Inlet diffuser and micro-bubble-micro-droplet hydrogenation reactor

Abstract

An inlet diffuser and a microbubble-microdroplet hydrogenation reactor, belonging to the field of chemical equipment, are disclosed. The inlet diffuser includes a support plate, with a slow-flow zone formed on the upper surface of the central region of the support plate. Through-holes are distributed on the surface of the slow-flow zone. The support plate has an arc-shaped convex structure with a high center and low edges, and a continuous extended plate surrounds its edge. The extended plate is arc-shaped and convex in the direction of the incoming flow, with its edge height exceeding the center of the support plate. A turbulent zone is formed at the connection between the extended plate and the support plate. The area on the upper surface of the extended plate above the center of the support plate forms a peripheral splash zone. This invention divides the gas-liquid mixture into three diffusion zones, enabling highly viscous heavy oil to diffuse effectively and rapidly to the periphery, increasing the diffusion range, and simultaneously enhancing mass transfer between the oil and gas phases.

Description

Technical Field

[0001] This invention relates to hydrogenation reactors in the field of chemical equipment, specifically an inlet diffuser and a microbubble-microdroplet hydrogenation reactor. Background Technology

[0002] With the increasing heavy and low-quality crude oil being processed domestically, coupled with my country's rapid economic development and increasingly stringent environmental regulations, the market demand for clean oil products is also increasing rapidly. Therefore, the lightening and upgrading of heavy oil is a crucial task that urgently needs to be addressed. Hydrotreating technology is an effective means to solve these problems. Through hydrotreating, impurities such as sulfur, nitrogen, metals, gums, and residual carbon can be effectively removed from oil products, and unsaturated hydrocarbons can be hydrogenated into saturated hydrocarbons.

[0003] As one of the core components of a hydrogenation reactor, the inlet diffuser is the first device that oil and gas pass through when entering the reactor. The inlet diffuser performs the initial distribution of oil and gas entering the reactor and plays a crucial role in the uniformity of gas-liquid distribution throughout the entire reaction process.

[0004] Currently, hydrogenation reactors are getting larger and larger. Conventional inlet diffusers have difficulty dispersing oil and gas evenly into the reactor, especially for highly viscous oils such as heavy oil. This leads to hot spots in the reactor, which in turn causes catalyst coking, overheating, and other issues, affecting product quality and production safety. Summary of the Invention

[0005] The purpose of this invention is to provide an inlet diffuser and a microbubble-microdroplet hydrogenation reactor. The inlet diffuser divides the gas-liquid mixture into three diffusion zones: a slow-flow zone that is in direct contact with the gas-liquid mixture, an outer splash zone that guides the gas-liquid mixture to diffuse to the periphery, and a turbulent zone between the two zones. By dividing the mixture into three zones, viscous heavy oil can be effectively and rapidly diffused to the periphery, increasing the diffusion range. At the same time, it can also enhance the mass transfer between the oil and the gas phase.

[0006] The technical solution adopted by the present invention to achieve the above-mentioned technical objective is as follows: an inlet diffuser, comprising a support disk that impacts and contacts a gas-liquid mixture existing in the form of microbubbles, and a slow-flow zone that reduces the velocity of the gas-liquid mixture is formed on the upper surface of the central region of the support disk, and through holes are distributed on the surface of the slow-flow zone. The support disk is an arc-shaped convex structure with a high center and a low edge, and a continuous extension plate is provided around its edge. The extension plate is an arc shape that convexes in the direction of the incoming flow, and the height of its edge exceeds the center of the support disk. A turbulent zone is formed at the connection between the extension plate and the support disk. The area on the upper surface of the extension plate that is higher than the center of the support disk forms an outer splash zone.

[0007] As an optimized solution for the aforementioned inlet diffuser, the surface of the peripheral splash zone is distributed with through holes.

[0008] As another optimization of the aforementioned inlet diffuser, the height of the central region of the epitaxial plate exceeds the height of the edge.

[0009] As another optimization of the aforementioned inlet diffuser, the support plate is provided with a connecting rod for fixing it inside the hydrogenation reactor.

[0010] As another optimization of the aforementioned inlet diffuser, the connecting rod is elastic, so that when the gas-liquid mixture impacts the support plate, the support plate can vibrate up and down.

