Hydrogenation device hot feed fractionation system

Abstract

The invention discloses a hot feed fractionating system of a hydrogenation device, and relates to the technical field of rectification, the hot feed fractionating system comprises a stripping tower, a heat exchanger, a suction pump, a heater and a fractionating tower, when a diesel raw material is subjected to hydrogenation operation, the diesel raw material enters the stripping tower, and after passing through the stripping tower, heavy components such as the diesel raw material are discharged into the fractionating tower for fractionating; diesel oil and wax oil at the bottom enter a heater through a suction pump and then are discharged into a fractionating tower, a first tower plate is fixedly arranged in the fractionating tower, a plurality of gas rising pipes are fixedly arranged on the first tower plate, a supporting piece is arranged in each gas rising pipe, a movable first bubble cap is arranged on each supporting piece, and a spiral piece is arranged in each first bubble cap. According to the invention, the rotatable first bubble cap is arranged, so that the problem of poor separation effect at a key position is solved, heavy components in rising gas can be separated in advance by cooling the spiral sheet, and the burden of separating the heavy components is reduced.

Description

Technical Field

[0001] The present invention relates to the technical field of rectification, and particularly relates to a hot feed fractionation system for a hydrogenation unit. Background Art

[0002] In a hydrogenation unit, after the feedstock oil (such as catalytic diesel, straight-run diesel, etc.) is mixed with hydrogen and enters the hydrofining reactor through the reaction feed heating furnace for reaction, it is introduced into a stripping column. By introducing superheated steam into the bottom of the column, using the heat provided by the steam and the effect of reducing the partial pressure of the oil and gas, the light components (such as hydrogen sulfide, some light hydrocarbons, etc.) in the diesel are separated from the diesel and discharged from the top of the column with the steam. The diesel after preliminary fractionation, etc. enters the fractionation column, and then, by utilizing the boiling point differences of different substances, through multiple gas-liquid equilibria and mass and heat transfer processes, the products after the hydrogenation reaction are separated. In the fractionation column, the rising gas-phase stream and the descending liquid-phase stream come into full contact on the trays or packing, so that the volatile light components (such as naphtha, etc.) are continuously vaporized from the liquid phase into the gas phase and move towards the top of the column; while the less volatile heavy components (such as wax oil, etc.) are continuously condensed from the gas phase into the liquid phase and flow towards the bottom of the column, thereby separating products with different distillation ranges in different column sections.

[0003] The current process flow usually passes the diesel after the hydrogenation reaction through a stripping column, and then through heat exchange equipment and heating equipment and introduces it into the fractionation column. After the separated products are intercepted in segments and passed through various cooling equipment, they are then introduced into the corresponding storage tank area. However, in actual operation, this process flow has disadvantages such as high water content in the products and high energy consumption.

[0004] It is found in actual use that when the existing bubble-cap fractionation column is in use, for the bubble caps on the lower side of the feed inlet, due to the excessive throughput here, the gas-liquid separation effect is poor, the contact between the gas and the liquid is not sufficient, the contact time is short, and the moving distance of the gas in the liquid is short, resulting in relatively large defects in the gas-liquid separation at this place, affecting the overall processing progress of the fractionation column and reducing the separation efficiency of the fractionation column.

[0005] It is found in actual use that although through the above improvement, the first bubble caps in the area with a relatively large throughput can be rotated, thereby increasing the mass and heat transfer between the gas and the liquid and alleviating the problem of large gas-liquid throughput to a certain extent. However, in actual use, since the rising gas contains a certain amount of heavy components, after contacting with the liquid in the first bubble cap, the liquefied heavy components at this place will increase the separation difficulty between the lighter components and the light components at this place and increase the content of the heavy components. Summary of the Invention

[0006] The purpose of the present invention is to provide a hot feed fractionation system for a hydrogenation unit to solve the technical problems of low mass and heat transfer efficiency of light and heavy components at the key positions and easy re-vaporization of heavy components as mentioned in the above background art.

