, thereby improving the energy utilization efficiency of the device. This recycling design helps to save energy and reduce carbon emissions, and is in line with the principle of low-carbon and environmental protection.

[0059] It should be noted that in this application, "upstream" and "downstream" are defined according to the direction of the oil route, and the logistics are transported from upstream to downstream.

[0060] In the embodiment of the present application, the system further includes a second heat exchanger 52, which is disposed upstream of the first heating reaction unit, and the shell side of the second heat exchanger 52 is connected to the reactor 10 of the last heating reaction unit. In the second heat exchanger 52, the crude oil and the first stream separated from the reactor 10 of the last heating reaction unit are subjected to convective heat exchange, which not only realizes the cooling of the first stream, but also increases the temperature of the crude oil, effectively utilizes thermal energy, and reduces the power consumption of the heater 40.

[0061] Specifically, the low-carbon catalytic reforming system also includes a first boost pump 81 and a buffer tank 90. ​​The crude oil enters the second heat exchanger 52 after being pressurized by the first boost pump 81, and the hydrogen enters the first mixer 61 through the buffer tank 90 to make the system more stable.

[0062] In the embodiment of the present application, the separation module further includes a third heat exchanger 53, the tube side of the third heat exchanger 53 is connected to the outlet of the oil-gas separation tower 20 and the inlet of the stabilization tower 30, and the shell side of the third heat exchanger 53 is connected to the outlet of the stabilization tower 30 for cooling the reformed product. The third stream separated from the oil-gas separation tower 20 and the reformed product separated from the stabilization tower 30 are subjected to convective heat exchange in the third heat exchanger 53, thereby improving the utilization rate of thermal energy and reducing the power consumption of the system.

[0063] Specifically, the separation module further includes a second booster pump 82 disposed between the oil-gas separation tower 20 and the third heat exchanger 53 for boosting the third material flow.

[0064] In the embodiment of the present application, the separation module also includes a fourth heat exchanger 54, the tube side of the fourth heat exchanger 54 corresponds to the outlet and inlet of the stabilization tower 30, and the shell side of the third heat exchanger 53 is connected to the outlet of the reactor 10 of the last heating reaction unit and the inlet of the oil-gas separation tower 20. The second stream separated by the reactor 10 and the fourth stream separated by the stabilization tower 30 are subjected to convection heat exchange in the fourth heat exchanger 54. After the heat exchange, the fourth stream returns to the stabilization tower 30 for separation, which improves the utilization rate of the crude oil on the one hand and realizes the cooling of the second stream on the other hand. Specifically, a cooler 70 is also provided between the fourth heat exchanger 54 and the oil-gas separation tower 20, which is used to reduce the second stream to a specified temperature to ensure the separation efficiency of the oil-gas separation tower 20.

[0065] like Figure 2 As shown, in the embodiment of the present application, the heater 40 includes an outer shell 41, a first fixed blade cascade 42, a rotating blade cascade 43, a second fixed blade cascade 44 and a rotor. The outer shell 41 is formed with a shock wave heating channel 45. The cross section of the shock wave heating channel 45 is annular. The first fixed blade cascade 42, the rotating blade cascade 43, and the second fixed blade cascade 44 are sequentially arranged in the shock wave heating channel 45 from front to back. The rotor is arranged on the outer shell 41 to drive the rotating blade cascade 43 to rotate in the shock wave heating channel 45. With the rotation of the rotating blade cascade 43, the heat exchange medium enters from the inlet of the first fixed blade cascade 42 at a subsonic speed, and is accelerated to a sonic speed or a supersonic speed by the rotating blade cascade 43, and then impacts the second fixed blade cascade 44. In the process of impacting the second fixed blade cascade 44, part of the kinetic energy of the heat exchange medium is converted into heat energy, and then flows out along the second fixed blade cascade 44. The rotor is driven by electric energy, so that the heat exchange medium first obtains kinetic energy in the heater 40 and then converts the kinetic energy into thermal energy. The source of electric energy can be clean energy such as wind energy, hydrogen energy, nuclear energy, etc., which is more low-carbon and environmentally friendly.

[0066] Specifically, the first fixed blade cascade 42 and the second fixed blade cascade 44 can be adjusted, and the relative spacing between the first fixed blade cascade 42 and the second fixed blade cascade 44 can be specifically set according to the speed of the heat exchange medium to meet the need for accelerating the heat exchange medium. Further, the first fixed blade cascade 42 and the second fixed blade cascade 44 constitute an air duct for the flow of the heat exchange medium. At the first fixed blade cascade 42, the air duct is set in a reduced manner. When the heat exchange medium passes through the first fixed blade, it is compressed by the air duct for initial acceleration, and then further accelerated to the speed of sound or supersonic speed under the high-speed rotation of the rotating blade cascade 43.

