Diesel oil low-pressure mesoscopic fixed bed hydrocracking method and system
By forming micron-scale oil beads and hydrogen bubbles in the mesoscopic tank, the oil and gas contact area is expanded, and the problems of high-pressure hydrogen consumption and high energy consumption in the diesel hydrocracking process are solved, and low-pressure hydrocracking is achieved to achieve the purpose of cleaning and safe production .
Patent Information
- Application Number
- CN202411351008.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-26
- Publication Date
- 2024-12-31
AI Technical Summary
The existing diesel hydrocracking process consumes a large amount of hydrogen at high pressure, has high energy consumption, and has heavy environmental pollution, making it difficult to achieve low-carbon green production.
Low-pressure mesoscopic hydrogenation technology is adopted to enable diesel and hydrogen gas to form micron-scale oil beads and hydrogen bubbles in the mesoscopic tank, convert kinetic energy into surface energy, expand the oil and gas contact area, improve mass transfer efficiency, and realize low-pressure hydrocracking reaction.
Diesel hydrocracking is achieved under low pressure conditions of 1 to 6Mpa, reducing reaction pressure, saving energy and consumption, improving the hydrogen supply capacity of the catalyst bed, and achieving clean and safe production.
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Figure CN119215786A_ABST
Abstract
Description
Technical Field
[0001] The invention relates to the technical field of petroleum resource processing and utilization and efficient lightweight treatment, and in particular to a diesel low-pressure mesoscopic fixed-bed hydrocracking method and system. Background Art
[0002] Diesel hydrocracking process is the most mature and widely used secondary processing technology for oil refining. It has many advantages such as strong raw material adaptability, flexible processing scheme, high liquid product yield, and good product quality. It has become a key clean production technology for modern refining enterprises to directly produce clean oil products and high-quality chemical raw materials from inferior and heavy raw materials. Diesel hydrocracking generally uses a fixed bed reactor. Under high temperature and high pressure hydrogen conditions, it carries out hydrocracking reaction with a matching catalyst to convert diesel into high-quality fuel oil, catalytic reforming raw materials and high-quality chemical raw materials. The operating pressure is usually around 8-12Mpa.
[0003] The fixed-bed hydrogenation of diesel consumes a large amount of hydrogen, but the solubility of hydrogen in diesel is low and cannot meet the requirements of the hydrocracking reaction. Therefore, the existing technology usually increases the solubility of hydrogen in oil by increasing the reaction pressure to ensure that the raw oil and hydrogen pass through the catalyst bed for hydrocracking reaction. However, increasing the reaction pressure is accompanied by higher energy investment, land occupation, emissions, costs, energy consumption, and consumption of refining equipment. With the continuous advancement of energy conservation, emission reduction, and clean production, it is an inevitable trend for refining enterprises to adopt new processes and technologies to achieve efficient, low-carbon, and green production. Summary of the invention
[0004] The purpose of the present invention is to provide a diesel low-pressure mesoscopic fixed bed hydrocracking method and system. Aiming at the current diesel high-pressure hydrocracking process, a new mesoscopic hydrogenation technology is adopted to make diesel undergo hydrocracking reaction at a low pressure of 1 to 6 MPa, so as to achieve the purpose of reducing reaction pressure, energy saving and consumption reduction, clean and safe production. The diesel low-pressure mesoscopic fixed bed hydrocracking method and system are based on the law of energy conversion and conservation, and use the independently developed mesoscopic pool to make diesel and hydrogen enter the mesoscopic pool under certain conditions. In the mesoscopic pool, the moving hydrogen flow hits the diesel, so that both oil and gas are in the form of micron-sized oil droplets and hydrogen bubbles, forming a mesoscopic state. In this process, the kinetic energy of hydrogen is converted into the surface energy of oil droplets and hydrogen bubbles, so that the oil and gas contact area is expanded by more than 1,000 times, and the mass transfer efficiency between oil and gas is improved. By changing the hydrogen supply mode, the mesoscopic state material increases the hydrogen supply capacity of the catalyst bed catalytic hydrocracking reaction, and realizes the diesel hydrocracking reaction in the fixed bed reactor under low pressure conditions, so as to achieve the purpose of reducing the reaction pressure.
[0005] The present invention provides a diesel low-pressure mesoscopic fixed-bed hydrocracking method, wherein the low pressure range is 1-6 MPa, comprising:
[0006] S1, obtaining diesel feedstock and hydrogen for hydrocracking;
[0007] S2, the diesel feedstock and the hydrogen form one or more mesoscopic state products after passing through one or more mesoscopic cells; wherein the mesoscopic state represents a coupling state of micron particles formed by the energy exchange of the diesel and hydrogen phases through the mesoscopic cells; or under different operating pressures and temperatures, for different flow rates, densities and viscosities of the gas and liquid phases, gas-liquid mixing is performed in a mesoscopic cell with kinetic energy to form a two-phase coupling state of gas-liquid phases with a scale of 1um to 500um, including bubbles and oil microparticles with or without nanoparticles; the mesoscopic cell has a specific cavity, in which a variety of components are built-in and has gas-liquid crushing and damping kinetic energy conversion functions;
[0008] S3, the mesoscopic product enters the mesoscopic reactor and passes through the catalyst bed in the form of a mesoscopic state to complete the hydrocracking reaction;
[0009] S4, post-processing the materials after the hydrocracking reaction.
