A hydrogenation reaction system

Abstract

The present invention discloses a hydrogenation reaction system, which belongs to the technical field of petroleum hydrogenation. The hydrogenation reaction system includes a quench box, a heating furnace, a hydrofining reactor, a hydrocracking reactor, a heat exchanger, and a water cooler. The raw oil is first heat-exchanged with the second product flowing out of the bottom of the hydrocracking reactor in the heat exchanger, and then sent to the hydrofining reactor after being heated by the heating furnace, and the first product is obtained after reacting with hydrogen; the first product is sent to the hydrocracking reactor, and the second product is obtained after reacting with hydrogen; the second product is cooled by the heat exchanger and the water cooler in turn and sent to the distillation system for processing; the hydrofining reactor and the hydrocracking reactor are both provided with a catalyst bed layer of not less than 2 layers, and a quench box is arranged between the catalyst beds. The hydrogenation reaction system provided by the present invention adopts a specific quench box, and the mixing effect of the cold medium and the hot reaction flow in the hydrogenation reactor is more ideal, the temperature distribution of the mixed flow is more uniform, the hydrogenation effect is improved, and the product distribution is improved.

Description

Technical Field

[0001] The invention belongs to the technical field of petroleum hydrogenation, and in particular relates to a hydrogenation reaction system. Background Art

[0002] Hydrogenation reactions are common in petroleum refining and petrochemical processes, such as hydrocracking and hydrofining reactions. Hydrogenation reactors provide a place for hydrogenation reactions. All hydrogenation reactors will release a large amount of reaction heat during operation. Excessive temperature will affect the performance of the catalyst. Therefore, in order to ensure the performance of the catalyst and the stable and safe operation of the device, the catalyst bed temperature must be effectively controlled; otherwise, when the heat released by the reaction is much greater than the heat removed from the device, the device will generate huge heat accumulation in a short period of time, resulting in a jump-like rise in the temperature inside the reactor, thermal imbalance of the system, and reaching a level that is difficult to control. This is what is commonly known as the "flying temperature" phenomenon. The flying temperature phenomenon can lead to a variety of adverse effects, such as a significant reduction in the selectivity, activity and life of the catalyst. Severe flying temperatures can even directly lead to sintering and deactivation of the catalyst; premature deactivation of the catalyst will not only increase the cost of the catalyst, but also frequent replacement of the catalyst will greatly shorten the operating cycle of the device, which will have a negative impact on the overall economic benefits of the refinery. Therefore, when the heat released by the reaction is large, it is very necessary to take appropriate measures to remove the heat from the reactor. The solution commonly used in industry is to divide the catalyst into several beds when loading it, and set a quench box between two adjacent catalyst beds to remove the heat released by the reaction, thereby reducing the temperature of the reactant flow. The number of beds and their respective heights are determined by the temperature rise curve, and are generally divided into 2 to 6 beds, each bed is about 3-6 meters high. Setting a quench box between adjacent catalyst beds can achieve full mixing of the reaction hot flow and the coolant and make it flow evenly into the next catalyst bed, so that the next catalyst bed can continue to undergo hydrogenation reaction.

[0003] At present, the mixing mechanism of the coolant and the reaction hot flow in the quench box generally includes throttling, collision and swirl, and baffle-type quench boxes, impact-type quench boxes and swirl-type quench boxes are designed accordingly.

[0004] Patent document US3723072 discloses a typical baffle-type quench box, in which the high-temperature fluid from the upper catalyst bed enters the quench box body through an annular plate with evenly distributed circular holes under the guidance of the flow channel, and the cold hydrogen enters the box body through the circular inlet in the center of the top plate. There is an annular mixing box in the central area of ​​the circular box body, and the gas-liquid two-phase completes preliminary mixing and heat transfer in the annular mixing box. After that, the gas-liquid mixture enters the conveying channel under the guidance of the baffle, and further turbulent flow is performed in the channel. After a reciprocating process, the gas-liquid two-phase is evenly mixed; however, this quench box is large in size, and a large number of baffles will increase the flow resistance of the fluid, resulting in excessive loss of fluid kinetic energy, a large pressure drop, and poor overall economic benefits.