[0011] A microbubble-microdroplet hydrogenation reactor is provided in which the gas phase is mixed with the liquid phase in the form of microbubbles to form a gas-liquid mixed flow, which is then introduced into the reactor inlet. After being diffused by an inlet diffuser, the mixture enters the reactor interior. The inlet diffuser is the same as described above.

[0012] As an optimized solution for the aforementioned microbubble-microdroplet hydrogenation reactor, a distribution plate is provided below the inlet diffuser inside the reactor. Several gas-liquid distributors are distributed on the distribution plate, and the bottom of the gas-liquid distributors extends to the bottom of the distribution plate, forming a funnel-shaped gas-liquid spray outlet.

[0013] As another optimized solution for the aforementioned microbubble-microdroplet hydrogenation reactor, the gas-liquid distributor includes a hollow tube that runs through the distribution plate, with a cover plate at the top, and a gas inlet formed between the bottom surface of the cover plate and the top of the hollow tube. One or two suction pipes are installed on the hollow tube above the distribution plate.

[0014] As another optimized solution for the aforementioned microbubble-microdroplet hydrogenation reactor, the suction pipe has a suction channel with an inner diameter that gradually narrows along the flow direction of the liquid phase to draw the liquid phase into the hollow tube to form small droplets. The portion of the hollow tube below the distribution plate is divided into a conical section and a gradually expanding section. The inner diameter of the conical section gradually narrows from top to bottom, while the inner diameter of the gradually expanding section gradually increases from top to bottom, and a neck is formed at the connection between the two sections.

[0015] As another optimized scheme for the above-mentioned microbubble-microdroplet hydrogenation reactor, in the liquid absorption channel, the ratio of minimum inner diameter: maximum inner diameter: axial length is 1:5-10:20-50; in the conical tube section, the ratio of minimum inner diameter: maximum inner diameter: axial length is 1:3-6:5-10; in the gradually expanding section, the ratio of minimum inner diameter: maximum inner diameter: axial length is 1:6-10:5-10, and the inner diameter of the gas-liquid spray outlet at the bottom of the gradually expanding section is greater than the maximum inner diameter of the conical tube section.

[0016] Compared with the prior art, the present invention has the following beneficial effects:

[0017] 1) The inlet diffuser of the present invention divides the gas-liquid mixture into three diffusion zones: a slow-flow zone that is in direct contact with the gas-liquid mixture, an outer splash zone that guides the gas-liquid mixture to diffuse to the surrounding area, and a turbulent zone between the two zones. By dividing the three zones, the viscous heavy oil can be effectively and quickly diffused to the surrounding area, thereby increasing the diffusion range. At the same time, it can also enhance the mass transfer between the oil and the gas phase.

[0018] 2) The microbubble-microdroplet hydrogenation reactor of the present invention is also equipped with a gas-liquid distributor with a special structure. The side of the top of the gas-liquid distributor forms a gas phase inlet. After the gas phase enters the hollow tube at high speed, the liquid phase is drawn in through the liquid suction pipe. Since the liquid suction channel in the liquid suction pipe has a variable diameter structure, the liquid phase is turned into small droplets and mixed with the gas phase. Then, as it moves downward along the hollow tube, it is first accelerated by the conical tube section and then ejected from the trumpet-shaped nozzle of the gradually expanding section. This allows the gas phase and the microbubbles remaining in the liquid phase in the hollow tube to interact, which further breaks the small droplets into even smaller droplets, so that the gas and liquid phases can enter the catalyst bed more uniformly to participate in the reaction. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of the inlet diffuser in this invention;

[0020] Figure 2 This is a simplified structural diagram of the microbubble-microdroplet hydrogenation reactor of the present invention;

[0021] Figure 3 This is a schematic diagram of the gas-liquid distributor in the microbubble-microdroplet hydrogenation reactor of the present invention;

[0022] Reference numerals: 1. Inlet diffuser; 101. Support plate; 102. Extension plate; 103. Connecting rod; 104. Slow flow zone; 105. Turbulent zone; 106. Peripheral splash zone; 2. Reactor inlet; 3. Gas-liquid distributor; 301. Hollow tube; 302. Conical tube section; 303. Gradually expanding section; 304. Neck; 305. Suction pipe; 306. Suction channel; 307. Cover plate; 308. Gas phase inlet; 309. Gas-liquid jet outlet; 4. Distribution plate; 401. Liquid storage zone. Detailed Implementation

[0023] The technical solution of the present invention will be further described in detail below with reference to specific embodiments. Parts not explained in the following embodiments of the present invention, such as the technology related to other structures of the catalyst bed inside the hydrogenation reactor, and how to make the gas phase exist stably in the form of microbubbles in the liquid phase, are all considered to be prior art known or should be known by those skilled in the art.