[0067] In the embodiment of the present application, the heater 40 further includes a plurality of partitions disposed in the shock wave heating channel 45, the plurality of partitions being used to separate a plurality of heating spaces, each of which is provided with a plurality of first fixed blades for constituting the first fixed blade grid 42, and a plurality of second fixed blades for constituting the second fixed blade grid 44. Although the heat exchange medium can achieve the purpose of heating after impacting the second fixed blade, the temperature increase is limited. In order to meet the actual needs of catalytic reforming, a plurality of heating spaces are separated by providing a plurality of partitions, so that the heat exchange medium passes through the plurality of heating spaces in the shock wave heating channel 45 in sequence. Through this multi-layer design, the heat exchange medium moves spirally along the shock wave heating channel 45 under the drive of the rotating blades, and repeatedly passes through the first fixed blade grid 42, the rotating blade grid 43, and the second fixed blade grid 44, thereby generating shock waves multiple times and gradually increasing the temperature until the requirement is met.

[0068] Specifically, refer to Figure 2 and Figure 3 The heater 40 is arranged in a circular shape as a whole, the shock wave heating channel surrounds the central axis of the heater 40, the first fixed blade 42, the rotating blade 43 and the second fixed blade 44 also surround the central axis, and the heater 40 also includes a rotor arranged through the central axis, and the rotor drives the rotating blade 43 to rotate around the central axis. The heat exchange medium flows in from the inlet of the outer shell 41, flows along the first fixed blade in the first heating space to the rotating blade 43, and is accelerated from subsonic speed to sonic speed or supersonic speed through the rotating blade 43, and then impacts the second fixed blade in the heating space and slows down to subsonic speed. In this process, part of the kinetic energy of the heat exchange medium is converted into internal energy, completing the first heating. The heat exchange medium after deceleration enters the bladeless area in the next heating space along the second fixed blade, and then flows along the annular bladeless area to the first fixed blade, and performs the second heating according to the above steps. Repeat the above process, the heat exchange medium enters from the inlet of the outer shell 41, and spirally moves along the shock wave heating channel 45 to the outlet of the outer shell 41. In this moving process, the heat exchange medium is repeatedly heated until it reaches the preset temperature. It should be noted that the inlet and the outlet of the outer shell 41 are respectively arranged at the front and rear sides of the outer shell 41 to correspond to the first fixed blade cascade 42 and the second fixed blade cascade 44 respectively.

[0069] Furthermore, the required preset temperature of the heat exchange medium entering the shell side of the second heat exchanger 52 is between 600-1200°C, and the specific temperature needs to be set according to the actual needs of catalytic reforming. The process of adjusting the temperature can be to change the number of heaters 40 in a working state, or to change the rotation speed of the rotating blade 43 to change the maximum speed of the heat exchange medium. The faster the speed of the heat exchange medium, the greater the kinetic energy, and the more heat energy is converted when impacting the second fixed blade.

[0070] In the embodiment of the present application, both the first stationary blade and the second stationary blade have a curved streamline profile.

[0071] In an embodiment of the present application, the installation angle of the first fixed blade is between 35° and 75°, the inlet angle of the first fixed blade is between 0° and 45°, and the outlet angle of the first fixed blade is between 35° and 75°; the installation angle of the second fixed blade is between 45° and 85°, the inlet angle of the second fixed blade is between 25° and 65°, and the outlet angle of the second fixed blade is between 25° and 65°.

[0072] In the embodiment of the present application, the rotating blade grid 43 includes a plurality of rotating blades, and each rotating blade has a curved profile facing its rotation direction.

[0073] In the embodiment of the present application, the installation angle of the rotating blade is between 10° and 80°, the inlet angle of the rotating blade is between 35° and 75°, and the outlet angle of the rotating blade is between 35° and 75°.

[0074] refer to Figure 4 , Figure 4 From left to right, there are the first fixed blade of the first fixed blade 42, the rotating blade of the rotating blade 43, and the second fixed blade of the second fixed blade 44. The heat exchange medium moves along the flow channel formed by the three. The angle settings of the first fixed blade, the rotating blade, and the second fixed blade are optimized to achieve effective heating of the heat exchange medium. Specifically, the specific angle settings of the first fixed blade, the rotating blade, and the second fixed blade can be optimized and selected according to the fluid dynamics requirements and the heating effect. By reasonably setting the installation angles of the first fixed blade, the rotating blade, and the second fixed blade, the heat exchange medium can flow smoothly between the rotating blade and the fixed blade, thereby effectively introducing or exporting the heat exchange medium into or out of the heating space. When selecting the installation angle, factors such as the speed and flow direction of the heat exchange medium, as well as the gap and shape between the blades, can be considered to ensure the best fluid dynamics performance and heat transfer effect.