[0010] Preferably, the S1 comprises:
[0011] S11, obtaining diesel raw materials;
[0012] S12, dividing the hydrogen used for the hydrocracking reaction into two paths, wherein the volume ratio of the first path of hydrogen is 5-20% of the total hydrogen, and the volume ratio of the second path of hydrogen is 80-95% of the total hydrogen; wherein the first path of hydrogen and the second path of hydrogen are used to form a first mesoscopic product and a second mesoscopic product, respectively;
[0013] Preferably, S2 includes:
[0014] S21, the diesel feedstock is pumped by the feedstock pump (1), preheated to a set temperature by the first heat exchange system (3), and then enters the first mesoscopic pool (5) together with the first hydrogen gas preheated to the set temperature, wherein the diesel feedstock and the first hydrogen gas form a first mesoscopic product in the first mesoscopic pool (5);
[0015] S22, the first mesoscopic product enters the second mesoscopic pool (6), the second mesoscopic pool (6) is arranged at the front or rear of the heating furnace (7), or at the entrance of the first mesoscopic reactor (8), or at the entrance of the second mesoscopic reactor (10), and at the same time, the second hydrogen gas preheated to a set temperature enters the second mesoscopic pool (6), and the conversion of kinetic energy to surface energy between hydrogen and diesel is completed in the second mesoscopic pool (6), so that the hydrogen and diesel are converted into the second mesoscopic product formed by hydrogen bubbles and oil droplets of set size.
[0016] S23, the one or more mesoscopic products enter the first mesoscopic reactor (8) and then pass through the first catalyst bed (9A) in the form of a mesoscopic state to undergo a hydrotreating reaction;
[0017] S24, one or more mesoscopic hydrogenation products from the first mesoscopic reactor (8) enter the second mesoscopic reactor 10 and pass through the second catalyst bed (11A) in the mesoscopic form to complete the hydrocracking reaction.
[0018] Preferably, S3 includes:
[0019] S31, sending the preheated second mesoscopic product into one or more first catalyst beds (9A) provided in the first mesoscopic reactor (8);
[0020] S32, the reacted material in the first mesoscopic reactor (8) is kept in a mesoscopic state and passes through the first catalyst bed (9A) for a hydrogenation refining reaction;
[0021] S33, the product after the hydrogenation reaction through the first catalyst bed (9A) is kept in a mesoscopic state and sent to one or more second catalyst beds (11A) arranged in the second mesoscopic reactor (10);
[0022] S34, the reacted material in the second mesoscopic reactor (10) is maintained in a mesoscopic state and passes through the second catalyst bed (11A) to undergo a hydrocracking reaction.
[0023] Preferably, S4 includes:
[0024] S41, the material after the hydrocracking reaction leaves the mesoscopic reactor (10) and enters the gas-liquid separation system (12) to undergo gas-liquid separation to form a liquid phase material and a hydrogen-rich gas phase material;
[0025] S42, the liquid phase material enters the fractionation system for fractionation, and the corresponding fraction exits the device;
[0026] S43, the hydrogen-rich gas phase material enters the circulating hydrogen system for treatment and then is recycled.
[0027] Preferably, the manner in which the second mesoscopic product enters the first mesoscopic reactor (8) and the second mesoscopic reactor (10) is determined by engineering design based on the overall plan of the process device, and is one of the methods of top-in and bottom-out or bottom-in and top-out.
[0028] Preferably, the first catalyst bed (9A) of the S32 is loaded with a first catalyst, which is mainly a hydrotreating catalyst, and then loaded into the first catalyst bed (9A) according to a first catalyst loading scheme.
[0029] Preferably, the second catalyst bed (11A) of the S34 is loaded with a second catalyst, wherein the second catalyst is mainly a hydrocracking catalyst, and then loaded into the second catalyst bed (11A) according to a second catalyst loading scheme.
[0030] The second aspect of the present invention is to provide a diesel low-pressure mesoscopic fixed-bed hydrocracking system, comprising:
[0031] A raw material delivery pump (1), a hydrogen compressor (2), a first heat exchange system (3), a second heat exchange system (4), a first mesoscopic pool (5), a second mesoscopic pool (6), a heating furnace (7), a first mesoscopic reactor (8), a second mesoscopic reactor (10) and a gas-liquid separation system (12); wherein:
[0032] The hydrogen raw material is pressurized to the process pressure by the hydrogen compressor (2), and the hydrogen is divided into two paths, the volume ratio of the hydrogen in the first path is 5-15% of the total hydrogen, and the volume ratio of the hydrogen in the second path is 80-95% of the total hydrogen;
[0033] The diesel feedstock is pumped by the feedstock delivery pump (1), preheated to a set temperature by the first heat exchange system (3), and then enters the first mesoscopic pool (5) together with the first hydrogen gas preheated to the set temperature. In the first mesoscopic pool (5), the diesel feedstock and the first hydrogen gas form a first mesoscopic product.