[0005] Patent document US3502445 is a representative of the impact quench box developed by Union Oil Company in the United States. It mainly includes an upper top plate, a central box body and a lower bottom plate. The upper top plate has two symmetrical circular throttling holes located directly above the central box body. There is a rectangular rectifying baffle at symmetrical positions on both sides of the central box body. The baffle is evenly distributed with circular small holes, and the bottom plate is evenly distributed with circular sieve holes. The reaction flow of the upper bed layer is blocked by the top plate of the quench box. Most of it is first retained on the top plate, and then it is brought into the central box body through the throttling holes on the top plate by the high-speed injection of the gas phase cold medium; due to the sudden reduction of the flow area at the throttling hole, the mixed flow produces a throttling effect, and hits the bottom plate at a very high speed to produce splashes and vortices, which enhances the disturbance effect of the fluid, and then the fluid is further accelerated at the contraction flow channel of the central box body; the high-speed mixed flow has a violent collision in the central box body and flows out of the central box body in two ways. When encountering the rectifying baffle, part of the mixed flow flows out from the openings on the baffle, and the other part of the mixed flow is deflected to the outer area of ​​the central box due to hitting the unopened area of ​​the baffle, and finally all the flows flow through the sieve holes opened on the bottom plate to the next catalyst bed. This quench box was once widely used in petroleum refining, but in devices with heavy crude oil as feed and high gas-liquid ratio, the radial temperature difference at the outlet of the catalyst bed is large, sometimes even up to 10-20°C.

[0006] Patent document CN2448440Y discloses a cyclone type quench box, which is composed of a cold hydrogen pipe, a baffle, a semicircular mixing channel, a tangential guide tube, and a mixing box. The hot reaction flow from the upper catalyst bed is initially mixed with the cold hydrogen on the baffle, and then enters the mixing box with a much smaller diameter than the quench box through the semicircular mixing channel. After cyclone mixing in the mixing box, it is baffled and mixed again through the throttle hole at the bottom of the mixing box. Finally, the mixed flow reaches the sieve plate, and the sieve plate makes the flow uniformly distributed to the next catalyst bed. This structure has a short contact time of the mixed flow in the mixing chamber, resulting in uneven temperature of the reactant flow flowing out of the sieve plate, which in turn affects the performance of the catalyst.

[0007] In view of this, the present invention provides a hydrogenation reaction system with a specific quench box structure. Summary of the invention

[0008] In view of the deficiencies in the prior art, the object of the present invention is to provide a hydrogenation reaction system so as to make the mixing effect of the cold medium and the hot reaction flow in the hydrogenation reactor more ideal, make the temperature distribution of the mixed flow more uniform, improve the hydrogenation effect, and improve the product distribution.

[0009] In order to achieve the above object, the present invention adopts the following technical solution:

[0010] A hydrogenation reaction system comprises a quench box, a heating furnace, a hydrofining reactor, a hydrocracking reactor, a heat exchanger and a water cooler. The raw oil is first heat-exchanged with a second product flowing out of the bottom of the hydrocracking reactor in the heat exchanger, and then heated in the heating furnace and sent to the hydrofining reactor to react with hydrogen to obtain a first product; the first product is sent to the hydrocracking reactor to react with hydrogen to obtain the second product; the second product is cooled in turn by the heat exchanger and the water cooler and then sent to the distillation system for treatment;

[0011] The hydrotreating reactor and the hydrocracking reactor are both provided with catalyst beds of not less than 2 layers, and a quench box is provided between the catalyst beds.