[0024] Example 1

[0025] An inlet diffuser, such as Figure 1 As shown, the device includes a support plate 101 that impacts and contacts the gas-liquid mixture flowing in the form of microbubbles. This gas-liquid mixture is a mixture of heavy oil and hydrogen, where the hydrogen is mixed with the oil in the form of microbubbles. This mixing is typically achieved using a microbubble generator, which stably stores the gas phase within the liquid phase in the form of microbubbles. Since the inlet diffuser is located inside the hydrogenation reactor, the gas-liquid mixture entering from the reactor's material inlet first impacts the inlet diffuser. After diffusion and distribution by the diffuser, it enters the reactor interior. The impact contact with the gas-liquid mixture here refers to the gas-liquid mixture directly impacting the upper surface of the support plate 101. The disk 101 is a plate-shaped component made of metal, generally circular in shape, but can also be other shapes, such as rectangular or other irregular shapes. A slow-flow zone 104 is formed on the upper surface of the central region of the disk 101 to reduce the velocity of the gas-liquid mixture. The disk 101 has a large area; after impacting the central region, the gas-liquid mixture flows towards the edge of the disk 101. Through-holes are distributed on the surface of the slow-flow zone 104. These through-holes allow some of the gas-liquid mixture to directly enter the reactor, while the majority flows towards the edge, thus reducing the flow velocity. The disk 101 has an arc-shaped convex structure with a high center and low edges. The reactor has continuous extended plates 102 surrounding its edge. In practice, the extended plates 102 are distributed around the edge of the support plate 101, forming a semi-closed structure. The bottom plate of the semi-closed structure is the support plate 101, the side plates are the extended plates 102, and the top opening forms the inlet for the gas-liquid mixture. The extended plates 102 are arc-shaped and convex in the direction of the incoming flow. The direction of the incoming flow refers to the direction in which the gas-liquid mixture enters, and the height of its edge exceeds the center of the support plate 101. The edge here refers to the side where the extended plate 102 is connected to the support plate 101. When the inlet diffuser is installed in the reactor, the position of the edge of the extended plate 102 is higher than the highest point of the center of the support plate 101. The position is such that a turbulent zone 105 is formed at the connection between the extension plate 102 and the support plate 101. In practice, the turbulent zone 105 is formed by the part of the support plate 101 excluding the slow flow zone 104 and the area on the upper surface of the extension plate 102 that is lower than the center of the support plate 101. The area on the upper surface of the extension plate 102 that is higher than the center of the support plate 101 forms the peripheral splash zone 106. The gas-liquid mixture overflows from the turbulent zone 105 and flows over the peripheral splash zone 106, and flows into the reactor from the edge of the peripheral splash zone 106. The surface of the peripheral splash zone 106 is distributed with through holes. The height of the middle region of the extension plate 102 exceeds the height of the edge, forming an arc-shaped structure that is high in the middle and low on both sides.

[0026] The above are the basic embodiments of the present invention. Further improvements, optimizations, and limitations can be made based on the above to obtain the following embodiments:

[0027] Example 2

[0028] This embodiment is a limitation of the installation method of embodiment 1. Its main structure is the same as that of embodiment 1. The improvement is that the support plate 101 is provided with connecting rods 103 for fixing it in the hydrogenation reactor. The number of connecting rods 103 is generally three or four. The support plate 101 is suspended below the feed inlet in the hydrogenation reactor, so that it can better maintain balance when the gas-liquid mixture impacts its upper surface.