[0007] To achieve the above object, the present invention provides the following technical solution: a thermal feed fractionation system for a hydrogenation unit, including a fractionation tower. A first tray is fixedly arranged in the fractionation tower. A plurality of riser pipes are fixedly arranged on the first tray. A support member is fixedly arranged in each of the riser pipes. A movable first bubble cap is arranged on each of the support members. A spiral sheet is arranged in each of the first bubble caps for driving the first bubble cap to rotate. A flow guide member is fixedly arranged on the outer peripheral surface of each of the spiral sheets for enabling the first bubble cap to rotate stably.

[0008] Preferably, a gap is left between each of the spiral sheets and the corresponding flow guide member and first bubble cap for discharging the rising gas.

[0009] Preferably, a moving member is arranged on each of the support members. A conducting member is fixedly arranged on each of the moving members. A conducting ring is fixedly arranged in each of the first bubble caps. The conducting ring can move on the support member. A heat preservation member is fixedly arranged on the outer sides of each of the conducting members and the conducting rings. Each of the spiral sheets is fixedly connected to the corresponding conducting ring for rapidly liquefying the heavy components in the first bubble cap.

[0010] Preferably, a first downcomer is arranged on one side of the first tray. A first overflow weir is fixedly arranged on the side of the first tray away from the first downcomer.

[0011] Preferably, a gas collecting hood is arranged on the side of the riser pipe away from the first bubble cap for enabling the gas to enter the riser pipe and accelerate rising.

[0012] Preferably, a moving groove is formed in each of the support members. Each of the moving members is inserted into the corresponding moving groove and can move in the corresponding moving groove.

[0013] Preferably, a plurality of second trays are fixedly arranged in the fractionation tower. A second downcomer is fixedly arranged on each of the second trays. A second overflow weir is fixedly arranged on the side of each of the second trays away from the corresponding second downcomer.

[0014] Preferably, a plurality of second riser pipes are fixedly arranged on each of the second trays. A support rod is fixedly arranged in each of the second riser pipes. A second bubble cap is arranged on each of the support rods.

[0015] Preferably, a light component outlet and a reflux liquid inlet are arranged at the top of the fractionation tower. A product discharge port is arranged at the bottom of the fractionation tower. A feed port is arranged on one side of the fractionation tower.

[0016] Preferably, the fractionation system also includes a stripping tower, a heat exchanger, a suction pump and a heater. When the diesel feedstock completes the hydrogenation operation, it enters the stripping tower from the upper part of the stripping tower, and superheated steam is introduced from the lower part of the stripping tower. After passing through the stripping tower, the diesel feedstock and other heavy components are discharged into the fractionation tower after passing through the heat exchanger to fractionate the diesel feedstock. The diesel and wax oil at the bottom enter the heater through the suction pump and are then discharged into the fractionation tower again. The light components are discharged into the reflux tank through the top of the fractionation tower. After condensation, part of them enter the top of the fractionation tower as reflux liquid, and the raw materials in the fractionation tower are repeatedly separated.

[0017] The beneficial effects of the present invention are: 1. By directly heating the materials at the bottom of the distillation tower, fuel gas and steam are saved, and the power consumption of air cooling is reduced. Since diesel and wax oil are directly extracted from the bottom of the distillation tower and directly transported to the tank area, the water content of the product is reduced, which improves the product quality. After the technical transformation, the middle section of the distillation tower is withdrawn and the diesel stripping tower is stopped. The wax oil and diesel are all mixed at the bottom of the distillation tower and then sent to the tank area through the diesel delivery process at the bottom of the distillation tower. At this point, the air cooling of wax oil is stopped to reduce power consumption, the water cooling of wax oil is stopped to reduce the consumption of circulating water, and the steam injection of the distillation tower is stopped to reduce the use of steam. The water content in the product is reduced through the reboil cycle to improve the product quality.

[0018] 2. The support, spiral sheet and guide member are arranged to make the first bubble cap rotate, so that when the bubble is discharged from the bottom of the first bubble cap, an initial centrifugal force is obtained, so that the bubble moves a longer distance in the reflux liquid, prolongs the time for the bubble to move in the reflux liquid, and increases the consumption of the gas in the bubble in the reflux liquid. The rotation of the first bubble cap can make the reflux liquid rotate, and the vortexes generated by the two adjacent rows of first bubble caps are in opposite directions, so that the reflux liquid and the bubbles in the reflux liquid can collide with each other, so that after the bubble collision, the contact area between the bubble and the reflux liquid is increased on the side.