[0075] To achieve the above objectives, the present application also provides a low-carbon catalytic reforming process, comprising:

[0076] S1: The heat exchange medium enters the shell side of the first heat exchanger 51 after being heated to a preset temperature by the shock wave;

[0077] S2: The feedstock oil and hydrogen are sequentially passed through multiple heating reaction units for catalytic reforming;

[0078] S3: heating the reaction unit to separate the first material flow and the second material flow;

[0079] S4: the first material flows through the shell side of the second heat exchanger 52 and enters the oil-gas separation tower 20, and the second material flows through the shell side of the fourth heat exchanger 54 and enters the oil-gas separation tower 20;

[0080] S5: The oil-gas separation tower 20 separates hydrogen and the third stream;

[0081] S6: The third material flows through the shell side of the third heat exchanger 53 and enters the stabilization tower 30;

[0082] S7: the stabilization tower 30 separates the fourth material stream and the fifth material stream. The fourth material stream re-enters the stabilization tower 30 only through the shell side of the fourth heat exchanger 54 , and the fifth material stream is discharged through the shell side of the third heat exchanger 53 .

[0083] In the embodiment of the present application, step S2 also includes: the crude oil passes through the second heat exchanger 52 and the first heat exchanger 51 of the first heating reaction unit in sequence and enters the first mixer 61 to mix with hydrogen, and then enters the reactor 10 of the first heating reaction unit after mixing.

[0084] In the embodiment of the present application, step S5 further includes: separating the unreacted feedstock oil and reintroducing it into the first mixer 61 .

[0085] In the embodiment of the present application, in step S1, the preset temperature is between 600-1200°C.

[0086] Specifically, the speed at which the heat exchange medium enters the shell side of the second heat exchanger 52 is between 30-100 m / s, and the speed at which the heat exchange medium flows out of the shell side of the second heat exchanger 52 is between 10-50 m / s; the speed at which the heat exchange medium enters the shock wave heating channel 45 is between 50-200 m / s, and the speed at which the heat exchange medium flows out of the shock wave heating channel 45 is between 50-200 m / s. Specifically, the air pressure at the inlet of the shock wave heating channel 45 is between 2.5-5 bar, and the temperature at the inlet is room temperature or the temperature of the heat exchange medium recovered by the waste heat recovery device.

[0087] In a specific embodiment of the present application:

[0088] Principle: After being pressurized by the first booster pump 81, the oil enters the second heat exchanger 52 and performs convection heat exchange with the first material flow after the reaction in the reactor 10; then it enters the first heat exchanger 51 of the first heating reaction unit to be heated to a preset temperature and enters the first mixer 61. At the same time, hydrogen also enters the first mixer 61 from the buffer tank 90, and after mixing, it enters the reactor 10 for reaction. In order to maintain sufficient temperature conditions, the number of heating reaction units is 3. In each heating reaction unit, a first heat exchanger 51 is provided in front of the reactor 10; the heat exchange medium enters the shock wave heating channel 45 of the heater 40 at a speed of 50-200m / s, the rotating blade 43 accelerates the heat exchange medium to supersonic speed, and then impacts the second fixed blade 44 to reduce the speed to subsonic speed to increase the temperature of the heat exchange medium. After the heat exchange medium is heated to the preset temperature, it enters the shell side of the first heat exchanger 51. The heat exchange medium after heat exchange enters the heater 40 of the next heating reaction unit along the pipeline, thereby achieving the purpose of recovering waste heat; the second stream discharged from the reactor 10 enters the fourth heat exchanger 54 for heat exchange and cooling, and the cooled second stream first enters the oil-gas separation tower 20 to separate the unreacted hydrogen, and the third stream discharged from the bottom of the oil-gas separation tower 20 is brought to the third heat exchanger 53 by the second booster pump 82 for heating and then enters the stabilization tower 30. The stabilization tower 30 separates the gaseous hydrocarbons and pentane dissolved in the reforming product from the top of the tower, and the reforming product produced at the bottom of the tower is cooled by the third heat exchanger 53 and then sent out of the device.

[0089] The following are specific examples and comparative examples of the present application.