[0012] As a preferred embodiment of the technical solution of the present invention, the quench box includes a top plate, a bottom plate and a mixing box formed therebetween, the top plate, the mixing box and the bottom plate are all centrally symmetrically arranged; a hollow annular feed boss is arranged on the top plate, a feed throttling hole is provided in the middle of the top plate, a first through hole corresponding to the feed throttling hole is provided in the middle of the annular feed boss, and a feed swirl plate is radially arranged between the outer side of the first through hole and the inner wall of the annular feed boss; a second through hole corresponding to the feed throttling hole is provided in the middle of the mixing box, a hollow cylindrical rectifying ring plate is also provided inside the mixing box, a mixing swirl plate is radially arranged between the outer side of the second through hole and the inner wall of the rectifying ring plate; a rectifying ring plate throttling hole is provided on the side wall of the rectifying ring plate; a mixing box inner sieve hole is provided on the part of the bottom plate located between the inner side of the rectifying ring plate and the outer side of the second through hole, and a mixing box outer sieve hole is provided on the part of the bottom plate located on the outer side of the rectifying ring plate;

[0013] The height of the feed rotary plate is higher than the height of the annular feed boss, and a liquid-blocking circular plate is fixedly mounted on the upper surface of the feed rotary plate.

[0014] As a preferred embodiment of the technical solution of the present invention, the upper end of the rectifying ring plate is fixedly mounted on the bottom of the top plate, and the lower end of the rectifying ring plate is fixedly mounted on the upper part of the bottom plate.

[0015] As a preferred embodiment of the technical solution of the present invention, the feed rotary plate is an arc-shaped vertical plate.

[0016] As a preferred embodiment of the technical solution of the present invention, the mixing rotating plate is an arc-shaped vertical plate.

[0017] As a preferred embodiment of the technical solution of the present invention, the arc bending directions of the feed rotary plate and the mixing rotary plate are opposite.

[0018] As a preferred embodiment of the technical solution of the present invention, the shape of the throttling hole of the rectifying ring plate is one or more of a triangle, a square or a circle.

[0019] As a preferred embodiment of the technical solution of the present invention, the number of throttling holes of the rectifying ring plate is 48 to 80, and the number of the feed rotary plate and the mixing rotary plate are both 4 to 8.

[0020] As a preferred embodiment of the technical solution of the present invention, the opening rates of the sieve holes inside the mixing box and the sieve holes outside the mixing box are both 5-20%, and the opening sizes are both 6-18 mm.

[0021] As a preferred embodiment of the technical solution of the present invention, the opening density of the sieve holes inside the mixing box is smaller than the opening density of the sieve holes outside the mixing box.

[0022] As a preferred embodiment of the technical solution of the present invention, the top plate and the bottom plate are both fixedly mounted on the reactor wall.

[0023] Compared with the prior art, the present invention has the following beneficial effects:

[0024] The present invention provides a hydrogenation reaction system, which adopts a quench box with a specific structure. The quench box mainly includes a top plate, an annular feed boss, a feed swirl, a mixing swirl, a bottom plate and other components, and has a novel and simple structure. In the quench box, the hot reaction flow from the upper catalyst bed and the added cold medium are first gathered on the top plate and pre-mixed. When the liquid phase accumulates to a certain thickness on the top plate, it passes over the annular feed boss and is accelerated by the feed swirl before entering the mixing box through the throttle hole. Compared with the previous quench boxes, since a feed swirl is added on the top plate and a mixing swirl is added in the mixing box, the flow channel length is increased, the contact time between the gas phase and the liquid phase is greatly extended, and the mixing and heat transfer effects are improved, thereby reducing the radial temperature difference at the inlet of the lower catalyst bed, which is conducive to the full play of the catalyst performance.

[0025] In short, by using a quench box with a specific structure in the hydrogenation reaction system, the cold and hot logistics can be mixed evenly, which plays a role in cooling the catalyst bed and distributing the temperature evenly, avoiding the generation of hot spots. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a schematic structural diagram of the quench box 100 of the present invention;

[0027] Figure 2 for Figure 1 A-A section view in FIG.

[0028] Figure 3 for Figure 1 The B-B section view in FIG.

[0029] Figure 4 It is a three-dimensional schematic diagram of the upper structure of the quench box of the present invention;

[0030] Figure 5 It is a three-dimensional schematic diagram of the lower part structure of the quench box of the present invention;

[0031] Figure 6 It is a schematic diagram of the structure of the hydrogenation reaction system of the present invention.