[0034] The first mesoscopic product enters the second mesoscopic pool (6), which is arranged at the front or rear of the heating furnace (7), or at the entrance of the first mesoscopic reactor (8), or at the entrance of the second mesoscopic reactor (10). At the same time, the second hydrogen gas preheated to a set temperature enters the second mesoscopic pool (6), and the conversion of kinetic energy between hydrogen and diesel into surface energy is completed in the second mesoscopic pool (6), so that the hydrogen and diesel are converted into the second mesoscopic product formed by hydrogen bubbles and oil droplets of 1 to 500 μm.
[0035] The second mesoscopic product enters the heating furnace (7) and is heated to a predetermined temperature before entering the mesoscopic reactor (8); the mesoscopic reactor (8) comprises one or more catalyst beds (9A); the reacted material in the mesoscopic reactor (8) is kept in the mesoscopic state and undergoes a hydrotreating reaction through the cracking catalyst loaded in the catalyst bed (9A);
[0036] The hydrogenation reaction product passing through the first catalyst bed (9) enters the second mesoscopic reactor (10); the second mesoscopic reactor (10) comprises one or more second catalyst beds (11A); the material to be reacted in the second mesoscopic reactor (10) is kept in a mesoscopic state and undergoes a hydrocracking reaction through the second catalyst loaded in the second catalyst bed (11A);
[0037] The material after the hydrocracking reaction leaves the second mesoscopic reactor (10) and enters the gas-liquid separation system (12) for gas-liquid separation. The liquid phase material enters the fractionation system for fractionation and the corresponding fraction is discharged from the device. The hydrogen-rich gas phase material enters the circulating hydrogen system for treatment and recycling.
[0038] Preferably, according to different operating pressures, different hydrogen-oil ratios and different liquid viscosities, the aperture of the hydrogen radiation channel, the geometric parameters of the longitudinal and transverse gas pulverizers, the geometric parameters of the disruptor and the geometric parameters of the gas-liquid mixing separator are adjusted to determine the structural form of the first mesoscopic pool (5) and the second mesoscopic pool (6).
[0039] Preferably, the first mesoscopic pool (5) and the second mesoscopic pool (6) are GC mesoscopic pool I, GC mesoscopic pool II or GC mesoscopic pool III, respectively; wherein:
[0040] The internal structural parts of the GC mesoscopic pool I include a shell, an oil inlet hole (11), a hydrogen radiation channel (12), a gas pulverizer (13) and a carrier plate flow guide splitter (14); applicable conditions include: operating pressure ≤ 2MPa; hydrogen-oil ratio within 800:1; catalyst layer loading, mixed loading, and mesoscopic state injection can be either upper or lower;
[0041] The internal structural parts of the GC mesoscopic cell II include a component shell (20), an oil inlet elliptical hole (21), a hydrogen radiation channel (22), a gas pulverizer (23), a segmentation disruptor (24) and a carrier plate flow diverter (25); applicable conditions include: operating pressure ≤ 3MPa / 5MPa; hydrogen-oil ratio within 1200:1; catalyst layer loading, mixed loading, and mesoscopic state injection upper and lower ports are all possible;
[0042] The internal structural parts of the GC mesoscopic pool III include a component shell, an oil inlet groove hole (31), a hydrogen radiation channel (32), a gas pulverizer (33), a disruptor (34) and a carrier plate flow guide splitter (35). The anti-backflow damper (30) has 7 0 ~12 0 The applicable conditions include: operating pressure ≤5MPa / 8MPa; hydrogen-to-oil ratio within 1500:1; catalyst layer loading, mixed loading, and mesoscopic injection can be performed at the upper and lower ports.
[0043] Beneficial effects of the method and system of the present invention:
[0044] In view of the current high-pressure diesel hydrocracking process, a new mesoscopic hydrogenation technology is adopted to make diesel undergo hydrocracking reaction at a low pressure of 1 to 6 MPa, so as to achieve the purpose of reducing reaction pressure, energy saving and consumption reduction, clean and safe production. The diesel low-pressure mesoscopic fixed bed hydrocracking method and system is based on the law of energy conversion and conservation, and uses the independently developed mesoscopic pool to allow diesel and hydrogen to enter the mesoscopic pool under certain conditions. In the mesoscopic pool, the moving hydrogen flow hits the diesel, so that both oil and gas are in the form of micron-sized oil droplets and hydrogen bubbles, forming a mesoscopic state. In this process, the kinetic energy of hydrogen is converted into the surface energy of oil droplets and hydrogen bubbles, which expands the oil-gas contact area by more than 1,000 times and improves the mass transfer efficiency between oil and gas. By changing the hydrogen supply mode, the mesoscopic material increases the hydrogen supply capacity of the catalyst bed catalytic hydrocracking reaction, and realizes the diesel hydrocracking reaction in the fixed bed reactor under low-pressure conditions, so as to achieve the purpose of reducing the reaction pressure. BRIEF DESCRIPTION OF THE DRAWINGS
[0045] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the related technologies, the drawings required for use in the specific embodiments or the related technical descriptions will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.