[0029] In this embodiment, the connecting rod 103 can be a rigid rod, but it is preferred to be elastic so that when the gas-liquid mixture impacts the support plate 101, the support plate 101 can vibrate up and down. In practice, the connecting rod 103 can be directly fixed in the hydrogenation reactor by a spring, or a combination of a rigid rod and a spring can be used, that is, the rigid rod is fixedly connected to the hydrogenation reactor, and the bottom of the rigid rod is fixedly connected to the support plate 101 by a spring.

[0030] Example 3

[0031] A microbubble-microdroplet hydrogenation reactor, such as Figure 2 As shown, the gas phase is mixed with the liquid phase in the form of microbubbles. Hydrogen is mixed with oil in the form of microbubbles. Generally, the mixing of the gas and liquid phases is achieved by a microbubble generator, and the gas phase exists stably in the liquid phase in the form of microbubbles. After forming a gas-liquid mixed flow, it is introduced into the reactor inlet 2, diffused by the inlet diffuser 1, and then enters the reactor. The inlet diffuser 1 is the inlet diffuser of the above embodiment 1 or 2.

[0032] Example 4

[0033] This embodiment is an improvement on embodiment 3. Its main structure is the same as that of embodiment 3, but the improvement lies in: [The following is a more detailed description of the improvement.] Figure 2 As shown, a distribution plate 4 is provided below the inlet diffuser 1 in the reactor. The distribution plate 4 isolates a space at the top of the reactor, forming a liquid storage zone 401. The gas-liquid mixture entering through the inlet diffuser 1 undergoes partial separation. The liquid phase containing microbubbles accumulates on the liquid storage zone 401, while the escaping gas phase is located in the upper region and maintains a certain pressure. Several gas-liquid distributors 3 are distributed on the distribution plate 4. The gas-liquid distributors 3 are used to guide the gas phase and liquid phase into the reaction bed below the distribution plate 4. The bottom of the gas-liquid distributors 3 extends to the bottom of the distribution plate 4 and forms a trumpet-shaped gas-liquid nozzle 309. The trumpet shape means that its inner diameter gradually increases from top to bottom.

[0034] Example 5

[0035] This embodiment is an improvement on embodiment 4. Its main structure is the same as that of embodiment 4, but the improvement lies in: [The following is a more detailed description of the improvement.] Figure 3 As shown, the gas-liquid distributor 3 includes a hollow tube 301 that penetrates the distribution plate 4. It is generally made of metal and has openings at both ends. The top has a cover plate 307, which is fixed to the end of the hollow tube 301 by connectors. There are generally 3 or 4 connectors, which are evenly distributed around the hollow tube 301. The edge of the cover plate 307 extends beyond the hollow tube 301, and a gas phase inlet 308 is formed between the bottom surface of the cover plate 307 and the top of the hollow tube 301. In fact, a gas phase inlet 308 is formed between two adjacent connectors, so that pressurized gas phase enters the hollow tube 301 at high speed through the gas phase inlet 308. One or two suction pipes 305 are set on the hollow tube 301 above the distribution plate 4. The suction pipes 305 are generally horizontal and are used to suck the liquid phase accumulated in the liquid storage area 401 into the hollow tube 301 and mix it with the gas phase again during the downward flow along the hollow tube 301.

[0036] In this embodiment, the suction tube 305 has a suction channel 306, which is actually a cavity inside the suction tube 305. Its two ends are connected to the liquid storage area 401 and the cavity of the hollow tube body 301, respectively. The inner diameter of the suction channel 306 gradually decreases along the flow direction of the liquid phase, that is, it gradually decreases from the liquid storage area 401 towards the hollow tube body 301. The diameter at its smallest point generally does not exceed 3 mm, so as to draw the liquid phase into the hollow tube body 301 to form small droplets. At this time, the small droplets also... Microbubbles are present. The portion of the hollow tube 301 below the distribution plate 4 is divided into a conical section 302 and a gradually expanding section 303. These two sections are integral with the hollow tube 301 above the distribution plate 4. The inner diameter of the conical section 302 gradually decreases from top to bottom, and the inner diameter of the gradually expanding section 303 gradually increases from top to bottom. Both the conical section 302 and the gradually expanding section 303 are arc-shaped or conical tubes, and a necking 304 is formed at the connection between the two. The diameter of the necking 304 generally does not exceed 10 mm.