[0032] Among them, 1. top plate; 2. liquid-blocking circular plate; 3. annular feed boss; 4. feed throttling hole; 5. feed rotary plate; 6. rectifying ring plate; 7. rectifying ring plate throttling hole; 8. sieve hole inside the mixing box; 9. mixing box; 10. mixing rotary plate; 11. sieve hole outside the mixing box; 12. bottom plate; 13. reactor wall; 100. quench box; 110. raw material pump; 120. heating furnace; 130. hydrotreating reactor; 140. inlet diffuser; 150. cold hydrogen pipe; 160. outlet collector; 170. hydrocracking reactor; 180. heat exchanger; 190. water cooler. DETAILED DESCRIPTION

[0033] The following will be combined with the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. 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.

[0034] See also Figure 6 A hydrogenation reaction system includes a quench box 100, a heating furnace 120, a hydrofining reactor 130, a hydrocracking reactor 170, a heat exchanger 180, and a water cooler 190. The raw oil is first heat-exchanged with a second product flowing out of the bottom of the hydrocracking reactor 170 in the heat exchanger 180, and then heated by the heating furnace 120 and sent to the hydrofining reactor 130 to react with hydrogen to obtain a first product; the first product is sent to the hydrocracking reactor 170 to react with hydrogen to obtain the second product; the second product is cooled by the heat exchanger 180 and the water cooler 190 in sequence and sent to the distillation system for treatment;

[0035] The hydrotreating reactor 130 and the hydrocracking reactor 170 are both provided with at least two catalyst beds, and a quench box 100 is provided between the catalyst beds.

[0036] In the above technical solution, it can be understood that the hydrogenation reaction system includes:

[0037] The heat exchanger 180 is used for exchanging heat between the second product flowing out from the bottom of the hydrocracking reactor 170 and the feedstock oil;

[0038] The heating furnace 120 is used to further heat up the crude oil after heat exchange in the heat exchanger 180;

[0039] The hydrofining reactor 130 is used for conducting a hydrofining reaction between the raw oil and hydrogen after heat exchange in the heating furnace 120, and obtaining a first product at the bottom after the reaction;

[0040] The hydrocracking reactor 170 is used for performing a hydrocracking reaction between the first product and hydrogen, and obtaining a second product at the bottom after the reaction;

[0041] The water cooler 190 is used to further cool the second product after heat exchange in the heat exchanger 180 .

[0042] In some embodiments, the feed oil may be pumped to the heat exchanger 180 by the feed pump 110 .

[0043] In some embodiments, an inlet diffuser 140 is provided at the bottom of the hydrofining reactor 130 to distribute the raw oil; an outlet collector is provided at the bottom of the hydrofining reactor 130 to collect and discharge the first product after the reaction of the hydrofining reactor 130; similarly, a similar structure can also be provided inside the hydrocracking reactor 170. The above structures are conventional means for those skilled in the art, and the specific structures are not limited or described in the present invention.

[0044] In some embodiments, hydrogen is sent from the cold hydrogen pipe 150 to the hydrotreating reactor 130 and the hydrocracking reactor 170 .

[0045] For further information, see Figures 1 to 5The quench box 100 comprises a top plate 1 and a bottom plate 12 which are separated from each other and a mixing box 9 formed therebetween. The top plate 1, the mixing box 9 and the bottom plate 12 are all centrally symmetrically arranged. A hollow annular feed boss 3 is arranged on the top plate 1. A feed throttling hole 4 is provided in the middle of the top plate 1. A first through hole (not numbered in the figure) corresponding to the feed throttling hole 4 is provided in the middle of the annular feed boss 3. A feed rotary plate 5 is radially arranged between the outer side of the first through hole and the inner wall of the annular feed boss 3. A second through hole (not numbered in the figure) corresponding to the feed throttle hole 4 is provided in the middle, a hollow cylindrical rectifying ring plate 6 is further provided inside the mixing box 9, a mixing swirl plate 10 is radially provided between the outer side of the second through hole and the inner wall of the rectifying ring plate 6; a rectifying ring plate throttle hole 7 is provided on the side wall of the rectifying ring plate 6; a mixing box inner sieve hole 8 is provided on the portion of the bottom plate 12 located between the inner side of the rectifying ring plate 6 and the outer side of the second through hole, and a mixing box outer sieve hole 11 is provided on the portion of the bottom plate 12 located on the outer side of the rectifying ring plate 6;

[0046] The height of the feed rotary plate 5 is higher than the height of the annular feed boss 3 , and a liquid-blocking circular plate 2 is fixedly mounted on the upper surface of the feed rotary plate 5 .