[0046] Figure 1 This is a schematic diagram of the system structure of a diesel low-pressure mesoscopic fixed-bed hydrocracking system according to an embodiment of the present invention.
[0047] FIG. 2( a ) and FIG. 2( b ) are two schematic structural diagrams of a mesoscopic cell I of model JG-GC-01 provided according to an embodiment of the present invention.
[0048] FIG. 3( a ) and FIG. 3( b ) are two schematic structural diagrams of a mesoscopic cell II of model JG-GC-02 provided according to an embodiment of the present invention.
[0049] FIG. 4( a ) and FIG. 4( b ) are two schematic diagrams of the structure of a mesoscopic cell II of model JG-GC-02 provided according to an embodiment of the present invention. DETAILED DESCRIPTION
[0050] The technical solution of the present invention will be described clearly and completely below in conjunction with the accompanying drawings. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.
[0051] In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention 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 limiting the present invention. In addition, the terms "first", "second", and "third" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance.
[0052] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, 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 the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.
[0053] This embodiment provides a diesel low-pressure mesoscopic fixed-bed hydrocracking system, wherein the low pressure range is 1-6 MPa, and comprises:
[0054] S1, obtaining diesel feedstock and hydrogen for hydrocracking;
[0055] As a preferred embodiment, the S1 includes:
[0056] S11, obtaining diesel raw materials;
[0057] S12, dividing the hydrogen used for hydrocracking into two paths, wherein the volume ratio of the first path of hydrogen is 5-20% of the total hydrogen, and the volume ratio of the second path of hydrogen is 80-95% of the total hydrogen; wherein the first path of hydrogen and the second path of hydrogen are used to form a first mesoscopic product and a second mesoscopic product, respectively;
[0058] S2, the diesel feedstock passes through one or more mesoscopic cells to form one or more mesoscopic products;
[0059] As a preferred embodiment, the S2 includes:
[0060] S21, the diesel feedstock is preheated to a set temperature by the first heat exchange system 3 and the first hydrogen gas preheated to a set temperature enters the first mesoscopic pool 5 respectively, and the diesel feedstock and the first hydrogen gas form a first mesoscopic product in the first mesoscopic pool 5;
[0061] S22, the first mesoscopic product enters the second mesoscopic pool 6, the second mesoscopic pool 6 is located at the front side or the rear side of the heating furnace 7, or at the entrance of the first mesoscopic reactor 8, or at the entrance of the second mesoscopic reactor 10, and the second hydrogen gas preheated to a set temperature enters the second mesoscopic pool 6, and the conversion of kinetic energy to surface energy between hydrogen and diesel is completed in the second mesoscopic pool 6, so that the hydrogen and diesel are converted into the second mesoscopic product formed by hydrogen bubbles and oil droplets of set sizes;
[0062] S23, one or more mesoscopic products enter the first mesoscopic reactor 8 and then undergo hydrogenation reaction in the form of a mesoscopic state through the first catalyst bed 9A;
[0063] S24, one or more mesoscopic hydrogenation products passing through the first mesoscopic reactor 8 enter the second mesoscopic reactor 10 and pass through the second catalyst bed 11A in the mesoscopic state to complete the hydrogenation reaction.
[0064] As a preferred implementation, S3 includes:
[0065] S31, sending the preheated second mesoscopic product into one or more first catalyst beds 9A provided in the first mesoscopic reactor 8;
[0066] S32, the reacted material in the first mesoscopic reactor 8 is kept in a mesoscopic state and passed through the first catalyst bed 9A for a hydrotreating reaction;
[0067] S33, sending one or more mesoscopic hydrogenation products passing through the first mesoscopic reactor 8 to one or more second catalyst beds 11A disposed in the second mesoscopic reactor 10;
[0068] S34, the materials to be reacted in the second mesoscopic reactor 10 are kept in a mesoscopic state and pass through the second catalyst bed 11A to undergo a hydrocracking reaction.
[0069] S4, post-processing the materials after the hydrocracking reaction.
[0070] As a preferred implementation, the S4 includes:
[0071] S41, the material after the hydrogenation reaction leaves the second mesoscopic reactor 10 and enters the gas-liquid separation system 12 for gas-liquid separation to form a liquid phase material and a hydrogen-rich gas phase material;
[0072] S42, the liquid phase material enters the fractionation system for fractionation, and the corresponding fraction exits the device;
[0073] S43, the hydrogen-rich gas phase material enters the circulating hydrogen system for treatment and then is recycled.