[0019] 3. Since the gap between the guide member and the first bubble cap is small, the rising air can obtain a certain acceleration again, so that when the bubbles are discharged, the movement speed is greater. The setting of the spiral blades can also accelerate the rising air to a certain extent, making the flow rate of the rising air faster, which is conducive to better moving the bubbles in the liquid and moving a longer distance.

[0020] 4. The impact between the reflux liquids can stir up some liquid droplets, so that the liquid droplets can contact with the rising gas, further increasing the contact probability between the reflux liquid and the rising gas, better consuming the heavy components in the bubbles and the light components in the reflux liquid, gasifying the light components in the reflux liquid and liquefying the heavy components in the rising gas.

[0021] 5. By enabling the first bubble cap to rotate, it is possible to prevent a large amount of viscous raw material oil from adhering to the first bubble cap, and to prevent the weight of the first bubble cap from increasing due to the adhesion of the raw material oil when the first bubble cap remains stationary for a long time, thus reducing the burden during the rotation of the first bubble cap.

[0022] 6. By providing the moving groove and the moving part, the first bubble cap can move up and down. By providing the conducting part, the heat-insulating part and the conducting ring, the relatively low temperature in the upper layer can be transferred to the spiral fins, thereby reducing the temperature of the spiral fins, causing the heavy components in the rising gas to be liquefied in advance, and reducing the probability of the heavy components in the liquid being vaporized again.

[0023] 7. By discharging the liquefied heavy components from the spiral fins and at the same time through the spiral arrangement of the spiral fins, the moving distance of the heavy components in the rising gas can be increased, the moving time at a lower temperature can be prolonged, giving sufficient time for the heavy components to be liquefied, thereby making the gas-liquid separation more efficient and preventing the heavy components in the rising gas from having a greater impact on the separation effect. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 It is a schematic diagram of the system of the present invention.

[0025] Figure 2 It is a schematic diagram of the overall structure of the fractionating tower of the present invention.

[0026] Figure 3 It is a schematic diagram of the full cross-sectional structure of the fractionating tower of the present invention.

[0027] Figure 4 It is a schematic diagram of the distribution of the second bubble cap on the second tray of the present invention.

[0028] Figure 5 It is a cross-sectional view of the structure of the second bubble cap of the present invention.

[0029] Figure 6 It is a schematic diagram of the distribution of the first bubble cap on the first tray of the present invention.

[0030] Figure 7 It is a schematic diagram of the connection relationship of the riser pipe on the first tray of the present invention.

[0031] Figure 8 It is a cross-sectional view of the structure of the first bubble cap of the present invention.

[0032] Figure 9 It is a schematic diagram of the connection relationship between the spiral fins and the flow guide part of the present invention.

[0033] Figure 10 It is a schematic diagram of the connection relationship between the moving part and the moving groove of the present invention.

[0034] The attached drawing reference numerals are: 1, stripping column; 101, condensate tank; 2, heat exchanger; 3, suction pump; 4, heater; 5, fractionating column; 6, reflux tank; 7, first tray; 701, riser pipe; 702, support; 703, first bubble cap; 704, spiral fin; 705, deflector; 706, conductor; 707, heat insulation member; 708, conduction ring; 709, first downcomer; 710, first overflow weir; 711, gas collecting hood; 712, moving member; 713, moving groove; 8, second tray; 801, second downcomer; 802, second overflow weir; 803, second riser pipe; 804, support rod; 805, second bubble cap. Detailed implementation manners

[0035] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative efforts shall fall within the protection scope of the present invention. Embodiment 1

[0036] The current process flow is usually to pass the diesel after hydrogenation reaction through the stripping column 1, and then through heat exchange equipment and heating equipment and then into the fractionating column 5. After the separated products are intercepted in segments and then passed through various cooling equipment and then into the corresponding tank farms. However, in actual operation of this process flow, due to the segmented taking method, there are disadvantages such as high water content in the products and high energy consumption.