[0047] In the above technical scheme, the quench box of the present invention is generally of central symmetrical structure. The first through hole, the feed throttling hole 4 and the second through hole are all arranged in the middle of the quench box and are interconnected, so as to facilitate the circulation of the hot and cold mixed flow; by setting the annular feed boss 3 and limiting the height of the feed spiral plate 5 to be higher than the height of the annular feed boss 3, a circulation channel is formed between the annular feed boss 3 and the liquid baffle circular plate 2, so as to facilitate the hot and cold flow to overflow into the mixing box 9 through the annular feed boss after being fully mixed on the top plate 1; the setting of the feed spiral plate 5 is used to guide and accelerate the hot and cold mixed materials; the setting of the feed throttling hole 4 is used to increase the flow rate of the hot and cold mixed materials by throttling; the bottom plate 12 is provided with a mixing box inner sieve hole 8 on the part between the inner side of the rectifying ring plate 6 and the outer side of the second through hole, and the bottom plate 12 is located on the rectifying ring plate 6. The outer part is provided with a mixing box outer sieve hole 11, which is arranged so that the bottom plate 12 is located in the corresponding area below the second through hole and no hole is provided (corresponding to area C). After the cold and hot mixed materials enter through the second through hole, they will bounce and splash on the bottom plate 12 to generate a vortex. The liquid phase flow is carried by the gas phase flow and broken into small droplets, and then further swirls and mixes along the mixing vortex plate 10. A part of the mixed flow passes through the sieve hole 8 in the mixing box (corresponding to area D) and flows out of the quench box roughly evenly; the other part of the mixed flow hits the rectifying ring plate 6 at a high speed, rushes out of the mixing box 9 through the rectifying ring plate throttling hole 7 on the rectifying ring plate 6, and is relatively evenly distributed on the opening area F outside the mixing box 9, and finally flows out of the quench box through the mixing box outer sieve hole 11 in area F.

[0048] In some embodiments, the top plate 1 and the bottom plate 12 are both fixedly mounted on the reactor wall 13. By such an arrangement, the quench box can be fixed.

[0049] In some embodiments, the upper end of the fairing ring plate 6 is fixedly mounted on the bottom of the top plate 1, and the lower end of the fairing ring plate 6 is fixedly mounted on the upper part of the bottom plate 12. It is understandable that the fixed installation form can be various common forms such as welding, which is a conventional choice for those skilled in the art.

[0050] In some embodiments, the feed rotary plate 5 is a curved vertical plate; in some embodiments, the mixing rotary plate 10 is a curved vertical plate.

[0051] In some embodiments, the arc bending directions of the feed rotary plate 5 and the mixing rotary plate 10 are opposite to each other. Such an arrangement can further enhance the mixing effect of the cold and hot mixed materials.

[0052] In some embodiments, the shape of the throttle hole 7 of the rectifying ring plate is one or more of a triangle, a square or a circle; preferably, a circle. It is understandable that the size of the throttle hole 7 of the rectifying ring plate can be set accordingly as needed, and this embodiment does not specifically limit it.

[0053] In some embodiments, the number of the throttling holes 7 of the rectifying ring plate is 48 to 80; it is understandable that the number of the throttling holes 7 of the rectifying ring plate can be flexibly selected according to actual needs; preferably, the number of the throttling holes 7 of the rectifying ring plate is 80.

[0054] The number of the feed vortex plates 5 and the mixing vortex plates 10 are both 4 to 8. It is understandable that the number of the feed vortex plates 5 can be 4, 5, 6, 7 or 8; the number of the mixing vortex plates 10 can also be 4, 5, 6, 7 or 8; the specific number of the two can be flexibly selected according to actual needs; preferably, the number of the feed vortex plates 5 and the mixing vortex plates 10 is equal, both 8.