[0074] As a preferred embodiment, the way in which the second mesoscopic product enters the first mesoscopic reactor 8 is determined by engineering design based on the overall plan of the process device, and is one of the ways of entering from top to bottom or entering from bottom to top.
[0075] As a preferred embodiment, the way in which one or more mesoscopic hydrogenation products from the first mesoscopic reactor 8 enter the second mesoscopic reactor 10 is determined by engineering design based on the overall plan of the process unit, and is one of the top-in and bottom-out or bottom-in and top-out methods.
[0076] As a preferred embodiment, the first catalyst is loaded in the first catalyst bed 9 of S32. The first catalyst is mainly a hydrogenation refining catalyst. In combination with the product quality index control requirements and the reaction intensity of each functional catalyst under the mesoscopic hydrogenation reaction conditions, the grading and matching scheme of each functional catalyst suitable for low-pressure 1-6MPa diesel hydrogenation is determined, and then the first catalyst is loaded.
[0077] As a preferred embodiment, the second catalyst is loaded in the second catalyst bed 11A of S33. The second catalyst is mainly a hydrocracking catalyst. In combination with the product quality index control requirements and the reaction intensity of each functional catalyst under the mesoscopic hydrogenation reaction conditions, the grading and matching scheme of each functional catalyst suitable for low-pressure 1-6MPa diesel hydrogenation is determined, and then the second catalyst is loaded.
[0078] As a preferred implementation, this embodiment adopts diesel low-pressure mesoscopic fixed-bed hydrocracking technology to meet the various types and types of catalysts and loading methods of existing diesel fixed-bed hydrocracking processes (4-10Mpa); at the same time, it meets the existing diesel fixed-bed hydrocracking agent main agent mixed loading method.
[0079] In this embodiment, the mesoscopic state represents a coupling state of gas-liquid two-phases through energy exchange in a mesoscopic pool to form micron particles as a mesoscopic state of gas-liquid two-phase mixing; or under different operating and temperature conditions, for different flow rates, densities and viscosities of gas and liquid phases, gas-liquid mixing is performed in a mesoscopic pool with kinetic energy to form a coupled physical state of gas-liquid two-phase mixing with a scale of 1um to 500um, containing or not containing bubbles of nanoparticles, and liquid microparticles in molecular state or micron-sized crystals; wherein the mesoscopic pool is a gas-liquid crushing and damping kinetic energy conversion device with multiple components built into a specific cavity to form a mesoscopic state;
[0080] As a preferred embodiment, during the physical and chemical reaction process, the diesel and hydrogen phases exchange energy through a mesoscopic pool (a gas-liquid crushing and damping kinetic energy conversion device with a specific function and built-in multiple components in a specific cavity) to form a coupled state of micron particles. Or under different operating pressures and temperatures, for different flow rates, densities, and viscosities of the gas and liquid phases, gas-liquid mixing is performed in a mesoscopic pool with kinetic energy to form a two-phase coupled state of gas-liquid bubbles (or nanoparticles) with a scale of 1um to 500um and oil microparticles, which is called a mesoscopic state.
[0081] like Figure 1 As shown, this embodiment also provides a system for low-pressure mesoscopic hydrocracking of diesel, comprising:
[0082] A raw material delivery pump 1, a hydrogen compressor 2, a first heat exchange system 3, a second heat exchange system 4, a first mesoscopic pool 5, a second mesoscopic pool 6, a heating furnace 7, a first mesoscopic reactor 8, a second mesoscopic reactor 10 and a gas-liquid separation system 12; wherein:
[0083] The hydrogen raw material is pressurized to the process pressure by the hydrogen compressor 2, and the hydrogen is divided into two paths, the volume ratio of the first path hydrogen is 5-20% of the total hydrogen, and the volume ratio of the second path hydrogen is 80-95% of the total hydrogen;
[0084] The diesel feedstock is pumped by the feedstock delivery pump 1, and after being preheated to a set temperature by the first heat exchange system 3, it and the first hydrogen gas preheated to a set temperature enter the first mesoscopic pool 5 respectively, and the diesel feedstock and the first hydrogen gas form a first mesoscopic product in the first mesoscopic pool 5;
[0085] The first mesoscopic product enters the second mesoscopic pool 6, which is arranged at the front or rear side of the heating furnace 7, or at the entrance of the first mesoscopic reactor 8, or at the entrance of the second mesoscopic reactor 10. At the same time, the second hydrogen gas preheated to the set temperature enters the second mesoscopic pool 6, and the conversion of kinetic energy to surface energy between hydrogen and diesel is completed in the second mesoscopic pool 6, so that hydrogen and diesel are converted into second mesoscopic products formed by hydrogen bubbles and oil droplets of 1 to 500 μm; the second mesoscopic pool 6 can be placed in multiple positions ( Figure 1 );
[0086] The second mesoscopic product enters the first mesoscopic reactor 8. In this embodiment, the first mesoscopic reactor 8 is a fixed bed mesoscopic reactor. Of course, other types of mesoscopic reactors can also be selected, all within the scope of protection of the present invention; the first mesoscopic reactor 8 includes one or more first catalyst beds 9A; the reacted material in the first mesoscopic reactor 8 is kept in the mesoscopic state and undergoes a hydrogenation refining reaction through the first catalyst loaded in the first catalyst bed 9A;
[0087] The second mesoscopic hydrogenation product enters the second mesoscopic reactor 10 through the first catalyst bed 9A. In this embodiment, the second mesoscopic reactor 10 is a fixed bed mesoscopic reactor. Of course, other types of mesoscopic reactors can also be selected, all within the scope of protection of the present invention; the second mesoscopic reactor 10 includes one or more second catalyst beds 11A; the reacted material in the second mesoscopic reactor 10 is kept in the mesoscopic state and undergoes a hydrocracking reaction through the second catalyst loaded in the second catalyst bed 11A;
[0088] The material after the hydrogenation reaction leaves the second mesoscopic reactor 10 and enters the gas-liquid separation system 12 for gas-liquid separation. The liquid phase material enters the fractionation system for fractionation, and the corresponding fraction exits the device. The hydrogen-rich gas phase material enters the circulating hydrogen system for treatment and recycling.