[0090] Example 1

[0091] Taking a 2 million tons / year low-carbon catalytic reforming system as an example, the initial temperature of the crude oil is 360°C, the temperature of the crude oil after heating is 510°C, and the required heat load is 30,000KW. The first fixed blade 42 includes 46 first fixed blades, the second fixed blade 44 includes 46 second fixed blades, and the rotating blade 43 includes 92 rotating blades. The installation angle of the first fixed blade is 56.5°, the inlet angle is 1°, and the outlet angle is 49.9°; the installation angle of the second fixed blade is 75.52°, the inlet angle is 54.12°, and the outlet angle is 35.4°; the installation angle of the rotating blade is 74.7°, the inlet angle is 42.7°, and the outlet angle is 41.87. The rotating blade 43 rotates at a speed of 7500rpm, the heat exchange medium is air, the speed of air entering the heater 40 is 115m / s, and the air is heated from 25°C to 1000°C by the heater 40. The number of heaters 40 is six. The heating device has negligible carbon emissions.

[0092] Comparative Example 1

[0093] Taking the original catalytic reforming system with an annual capacity of 2 million tons as an example, the initial temperature of the crude oil is 3600°C, the temperature of the crude oil after heating is 510°C, the branch temperature difference does not exceed 10°C, the temperature in the radiation room does not exceed 800°C, the fuel used is methane, and the annual carbon emissions are approximately 15,000 tons / year.

[0094] Example 2

[0095] Taking a 1 million tons / year low-carbon catalytic reforming system as an example, the initial temperature of the crude oil is 360°C, the temperature of the crude oil after heating is 510°C, and the required heat load is 15,000KW. The first fixed blade 42 includes 44 first fixed blades, the second fixed blade 44 includes 44 second fixed blades, and the rotating blade 43 includes 88 rotating blades. The installation angle of the first fixed blade is 56.5°, the inlet angle is 1°, and the outlet angle is 49.9°; the installation angle of the second fixed blade is 75.52°, the inlet angle is 54.12°, and the outlet angle is 35.4°; the installation angle of the rotating blade is 74.7°, the inlet angle is 42.7°, and the outlet angle is 41.87. The rotating blade 43 rotates at a speed of 7500rpm, the heat exchange medium is air, the speed of air entering the heater 40 is 115m / s, and the air is heated from 25°C to 1000°C by the heater 40. The number of heaters 40 is three. The carbon emissions of this heating device are negligible.

[0096] Comparative Example 2

[0097] Taking 200,000 tons / year raw catalytic reforming as an example, the initial temperature of the crude oil is 360°C, the temperature of the crude oil after heating is 510°C, the branch temperature difference does not exceed 10°C, the temperature in the radiation room does not exceed 800°C, the fuel used is methane, and the annual carbon emissions are approximately 7,700 tons.

[0098] Through the above-mentioned embodiments and comparative examples, the low-carbon hydrocracking system of the present application not only achieves the purpose of catalytic reforming but also reduces the generation of carbon dioxide and sulfide, which is beneficial to environmental protection.

[0099] In the description of the present application, it should be understood that the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of the features. In the description of the present application, "plurality" means at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0100] In this application, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like 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, an electrical connection, or communication with each other; it can be a direct connection, or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0101] In the description of this specification, the description with reference to the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0102] Although the embodiments of the present application have been shown and described above, it can be understood that the above embodiments are exemplary and cannot be understood as limitations on the present application. Ordinary technicians in this field can change, modify, replace and modify the above embodiments within the scope of the present application.

Claims

1. A low-carbon catalytic reforming system, characterized in that: It includes a heating reaction module and a separation module; The heating reaction module comprises a reactor (10), a heater (40) and a first heat exchanger (51); the heater (40) is formed with a shock wave heating channel (45) for shock wave heating of a heat exchange medium; the tube side of the first heat exchanger (51) is connected to the reactor (10); the shell side of the first heat exchanger (51) is connected to the heater (40); and the crude oil undergoes a catalytic reforming reaction in the reactor (10); The separation module comprises an oil-gas separation tower (20) and a stabilization tower (30); the oil-gas separation tower (20) is connected to the reactor (10) and is used to separate hydrogen from a first stream flowing out of the reactor (10); the stabilization tower (30) is connected to the oil-gas separation tower (20) and is used to separate gaseous hydrocarbons, pentane and reforming products from a third stream flowing out of the oil-gas separation tower (20).

2. The low-carbon catalytic reforming system according to claim 1, characterized in that: The heating reaction module comprises a plurality of heating reaction units connected in sequence, each of the heating reaction units comprises a reactor (10), a first heat exchanger (51) and at least one heater (40), and the reactor (10) of the last heating reaction unit is connected to the oil-gas separation tower (20).