[0037] To solve the above technical problems, please refer to Figures 1 to 10 As shown, the technical solutions adopted include a stripping column 1, a heat exchanger 2, a suction pump 3 and a heater 4, and also include a fractionating column 5. When the diesel raw material completes the hydrogenation operation, it enters the stripping column 1 from the upper part of the stripping column 1, and the superheated steam is introduced from the lower part of the stripping column 1. After passing through the stripping column 1, the heavy components such as the diesel raw material are discharged into the fractionating column 5 through the heat exchanger 2, and the diesel raw material is fractionated. The diesel and wax oil at the bottom enter the heater 4 through the suction pump 3 and then are discharged into the fractionating column 5 again. The light components are discharged into the reflux tank 6 from the top of the fractionating column 5. After condensation, part of it enters the top of the fractionating column 5 as reflux liquid, and the raw materials in the fractionating column 5 are repeatedly separated. A light component outlet and a reflux liquid inlet are provided at the top of the fractionating column 5, a product discharge port is provided at the bottom of the fractionating column 5, and a feed port is provided on one side of the fractionating column 5.

[0038] In actual production, after the feedstock oil (such as catalytic diesel, straight-run diesel, etc.) is mixed with hydrogen and enters the hydrofining reactor through the reaction feed heating furnace for reaction (this process is not shown in the figure and is prior art, so it will not be described in detail here), after the feedstock oil is preliminarily separated and purified, the separated feedstock oil is introduced into the stripping column 1. By introducing superheated steam into the bottom of the stripping column 1, using the heat provided by the steam and the effect of reducing the oil-gas partial pressure, the light components in the diesel (such as hydrogen sulfide, some light hydrocarbons, etc.) are separated from the diesel and discharged from the top of the column with the steam. A condensate tank 101 is provided at the top of the stripping column 1. Subsequently, after the light components enter the condensate tank 101 and are condensed, part of them enters the top of the stripping column 1 as reflux liquid to participate in the separation, and the other part is collected and processed.

[0039] The diesel after preliminary fractionation passes through the heat exchanger 2 and then enters the fractionating column 5 through the feed port. Then, by using the boiling point differences of different substances, through multiple gas-liquid equilibria and mass and heat transfer processes, the products after the hydrogenation reaction are separated. In the fractionating column 5, the rising gas-phase stream and the descending liquid-phase stream come into full contact on the trays. A temperature monitoring device and control equipment are provided in the fractionating column 5 (not shown in the figure). When the temperature is too high or too low, the temperature inside the fractionating column 5 is maintained within a suitable range by adjusting the reflux of the reflux tank 6 or the heating degree of the heater 4. The reflux tank 6 can liquefy the gas at a higher temperature. This technology is prior art and will not be described in detail here. Moreover, the bottom temperature of the fractionating column 5 is controlled to a degree that can liquefy diesel and wax oil, enabling the volatile light components to continuously vaporize from the liquid phase into the gas phase and move towards the top of the column.

[0040] The less volatile heavy components such as wax oil and diesel continuously condense from the gas phase into the liquid phase and flow towards the bottom of the fractionating column 5. The liquefied diesel and wax oil are discharged into the heater 4 through the discharge port and the suction of the suction pump 3 for circulating heating. Only the materials at the bottom of the column are heated, saving energy consumption. The heated materials are discharged into the fractionating column 5 through the pipeline to participate in the separation of the feedstock oil again and provide heat for the fractionating column 5 to maintain the internal temperature balance. After fractionation, part of the diesel and wax oil are discharged to the tank farm for storage through the suction pump 3. The light components are discharged into the reflux tank 6 through the light component outlet at the top of the fractionating column 5. After condensation, part of them enters the fractionating column 5 as reflux liquid through the reflux liquid inlet to participate in the separation of the fractionating column 5, and the excess part is collected and processed. During the process of discharging the diesel and wax oil to the tank farm, the wax oil air cooler and the wax oil water cooler are both shut down, reducing energy consumption.