[0089] As a preferred embodiment, the feed form of the first mesoscopic reactor 8 is determined to be upper feed and lower discharge or lower feed and upper discharge according to the raw material properties and product plan, and the feed state is a mesoscopic state.
[0090] As a preferred embodiment, the feeding form of the second mesoscopic reactor 10 is determined to be upper feeding and lower discharging or lower feeding and upper discharging according to the raw material properties and product plan, and the feeding state is a mesoscopic state.
[0091] As a preferred embodiment, the first mesoscopic pool 5 and the second mesoscopic pool 6 are Figure 1 "JG-GC" is used in the representation; the first mesoscopic pool 5 and the second mesoscopic pool 6 are both composed of a shell, a beveled circular channel, a hydrogen radiation channel, a longitudinal and transverse gas pulverizer, an interrupter, a gas-liquid mixing divider and a guide plate; the suitable operating pressure is 1-6Mp, the hydrogen-to-oil ratio is 500-1500:1, and the processed raw oil is diesel.
[0092] As a preferred embodiment, the aperture of the hydrogen radiation channel, the geometric parameters of the longitudinal and transverse gas pulverizers, the geometric parameters of the disruptor, and the geometric parameters of the gas-liquid mixing divider are adjusted according to different operating pressures, different hydrogen-to-oil ratios, and different liquid viscosities, so as to determine the specifications of the "JG-GC" device. The determined "JG-GC" is excited by gas kinetic energy to form a mesoscopic state of gas-liquid two-phase mixing that meets the requirements of the operating conditions. The mesoscopic state reactants to be reacted enter the mesoscopic reactor 8 equipped with a refined catalyst for physical and chemical reactions.
[0093] As a preferred embodiment, the first mesoscopic pool 5 and the second mesoscopic pool 6 are respectively GC mesoscopic pool I, GC mesoscopic pool II or GC mesoscopic pool III; wherein:
[0094] 1. As shown in Figure 2(a) and Figure 2(b), the GC mesoscopic cell I is of model JG-GC-01, wherein the internal structural parts include a shell, an oil inlet hole 11 (in the form of an oil distribution plate), a hydrogen radiation channel 12 (in the form of a gas distribution plate), a gas pulverizer 13 and a carrier plate flow guide divider 14 (in the form of a current carrier plate); applicable conditions include: operating pressure ≤ 2MPa; hydrogen-oil ratio within 800:1; catalyst layer loading, mixed loading, mesoscopic injection upper and lower ports are all possible; Figure 2(a) and Figure 2(b) are different in the position and method of hydrogen and diesel entering the mesoscopic cell;
[0095] 2. As shown in 3(a) and 3(b), the GC mesoscopic cell II is of model JG-GC-02, wherein the internal structural parts include a component shell 20, an oil inlet elliptical hole 21 (in the form of an oil distribution plate), a hydrogen radiation channel 22 (in the form of a gas distribution plate), a gas pulverizer 23, a segmentation disruptor 24 and a carrier plate flow guide divider 25 (in the form of a current carrier plate); applicable conditions include: operating pressure ≤3MPa / 5MPa; hydrogen-oil ratio within 1200:1; catalyst layer loading, mixed loading, mesoscopic state injection upper and lower ports are all possible; wherein FIG3(a) and FIG3(b) are different in the shape of the circular hole of the oil distribution plate, and the number and distribution of the oil distribution plates are different;
[0096] 3. As shown in Figure 4(a) and Figure 4(b), the GC mesoscopic pool III is of model JG-GC-03, wherein the internal structural parts include a component shell, an anti-backflow damper 30 (with 7 0 ~12 0 The invention relates to a catalyst system comprising: a flow guide angle 301), an oil inlet groove hole 31 (in the form of an oil distribution plate), a hydrogen radiation channel 32 (in the form of a gas distribution plate), a gas pulverizer 33, an interrupter 34 and a carrier plate flow guide divider 35 (in the form of a current carrier plate); applicable conditions include: operating pressure ≤5MPa / 8MPa; hydrogen-oil ratio within 1500:1; catalyst layer loading, mixed loading, and mesoscopic injection at the upper and lower ports are both possible; the difference between FIG4(a) and FIG4(b) is that the distribution of anti-backflow resistance is different.