3. The low-carbon catalytic reforming system according to claim 2, characterized in that: The system further comprises a second heat exchanger (52), wherein the second heat exchanger (52) is arranged upstream of the first heating reaction unit, and the shell side of the second heat exchanger (52) is connected to the reactor (10) of the last heating reaction unit.

4. The low-carbon catalytic reforming system according to claim 2, characterized in that: The separation module also includes a third heat exchanger (53), the tube side of the third heat exchanger (53) correspondingly connects the outlet of the oil-gas separation tower (20) and the inlet of the stabilization tower (30), and the shell side of the third heat exchanger (53) connects the outlet of the stabilization tower (30) for cooling the reforming product.

5. The low-carbon catalytic reforming system according to claim 4, characterized in that: The separation module also includes a fourth heat exchanger (54), the tube side of the fourth heat exchanger (54) correspondingly connects the outlet and the inlet of the stabilization tower (30), and the shell side of the third heat exchanger (53) connects the outlet of the reactor (10) of the last heating reaction unit and the inlet of the oil-gas separation tower (20).

6. The low-carbon catalytic reforming system according to claim 1, characterized in that: The heater (40) comprises an outer shell (41), a first fixed blade grid (42), a rotating blade grid (43), a second fixed blade grid (44) and a rotor. The outer shell (41) forms a shock wave heating channel (45). The cross section of the shock wave heating channel (45) is annular. The first fixed blade grid (42), the rotating blade grid (43) and the second fixed blade grid (44) are sequentially arranged in the shock wave heating channel (45) from front to back. The rotor is arranged on the outer shell (41) and is used to drive the rotating blade grid (43) to rotate in the shock wave heating channel (45).

7. The low-carbon catalytic reforming system according to claim 6, characterized in that: The heater (40) further comprises a plurality of partitions arranged in the shock wave heating channel (45), the plurality of partitions being used to separate a plurality of heating spaces, each of the heating spaces being provided with a plurality of first fixed blades for constituting the first fixed blade grid (42), and a plurality of second fixed blades for constituting the second fixed blade grid (44).

8. The low-carbon catalytic reforming system according to claim 7, characterized in that: The first stationary blade and the second stationary blade each have a curved streamline profile.

9. The low-carbon catalytic reforming system according to claim 8, characterized in that: The installation angle of the first fixed blade is between 35° and 75°, the inlet angle of the first fixed blade is between 0° and 45°, and the outlet angle of the first fixed blade is between 35° and 75°; the installation angle of the second fixed blade is between 45° and 85°, the inlet angle of the second fixed blade is between 25° and 65°, and the outlet angle of the second fixed blade is between 25° and 65°.

10. The low-carbon catalytic reforming system according to claim 7, characterized in that: The rotating blade grid (43) comprises a plurality of rotating blades, each of which has a curved profile facing its rotation direction.

11. The low-carbon catalytic reforming system according to claim 10, characterized in that: The installation angle of the rotating blade is between 10° and 80°, the inlet angle of the rotating blade is between 35° and 75°, and the outlet angle of the rotating blade is between 35° and 75°.

12. A low-carbon catalytic reforming process, characterized in that: The process comprises: S1: The heat exchange medium enters the shell side of the first heat exchanger (51) after being heated to a preset temperature by the shock wave; S2: The feedstock oil and hydrogen are sequentially passed through multiple heating reaction units for catalytic reforming; S3: the heating reaction unit splits out a first material stream and a second material stream; S4: the first material flow passes through the shell side of the second heat exchanger (52) and enters the oil-gas separation tower (20), and the second material flow passes through the shell side of the second heat exchanger (52) and enters the oil-gas separation tower (20); S5: the oil-gas separation tower (20) separates hydrogen and a third stream; S6: the third material flows through the shell side of the third heat exchanger (53) and enters the stabilization tower (30); S7: The stabilization tower (30) separates a fourth material stream and a fifth material stream, the fourth material stream re-enters the stabilization tower (30) only through the shell side of the fourth heat exchanger (54), and the fifth material stream is discharged through the shell side of the third heat exchanger (53).

13. The low-carbon catalytic reforming process according to claim 12, characterized in that: The step S2 also includes: the crude oil is heated and mixed with hydrogen in the second heat exchanger (52) and the first heat exchanger (51) of the first heating reaction unit in sequence, and then enters the reactor (10) of the first heating reaction unit after mixing.

14. The low-carbon catalytic reforming process according to claim 12, characterized in that: The step S5 further comprises: separating the unreacted raw oil and reintroducing it into the first mixer (61).

15. The low-carbon catalytic reforming process according to claim 12, characterized in that: In the step S1, the preset temperature is between 600-1200°C.

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