[0055] In some embodiments, the opening ratio of the mixing box inner sieve hole 8 and the mixing box outer sieve hole 11 are both 5-20%, and the opening size is both 6-18 mm. It is understandable that the opening ratio and the opening size can be set according to actual needs.

[0056] In some embodiments, the opening density of the mesh holes 8 in the mixing box is less than the opening density of the mesh holes 11 outside the mixing box. In this way, the mesh holes 8 in the mixing box with a small opening density can slow down the fluid from flowing out of the mixing box and prolong the mixing time; the mesh holes 11 outside the mixing box with a large opening density can make the fluid flow more smoothly to the next bed layer and reduce the pressure drop.

[0057] In some embodiments, the quench box is installed on the reactor wall 13. Meanwhile, it should be noted that, for the convenience of description, the reactor walls of the hydrotreating reactor 130 and the hydrocracking reactor 170 are not strictly distinguished in the present invention, and are uniformly referred to as the reactor wall 13.

[0058] Further reading Figure 1 to Figure 6 , the entire working process and principle of the hydrogenation reaction system of the present invention are specifically described:

[0059] The raw oil is sent to the heat exchanger 180 through the raw material pump 110, and is heated by the heat exchange with the hot flow flowing out of the hydrocracking reactor 170 and then enters the heating furnace 120 for heating. The heated hot flow enters from the top of the hydrofining reactor 130, first diffuses to the entire reactor cross section through the inlet diffuser 140, and then flows downward to the catalyst bed for refining reaction. The heated hot flow continues to flow downward after the reaction; then, the hot reaction flow from the upper catalyst bed and the cold medium (hydrogen) added through the cold hydrogen pipe 150 enter the quench box 100. The specific action process is: the hot reaction flow and the cold medium are first gathered on the top plate 1 and pre-mixed. When the liquid phase accumulates to a certain thickness on the top plate 1, it passes over the annular feed boss 3. Under the action of the feed rotary plate 5, the mixed flow begins to rotate and accelerate, and then enters the mixing box 9 through the feed throttling hole 4. Due to the sudden throttling, the flow rate surges, and the mixed flow violently impacts the central non-perforated area C of the mixing box 9, rebounds and splashes on the bottom plate 12, and generates a vortex; the liquid phase flow is carried by the gas phase flow and broken into small droplets, and then further swirls and mixes along the mixing vortex plate 10, and a part of the mixed flow flows through the sieve holes 8 in the mixing box on the perforated area D in the mixing box and flows out of the quench box roughly evenly; the other part of the mixed flow hits the rectifying ring plate 6 at a high speed, rushes out of the mixing box 9 through the rectifying ring plate throttling hole 7 on the rectifying ring plate 6, and is more evenly distributed on the perforated area F outside the mixing box, and finally flows out of the quench box through the sieve holes 11 outside the mixing box on the area F;

[0060] The reaction flow after cooling enters the catalyst bed again for reaction, and enters the quench box 110 for cooling after heating, and this process is repeated many times until it flows out of the last catalyst bed and flows out through the outlet collector 160 installed at the bottom of the hydrotreating reactor 130. Then the reaction flow flows into the top of the hydrocracking reactor 170, and after a process similar to that of the hydrotreating reactor 130, flows out from the bottom of the hydrocracking reactor 170, enters the heat exchanger 180, exchanges heat with the raw material sent by the raw material pump 110 for cooling, and then enters the water cooler 190 for cooling. The cooled flow is sent to the distillation system for separation to obtain various products.

[0061] A hydrogenation reaction system of the present invention is further described below in conjunction with specific embodiments.