[0097] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with 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 embodiments of the present invention.
Claims
1. A diesel low-pressure mesoscopic fixed-bed hydrocracking method, characterized in that: The low pressure range is 1-6MPa, including: S1, obtaining diesel feedstock and hydrogen for hydrocracking; S2, the diesel feedstock and the hydrogen form a mesoscopic state product after passing through one or more mesoscopic cells; wherein the mesoscopic state represents a coupling state of micron particles formed by the energy exchange of the diesel and hydrogen phases through the mesoscopic cells; or under different operating pressures and temperatures, for different flow rates, densities and viscosities of the gas and liquid phases, gas-liquid mixing is performed in a mesoscopic cell with kinetic energy to form a two-phase coupling state of gas-liquid phases with a scale of 1um to 500um, including bubbles and oil microparticles with or without nanoparticles; the mesoscopic cell has a specific cavity, in which a variety of components are built-in and has gas-liquid crushing and damping kinetic energy conversion functions; S3, the mesoscopic product enters the mesoscopic reactor and passes through the catalyst bed in the form of a mesoscopic state to complete the hydrocracking reaction; S4, post-processing the materials after the hydrocracking reaction.
2. A diesel low-pressure mesoscopic fixed-bed hydrocracking method according to claim 1, characterized in that: The S1 includes: S11, obtaining diesel raw materials; S12, dividing the hydrogen used for hydrogenation into two paths, the volume ratio of the first path of hydrogen is 5-20% of the total hydrogen, and the volume ratio of the second path of hydrogen is 80-95% of the total hydrogen; wherein the first path of hydrogen and the second path of hydrogen are used to form a first mesoscopic product and a second mesoscopic product, respectively.
3. A diesel low-pressure mesoscopic fixed-bed hydrocracking method according to claim 2, characterized in that: The S2 includes: S21, the diesel feedstock is pumped by the feedstock delivery pump (1), preheated to a set temperature by the first heat exchange system (3), and then enters the first mesoscopic pool (5) together with the first hydrogen gas preheated to the set temperature, wherein the diesel feedstock and the first hydrogen gas form a first mesoscopic product in the first mesoscopic pool (5); S22, the first mesoscopic product enters the second mesoscopic pool (6), the second mesoscopic pool (6) is arranged at the front or rear of the heating furnace (7), or at the entrance of the first mesoscopic reactor (8), or at the entrance of the second mesoscopic reactor (10), and the second hydrogen gas preheated to a set temperature enters the second mesoscopic pool (6), and the conversion of kinetic energy to surface energy between hydrogen and diesel is completed in the second mesoscopic pool (6), so that the hydrogen and diesel are converted into the second mesoscopic product formed by hydrogen bubbles and oil droplets of set size.
4. A diesel low-pressure mesoscopic fixed-bed hydrocracking method according to claim 3, characterized in that: The S3 includes: S31, sending the preheated second mesoscopic product into one or more first catalyst beds (9A) provided in the first mesoscopic reactor (8); S32, the material to be reacted in the first mesoscopic reactor (8) is kept in a mesoscopic state and passes through the first catalyst bed (9A) to undergo a hydrogenation refining reaction; S33, the product after the hydrogenation reaction through the first catalyst bed (9A) is kept in a mesoscopic state and sent to one or more second catalyst beds (11A) arranged in the second mesoscopic reactor (10); S34, the reacted material in the second mesoscopic reactor (10) is maintained in a mesoscopic state and passes through the second catalyst bed (11A) to undergo a hydrocracking reaction.
5. A diesel low-pressure mesoscopic fixed-bed hydrocracking method according to claim 4, characterized in that: The S4 includes: S41, the material after the hydrocracking reaction leaves the second mesoscopic reactor (10) and enters the gas-liquid separation system (12) to undergo gas-liquid separation to form a liquid phase material and a hydrogen-rich gas phase material; S42, the liquid phase material enters the fractionation system for fractionation, and the corresponding fraction exits the device; S43, the hydrogen-rich gas phase material enters the circulating hydrogen system for treatment and then is recycled.
6. A diesel low-pressure mesoscopic fixed-bed hydrocracking method according to claim 5, characterized in that: The manner in which the second mesoscopic product enters the first mesoscopic reactor (8) and the second mesoscopic reactor (10) is determined by engineering design based on the overall plan of the process device, and is one of the methods of top-in and bottom-out or bottom-in and top-out.
7. A diesel low-pressure mesoscopic fixed-bed hydrocracking method according to claim 6, characterized in that: The first catalyst bed (9A) and the second catalyst bed (11A) are respectively loaded with a first catalyst and a second catalyst, wherein the first catalyst and the second catalyst are respectively a hydrorefining catalyst and a hydrocracking catalyst, and then the first catalyst bed (9A) and the second catalyst bed (11A) are respectively loaded according to a first catalyst loading scheme and a second catalyst loading scheme.