[0041] By directly heating the materials at the bottom of the fractionating tower 5, fuel gas and steam are saved, the power consumption of the air cooler is reduced. Since diesel oil and wax oil are directly extracted from the bottom of the fractionating tower 5 and directly transported to the tank farm, the water content of the products is reduced, and the product quality is improved. After the technical transformation, the middle section extraction of the fractionating tower 5 is stopped, the diesel stripping tower 1 is stopped, and the wax oil and diesel are all mixed at the bottom of the fractionating tower 5 and sent to the tank farm through the bottom external delivery process of the fractionating tower 5. Thus, the air cooler for wax oil is stopped to reduce the power consumption, the water cooler for wax oil is stopped to reduce the circulating water consumption, the steam injection of the fractionating tower 5 is stopped to reduce the steam consumption, and the water content in the products is reduced through the reboiling cycle to improve the product quality. Example Two

[0042] During actual use, it is found that when the existing bubble-cap fractionating tower 5 is in use, the bubble caps on the lower side of the feed inlet have poor gas-liquid separation effect during use because the throughput here is too large, resulting in insufficient contact between gas and liquid, short contact time, and short moving distance of the gas in the liquid, leading to large defects in gas-liquid separation at this place, affecting the overall processing progress of the fractionating tower 5 and reducing the separation efficiency of the fractionating tower 5.

[0043] To solve the above technical problems, please refer to Figures 1 to 10 As shown in the figure, the technical solution adopted includes a fractionating tower 5. A first tray 7 is fixedly arranged inside the fractionating tower 5. A plurality of riser pipes 701 are fixedly arranged on the first tray 7. A support member 702 is fixedly arranged inside each riser pipe 701. A movable first bubble cap 703 is arranged on each support member 702. A spiral piece 704 is arranged inside each first bubble cap 703 for driving the first bubble cap 703 to rotate. A guide member 705 is fixedly arranged on the outer peripheral surface of each spiral piece 704 for enabling the first bubble cap 703 to rotate stably. A gap is left between each spiral piece 704 and the corresponding guide member 705 and first bubble cap 703 for discharging the rising gas. A first downcomer 709 is arranged on one side of the first tray 7. A first overflow weir 710 is fixedly arranged on the side of the first tray 7 away from the first downcomer 709. A gas collecting hood 711 is arranged on the side of the riser pipe 701 away from the first bubble cap 703 for enabling gas to enter the riser pipe 701 to accelerate rising. A plurality of second trays 8 are fixedly arranged inside the fractionating tower 5. A second downcomer 801 is fixedly arranged on each second tray 8. A second overflow weir 802 is fixedly arranged on the side of each second tray 8 away from the corresponding second downcomer 801. A plurality of second riser pipes 803 are fixedly arranged on each second tray 8. A support rod 804 is fixedly arranged inside each second riser pipe 803. A second bubble cap 805 is arranged on each support rod 804.

[0044] During use, when processing is carried out at this location, since this location is relatively close to the heat source, there is sufficient rising gas and a large impact force of the rising gas. Before the rising gas passes through the riser pipe 701 on the first tray 7, the gas enters the gas collecting hood 711, and most of the surrounding gas is collected and enters the riser pipe 701. Since the diameter of the gas collecting hood 711 gradually decreases in the direction from far away from the first tray 7 to close to the first tray 7, the rising gas can be accelerated in the riser pipe 701, so that the initial velocity of the rising gas is relatively large.

[0045] The feedstock oil and the reflux liquid gradually flow downward onto the first tray 7 and the second tray 8 on the lower side through the first downcomer 709 and the second downcomer 801. The first overflow weir 710 and the second overflow weir 802 can maintain a certain height of the liquid and then discharge it to the tray, making the range of the liquid flow onto the first tray 7 and the second tray 8 larger and more evenly dispersed. The rising gas flows upward through the riser pipe 701, the gas collecting hood 711, and the second riser pipe 803, so that there is a certain contact time between the gas and the liquid, and the mass transfer and heat transfer processes are completed.

[0046] After passing through the riser pipe 701, the rising gas enters the deflector 705, and the rising gas begins to act on the helical fins 704. Since the helical fins 704 are helical and have a certain angle, and there is a gap between the helical fins 704 and the deflector 705, the rising gas can pass through the gap, and the gas is discharged between the deflector 705 and the first bubble cap 703. Therefore, the rising gas can make the helical fins 704 rotate on the support 702, and the helical fins 704 drive the deflector 705 and the first bubble cap 703 to rotate on the support 702. The rising gas is discharged from the bottom of the first bubble cap 703 and contacts the liquid. And because the gap between the deflector 705 and the first bubble cap 703 is relatively small, the rising gas can obtain a certain acceleration again, so that when the bubbles are discharged, the moving speed is relatively large.