[0037] In this embodiment, in the liquid suction channel 306, the ratio of minimum inner diameter to maximum inner diameter to axial length is 1:5-10:20-50; in the tapered tube section 302, the ratio of minimum inner diameter to maximum inner diameter to axial length is 1:3-6:5-10; in the expanding section 303, the ratio of minimum inner diameter to maximum inner diameter to axial length is 1:6-10:5-10, and the inner diameter of the gas-liquid spray outlet 309 at the bottom of the expanding section 303 is greater than the maximum inner diameter of the tapered tube section 302.

Claims

1. An inlet diffuser comprising a support disk (101) in impact contact with a gas-liquid mixture existing in the form of microbubbles, wherein a slowing zone (104) for decelerating the gas-liquid mixture is formed on the upper surface of the central region of the support disk (101), and through holes are distributed on the surface of the slowing zone (104), characterized in that: The bearing plate (101) is an arc-shaped protrusion structure with a high center and low edges, and has a continuous extension plate (102) around its edge. The extension plate (102) is an arc protrusion in the direction of the incoming flow, and the height of its edge exceeds the center of the bearing plate (101). A turbulence zone (105) is formed at the connection between the extension plate (102) and the bearing plate (101). The area on the upper surface of the extension plate (102) that is higher than the center of the bearing plate (101) forms a peripheral splash zone (106). Through holes are distributed on the surface of the peripheral splash zone (106). The height of the middle area of ​​the extension plate (102) exceeds the height of the edge.

2. An inlet diffuser according to claim 1, characterised in that: The support plate (101) is provided with a connecting rod (103) for fixing it inside the hydrogenation reactor.

3. An inlet diffuser according to claim 2, characterised in that: The connecting rod (103) is elastic so that when the gas-liquid mixture impacts the bearing plate (101), the bearing plate (101) can vibrate up and down.

4. A microbubble-microdroplet hydrogenation reactor, wherein the gas phase is mixed with the liquid phase in the form of microbubbles to form a gas-liquid mixture, which is then introduced into the reactor inlet (2), diffused through the inlet diffuser (1), and then enters the reactor interior, characterized in that: The inlet diffuser (1) is the inlet diffuser according to any one of claims 1-3.

5. The microbubble-microdroplet hydrogenation reactor according to claim 4, wherein: Below the inlet diffuser (1) of the reactor is a distribution plate (4), on which several gas-liquid distributors (3) are distributed, and the bottom of the gas-liquid distributors (3) extends to the bottom of the distribution plate (4) and forms a trumpet-shaped gas-liquid spray outlet (309).

6. The microbubble-microdroplet hydrogenation reactor according to claim 5, wherein: The gas-liquid distributor (3) includes a hollow tube (301) that penetrates the distribution plate (4), and has a cover plate (307) at the top. A gas inlet (308) is formed between the bottom surface of the cover plate (307) and the top of the hollow tube (301). One or two suction tubes (305) are provided on the hollow tube (301) above the distribution plate (4).

7. The microbubble-microdroplet hydrogenation reactor according to claim 6, wherein: The suction tube (305) has a suction channel (306) inside. The inner diameter of the suction channel (306) gradually decreases along the flow direction of the liquid phase to draw the liquid phase into the hollow tube body (301) to form small droplets. The part of the hollow tube body (301) below the distribution plate (4) is divided into a tapered section (302) and a gradually expanding section (303). The inner diameter of the tapered section (302) gradually decreases from top to bottom, and the inner diameter of the gradually expanding section (303) gradually increases from top to bottom, and a neck (304) is formed at the connection between the two.

8. The microbubble-microdroplet hydrogenation reactor according to claim 7, characterized in that: In the liquid suction channel (306), the ratio of minimum inner diameter to maximum inner diameter to axial length is 1:5-10:20-50; in the conical tube section (302), the ratio of minimum inner diameter to maximum inner diameter to axial length is 1:3-6:5-10; in the expanding section (303), the ratio of minimum inner diameter to maximum inner diameter to axial length is 1:6-10:5-10, and the inner diameter of the gas-liquid spray outlet (309) at the bottom of the expanding section (303) is greater than the maximum inner diameter of the conical tube section (302).

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