8. A diesel low-pressure mesoscopic fixed-bed hydrocracking system, used for implementing the method described in any one of claims 1 to 7, characterized in that: include: A raw material delivery pump (1), a hydrogen compressor (2), a first heat exchange system (3), a second heat exchange system (4), a first mesoscopic pool (5), a second mesoscopic pool (6), a heating furnace (7), a first mesoscopic reactor (8), a second mesoscopic reactor (10) and a gas-liquid separation system (12); wherein: The hydrogen raw material is pressurized to the process pressure by the hydrogen compressor (2), and after passing through the second heat exchange system (4), the hydrogen is divided into two paths, the volume ratio of the first path hydrogen is 5-20% of the total hydrogen, and the volume ratio of the second path hydrogen is 80-95% of the total hydrogen; The diesel feedstock is pumped by the feedstock delivery pump (1), and after being preheated to a set temperature by the first heat exchange system (3), it enters the first mesoscopic pool (5) together with the first hydrogen gas preheated to the set temperature. In the first mesoscopic pool (5), the diesel feedstock and the first hydrogen gas form a first mesoscopic product. The first mesoscopic product enters the second mesoscopic pool (6), and the second mesoscopic pool (6) is arranged at the front or rear of the heating furnace (7), or at the entrance of the first mesoscopic reactor (8), or at the entrance of the second mesoscopic reactor (10). At the same time, the second hydrogen gas preheated to a set temperature enters the second mesoscopic pool (6), and the conversion of kinetic energy to surface energy between hydrogen and diesel is completed in the second mesoscopic pool (6), so that the hydrogen and diesel are converted into the second mesoscopic product formed by hydrogen bubbles and oil droplets of 1 to 500 μm. The placement position of the second mesoscopic pool (6) can be selected in a variety of ways (Figure 1); The second mesoscopic product enters the first mesoscopic reactor (8); the first mesoscopic reactor (8) comprises one or more first catalyst beds (9A); the reacted material in the first mesoscopic reactor (8) is kept in the mesoscopic state and undergoes a hydrogenation reaction through the hydrorefining catalyst loaded in the first catalyst bed (9A); The hydrogenation reaction product passing through the first catalyst bed (9A) enters the second mesoscopic reactor (10); the second mesoscopic reactor (10) comprises one or more second catalyst beds (11A); the reacted material in the second mesoscopic reactor (10) is kept in a mesoscopic state and undergoes a hydrocracking reaction through the second catalyst loaded in the second catalyst bed (11A); The material after the hydrogenation reaction leaves the second mesoscopic reactor (10) and enters the gas-liquid separation system (12) for gas-liquid separation. The liquid phase material enters the fractionation system for fractionation and the corresponding fraction is discharged from the device. The hydrogen-rich gas phase material enters the circulating hydrogen system for treatment and then is recycled.
9. The system according to claim 8, characterized in that According to different operating pressures, different hydrogen-oil ratios and different liquid viscosities, the aperture of the hydrogen radiation channel, the geometric parameters of the longitudinal and transverse gas pulverizers, the geometric parameters of the disruptor and the geometric parameters of the gas-liquid mixing divider are adjusted to determine the structural form of the first mesoscopic pool (5) and the second mesoscopic pool (6).
10. The system according to claim 9, characterized in that The first mesoscopic pool (5) and the second mesoscopic pool (6) are respectively GC mesoscopic pool I, GC mesoscopic pool II or GC mesoscopic pool III; wherein: The internal structural parts of the GC mesoscopic pool I include a shell, an oil inlet hole (11), a hydrogen radiation channel (12), a gas pulverizer (13) and a carrier plate flow guide divider (14); applicable conditions include: operating pressure ≤ 2MPa; hydrogen-oil ratio within 800:1; catalyst layer loading, mixed loading, and mesoscopic injection can be either upper or lower; The internal structural parts of the GC mesoscopic cell II include a component shell (20), an oil inlet elliptical hole (21), a hydrogen radiation channel (22), a gas pulverizer (23), a segmentation disruptor (24) and a carrier plate flow diverter (25); applicable conditions include: operating pressure ≤ 3MPa / 5MPa; hydrogen-oil ratio within 1200:1; catalyst layer loading, mixed loading, and mesoscopic state injection can be either upper or lower; The internal structural components of the GC mesoscopic pool III include a component shell, an oil inlet groove hole (31), a hydrogen radiation channel (32), a gas pulverizer (33), a disruptor (34) and a carrier plate flow diverter (35). The anti-backflow damper (30) has 7 0 ~12 0 The applicable conditions include: operating pressure ≤5MPa / 8MPa; hydrogen-to-oil ratio within 1500:1; catalyst layer loading, mixed loading, and mesoscopic injection can be done at the upper and lower ports.