[0047] Moreover, the setting of the helical fins 704 can also accelerate the rising gas to a certain extent, making the flow rate of the rising gas faster. Since the first bubble cap 703 rotates at this time, it can make the liquid flow to a certain extent, and at the same time give the rising gas a centrifugal force, making the discharged bubbles of uniform size and enabling the rising gas to move farther in the liquid and have a longer contact time, better completing the mass transfer and heat transfer between the gas and the liquid, better separating the light components from the heavy components, and better liquefying the heavy components and vaporizing the light components.

[0048] When the rising gas enters the second bubble cap 805 through the gas-lifting pipe 803, the gas is discharged from the bottom of the second bubble cap 805. A plurality of exhaust grooves are provided on the lower end surfaces of the first bubble cap 703 and the second bubble cap 805, facilitating the dispersion of the gas into multiple strands and making the gas more evenly dispersed in the liquid, which is not shown in the figure. The discharged gas becomes liquid bubbles and moves in the liquid. The remaining gas after mass transfer and heat transfer continues to participate in the gas-liquid mass transfer and heat transfer reactions on the upper layer of the first tray 7 or the second tray 8 as the rising gas.

[0049] Moreover, the first bubble caps 703 are arranged in rows on the first tray 7, and the spiral directions of the spiral fins 704 in adjacent rows are different, making the rotation directions of the first bubble caps 703 in adjacent rows opposite. Therefore, the moving directions of the reflux liquid and the feedstock oil can be staggered, better enabling the impact between the vortices of the reflux liquid, dispersing the bubbles into smaller bubbles, increasing the contact area between the bubbles and the liquid, and being more conducive to heat and mass transfer. The impact between the reflux liquids can stir up some droplets, enabling the droplets to contact the rising gas, further increasing the contact probability between the reflux liquid and the rising gas, better consuming the heavy components in the bubbles and the light components in the reflux liquid. The rotation of the first bubble cap 703 can prevent a large amount of the feedstock oil from adhering to the first bubble cap 703, reducing the influence of the adhesion of the feedstock oil on the rotation of the first bubble cap 703.

[0050] By providing the support member 702, the spiral fin 704, and the flow guide member 705, the first bubble cap 703 can be rotated. When the bubbles are discharged from the bottom of the first bubble cap 703, an initial centrifugal force can be obtained, enabling the bubbles to move a longer distance in the reflux liquid, extending the moving time of the bubbles in the reflux liquid, and increasing the consumption of the gas in the bubbles in the reflux liquid. The rotation of the first bubble cap 703 can cause the reflux liquid to rotate, and the vortex directions generated by adjacent rows of the first bubble caps 703 are opposite, enabling collisions between the reflux liquids and between the bubbles in the reflux liquid. After the bubbles collide, the contact area between the bubbles and the reflux liquid can be increased on the side. Since the gap between the flow guide member 705 and the first bubble cap 703 is relatively small, the rising gas can obtain a certain acceleration again, making the moving speed of the bubbles larger when they are discharged. The setting of the spiral fin 704 can also enable the rising gas to obtain a certain acceleration, increasing the flow rate of the rising gas, being conducive to better enabling the bubbles to move in the liquid and move a longer distance. The impact between the reflux liquids can stir up some droplets, enabling the droplets to contact the rising gas, further increasing the contact probability between the reflux liquid and the rising gas, better consuming the heavy components in the bubbles and the light components in the reflux liquid, vaporizing the light components in the reflux liquid, and liquefying the heavy components in the rising gas. At the same time, the rotation of the first bubble cap 703 can prevent a large amount of viscous feedstock oil from adhering to the first bubble cap 703, preventing the weight of the first bubble cap 703 from being increased due to the adhesion of the feedstock oil when the first bubble cap 703 does not move for a long time, and reducing the burden on the rotation of the first bubble cap 703. Embodiment III

[0051] In actual use, it is found that although the above improvements can make the first bubble cap 703 in the area with a large processing capacity rotate, thereby increasing the mass transfer and heat transfer between gas and liquid, and alleviating the problem of large gas-liquid processing volume to a certain extent, in actual use, due to the fact that the rising gas contains a certain amount of heavy components, after contacting with the liquid in the first bubble cap 703, the liquefied heavy components at this place will increase the separation difficulty between the lighter components and the light components, increase the content of heavy components, and increase the probability of the heavy components being liquefied again.