[0062] Example 1

[0063] In this specific embodiment, a hydrogenation reaction system includes a quench box 100, a heating furnace 120, a hydrofining reactor 130, a hydrocracking reactor 170, a heat exchanger 180, and a water cooler 190. The raw oil is first heat-exchanged with the second product flowing out of the bottom of the hydrocracking reactor 170 in the heat exchanger 180, and then heated by the heating furnace 120 and sent to the hydrofining reactor 130 to react with hydrogen to obtain a first product; the first product is sent to the hydrocracking reactor 170 to react with hydrogen to obtain the second product; the second product is cooled by the heat exchanger 180 and the water cooler 190 in turn and sent to the distillation system for treatment;

[0064] The hydrotreating reactor 130 and the hydrocracking reactor 170 are both provided with three catalyst beds, and a quench box 100 is provided between the catalyst beds.

[0065] The raw oil is delivered to the heat exchanger 180 by the raw material pump 110; meanwhile, the tops of the hydrofining reactor and the hydrocracking reactor are both equipped with an inlet diffuser 140; and the bottoms are both equipped with an outlet collector 160.

[0066] Among them, a quench box 100 of the same structure is installed between the catalyst beds in the hydrotreating reactor 130 and the hydrocracking reactor 170 (the specific specifications and dimensions are different), and the quench box 100 includes a top plate 1 and a bottom plate 12 separated from each other and a mixing box 9 formed therebetween, and the top plate 1, the mixing box 9 and the bottom plate 12 are all centrally symmetrically arranged; a hollow annular feed boss 3 is arranged on the top plate 1, a feed throttling hole 4 is opened in the middle of the top plate 1, and a first through hole corresponding to the feed throttling hole 4 is opened in the middle of the annular feed boss 3, and the outer side of the first through hole is connected to the outer side of the first through hole. A feed swirl plate 5 is radially arranged between the inner walls of the annular feed boss 3; a second through hole corresponding to the feed throttling hole 4 is provided in the middle of the mixing box 9, and a hollow cylindrical rectifying ring plate 6 is also provided inside the mixing box 9, and a mixing swirl plate 10 is radially arranged between the outer side of the second through hole and the inner wall of the rectifying ring plate 6; a rectifying ring plate throttling hole 7 is provided on the side wall of the rectifying ring plate 6; a mixing box inner sieve hole 8 is provided on the portion of the bottom plate 12 located between the inner side of the rectifying ring plate 6 and the outer side of the second through hole, and a mixing box outer sieve hole 11 is provided on the portion of the bottom plate 12 located on the outer side of the rectifying ring plate 6. The quench box is fixedly mounted on the reactor wall 13 through the top plate 1 and the bottom plate 12;

[0067] The height of the feed rotary plate 5 is higher than that of the annular feed boss 3 , and a liquid blocking circular plate 2 is fixedly mounted on the upper surface of the feed rotary plate 5 .

[0068] In this specific embodiment, the upper end of the rectifying ring plate 6 is fixedly mounted on the bottom of the top plate 1 , and the lower end of the rectifying ring plate 6 is fixedly mounted on the upper part of the bottom plate 12 .

[0069] In this specific embodiment, the feed rotary plate 5 and the mixing rotary plate 10 are both arc-shaped vertical plates, and the arc bending directions of the two are opposite.

[0070] In this specific embodiment, the throttle holes 7 of the rectifying ring plate are circular in shape and are 80 in number.

[0071] In this specific embodiment, the number of the feed rotary plate 5 and the number of the mixing rotary plate 10 are both 8.

[0072] In this specific embodiment, the opening size of the sieve hole 8 inside the mixing box is 8 mm, and the opening rate is 7%; the opening size of the sieve hole 11 outside the mixing box is 8 mm, and the opening rate is 12%.

[0073] In this embodiment, the hydrogenation reaction system adopts a specific quench box, which has a feed vortex plate 5 added on the top plate 1 and a mixing vortex plate 10 and a rectifying ring plate 6 added in the mixing box. Under the combined effect of these three, not only the residence time of the mixed flow in the quench box is greatly prolonged, but also the mixed flow has multiple throttling, collision and swirl, which are beneficial to the full mixing and heat exchange of the hot reaction flow and the added cold medium, and uniform distribution to the lower catalyst bed.