[0052] To solve the above technical problems, please refer to Figures 1 to 10 As shown, the technical solution adopted includes a support member 702. A moving member 712 is provided on each support member 702. A conducting member 706 is fixedly provided on each moving member 712. A conducting ring 708 is fixedly provided in each first bubble cap 703. The conducting ring 708 can move on the support member 702. A heat insulation member 707 is fixedly provided on the outer side of each conducting member 706 and conducting ring 708. Each spiral fin 704 is fixedly connected to the corresponding conducting ring 708 for quickly liquefying the heavy components in the first bubble cap 703. A moving groove 713 is formed in each support member 702. Each moving member 712 is inserted into the corresponding moving groove 713 and can move in the corresponding moving groove 713.

[0053] In specific use, on the basis of the above Embodiment I and Embodiment II, when the rising gas enters the riser 701 through the gas collecting hood 711, the impact force of the rising gas causes the first bubble cap 703 to move upward. The first bubble cap 703 drives the spiral fin 704 and the flow guiding member 705 to move upward. The first bubble cap 703 drives the conducting ring 708 and the heat insulation member 707 to move upward. After the conducting ring 708 moves upward a certain distance, it contacts the conducting member 706 and pushes the conducting member 706 to move upward. The conducting member 706 drives the moving member 712 to move upward. The moving member 712 can first slide in the moving groove 713. After sliding until the conducting member 706 contacts the upper second tray 8, the moving member 712 can rotate in the moving groove 713. This can be solved by using the way of keyway and spline, which is not shown in the figure. This technology is prior art and will not be described in detail here.

[0054] At the same time, the spiral fin 704 drives the first bubble cap 703 and the flow guiding member 705 to rotate. The first bubble cap 703 drives the conducting ring 708 to rotate. Since the temperature of the second tray 8 above the first tray 7 is relatively low, the heat insulation member 707 is made of heat insulation material, and the conducting ring 708 and the conducting member 706 are made of heat conducting material, so that heat exchange occurs between the second tray 8 and the conducting ring 708 and the conducting member 706, thereby quickly reducing the temperature of the conducting ring 708 and the conducting member 706.

[0055] Meanwhile, the heat insulation member 707 can prevent the heat on the conduction ring 708 and the conduction member 706 from quickly rising after exchanging with the upper space of the first tray 7. After the temperature of the conduction ring 708 decreases, the temperature of the helical fin 704 decreases, so that the heavy components are liquefied after contacting the helical fin 704. The released heat is carried out by the ascending gas and transfers heat after contacting the liquid to vaporize the light components, or is absorbed by the helical fin 704, reducing the burden during gas-liquid separation at this place, separating the heavy components in the ascending gas in advance, reducing the content of the heavy components discharged from the first bubble cap 703, thereby making the gas-liquid separation more efficient and reducing the probability of the re-vaporization of the heavy components. The liquefied heavy components are thrown off from the helical fin 704. Since there is a centrifugal force when the helical fin 704 rotates, the heavy components can be thrown off between the helical fin 704 and the flow guide member 705 and will not fall back into the riser pipe 701, preventing the riser pipe 701 from being blocked.

[0056] Meanwhile, since the helical fin 704 is helically arranged, it can make the moving time of the ascending gas between the helical fin 704 and the flow guide member 705 longer and the moving distance increase, so that the heavy components and the light components can be better separated in the helical fin 704. Thus, the heavy components are liquefied after contacting the helical fin 704, reducing the burden during gas-liquid separation at this place, separating the heavy components in the ascending gas in advance, reducing the content of the heavy components discharged from the first bubble cap 703, thereby making the gas-liquid separation more efficient and reducing the probability of the re-vaporization of the heavy components.