[0074] The present invention illustrates the technical concept of the present invention through the above-mentioned embodiments, but the present invention is not limited to the above-mentioned embodiments, that is, it does not mean that the present invention must rely on the above-mentioned embodiments to be implemented. Those skilled in the art should understand that any improvement of the present invention, equivalent replacement of individual raw materials of the product of the present invention, addition of auxiliary components, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the present invention.

Claims

1. A hydrogenation reaction system, characterized in that: The method comprises a quench box (100), a heating furnace (120), a hydrofining reactor (130), a hydrocracking reactor (170), a heat exchanger (180), and a water cooler (190). The crude oil is firstly heat-exchanged with a second product flowing out of the bottom of the hydrocracking reactor (170) in the heat exchanger (180), and then heated in the heating furnace (120) and sent to the hydrofining reactor (130), where it reacts with hydrogen to obtain a first product. The first product is sent to a hydrocracking reactor (170) and reacts with hydrogen to obtain the second product; The second product is cooled in turn by a heat exchanger (180) and a water cooler (190) and then sent to a distillation system for treatment; The hydrotreating reactor (130) and the hydrocracking reactor (170) are both provided with at least two catalyst beds, and a quench box (100) is provided between the catalyst beds; The quench box (100) comprises a top plate (1) and a bottom plate (12) which are separated from each other and a mixing box (9) formed therebetween. The top plate (1), the mixing box (9) and the bottom plate (12) are all centrally symmetrically arranged. A hollow annular feed boss (3) is arranged on the top plate (1). A feed throttling hole (4) is provided in the middle of the top plate (1). A first through hole corresponding to the feed throttling hole (4) is provided in the middle of the annular feed boss (3). A feed rotary plate (5) is radially arranged between the outer side of the first through hole and the inner wall of the annular feed boss (3). A second through hole corresponding to the feed throttling hole (4) is provided in the middle of the mixing box (9). The mixing box (9) is also provided with a hollow cylindrical rectifying ring plate (6) inside, and a mixing swirl plate (10) is radially provided between the outer side of the second through hole and the inner wall of the rectifying ring plate (6); a rectifying ring plate throttling hole (7) is provided on the side wall of the rectifying ring plate (6); a mixing box inner sieve hole (8) is provided on the portion of the bottom plate (12) located between the inner side of the rectifying ring plate (6) and the outer side of the second through hole, and a mixing box outer sieve hole (11) is provided on the portion of the bottom plate (12) located on the outer side of the rectifying ring plate (6); wherein the height of the feed swirl plate (5) is higher than the height of the annular feed boss (3), and a liquid blocking circular plate (2) is fixedly mounted on the upper surface of the feed swirl plate (5); The opening density of the sieve holes (8) inside the mixing box is smaller than the opening density of the sieve holes (11) outside the mixing box.

2. A hydrogenation reaction system according to claim 1, characterized in that: The upper end of the rectifying ring plate (6) is fixedly mounted on the bottom of the top plate (1), and the lower end of the rectifying ring plate (6) is fixedly mounted on the upper part of the bottom plate (12).

3. A hydrogenation reaction system according to claim 1, characterized in that: The feed rotary plate (5) is an arc-shaped vertical plate.

4. A hydrogenation reaction system according to claim 1, characterized in that: The mixing rotating plate (10) is an arc-shaped vertical plate.

5. A hydrogenation reaction system according to claim 4, characterized in that: The arc bending directions of the feed rotary plate (5) and the mixing rotary plate (10) are opposite.

6. A hydrogenation reaction system according to claim 1, characterized in that: The shape of the throttle hole (7) of the rectifying ring plate is one or more of a triangle, a square or a circle.

7. A hydrogenation reaction system according to claim 1, characterized in that: The number of throttling holes (7) of the rectifying ring plate is 48 to 80, and the number of the feeding rotary plate (5) and the number of the mixing rotary plate (10) are both 4 to 8.

8. A hydrogenation reaction system according to claim 1, wherein the opening rate of the sieve holes (8) in the mixing box is 5-20%, and the opening size is 6-18 mm.

9. A hydrogenation reaction system according to claim 1, wherein the opening rate of the sieve holes (11) outside the mixing box is 5-20%, and the opening size is 6-18 mm.

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