[0057] By providing the moving groove 713 and the moving member 712, the first bubble cap 703 can move up and down. By providing the conduction member 706, the heat insulation member 707 and the conduction ring 708, the lower temperature of the upper layer can be transferred to the helical fin 704, so that the temperature of the helical fin 704 decreases, and thus the heavy components in the ascending gas are liquefied in advance, reducing the probability of the re-vaporization of the heavy components in the liquid. The liquefied heavy components are thrown off from the helical fin 704. Meanwhile, due to the helical arrangement of the helical fin 704, the moving distance of the heavy components in the ascending gas can be increased, and the moving time at a lower temperature can be prolonged, giving enough time for the heavy components to liquefy, thereby making the gas-liquid separation more efficient and preventing the heavy components in the ascending gas from having a greater impact on the separation effect.

[0058] The above is only a preferred specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention, according to the technical solution and inventive concept of the present invention, makes equivalent substitutions or changes, and should be covered by the protection scope of the present invention.

Claims

1. A hot feed fractionation system for a hydrogenation unit, comprising a fractionation tower (5), characterized in that: A first tower plate (7) is fixedly provided in the fractionation tower (5), and a plurality of riser pipes (701) are provided on the first tower plate (7), each of the riser pipes (701) is provided with a support member (702), each of the support members (702) is provided with a movable first bubble cap (703), each of the first bubble caps (703) is provided with a spiral sheet (704) for driving the first bubble cap (703) to rotate, and a flow guide member (705) is fixedly provided on the outer peripheral surface of each of the spiral sheets (704) for ensuring stable rotation of the first bubble cap (703).

2. A hot feed fractionation system for a hydrogenation unit according to claim 1, characterized in that: A gap is left between each spiral sheet (704) and the corresponding guide member (705) and the first bubble cap (703) for allowing the rising air to be discharged.

3. A hot feed fractionation system for a hydrogenation unit according to claim 2, characterized in that: Each of the support members (702) is provided with a moving member (712), each of the moving members (712) is fixedly provided with a conducting member (706), each of the first bubble caps (703) is fixedly provided with a conducting ring (708), the conducting ring (708) is movable on the support member (702), a heat-insulating member (707) is fixedly provided on the outside of each of the conducting members (706) and the conducting ring (708), and each of the spiral sheets (704) is fixedly connected to the corresponding conducting ring (708), so as to rapidly liquefy the heavy components in the first bubble caps (703).

4. A hot feed fractionation system for a hydrogenation unit according to claim 3, characterized in that: A first downcomer (709) is disposed on one side of the first tower plate (7), and a first overflow weir (710) is fixedly disposed on a side of the first tower plate (7) away from the first downcomer (709).

5. A hot feed fractionation system for a hydrogenation unit according to claim 4, characterized in that: A gas collecting hood (711) is provided on a side of the gas riser (701) away from the first bubble cap (703) and is used to allow gas to enter the gas riser (701) and accelerate its ascent.

6. A hot feed fractionation system for a hydrogenation unit according to claim 5, characterized in that: A moving groove (713) is provided in each of the supporting members (702), and each of the moving members (712) is inserted into a corresponding moving groove (713) and is capable of moving in the corresponding moving groove (713).

7. A hot feed fractionation system for a hydrogenation unit according to claim 6, characterized in that: A plurality of second trays (8) are fixedly provided in the fractionation tower (5), each of the second trays (8) is fixedly provided with a second downcomer (801), and each of the second trays (8) is fixedly provided with a second overflow weir (802) on a side away from the corresponding second downcomer (801).

8. A hot feed fractionation system for a hydrogenation unit according to claim 7, characterized in that: Each of the second tower plates (8) is provided with a plurality of second gas lift tubes (803), each of the second gas lift tubes (803) is fixedly provided with a support rod (804), and each of the support rods (804) is provided with a second bubble cap (805).

9. A hot feed fractionation system for a hydrogenation unit according to claim 8, characterized in that: The top of the fractionation tower (5) is provided with a light component outlet and a reflux liquid inlet, the bottom of the fractionation tower (5) is provided with a product discharge port, and one side of the fractionation tower (5) is provided with a feed port.

10. A hot feed fractionation system for a hydrogenation unit according to claim 9, comprising a stripping tower (1), a heat exchanger (2), a suction pump (3) and a heater (4), characterized in that: After the diesel feedstock has completed the hydrogenation operation, it enters the stripping tower (1) from the upper part of the stripping tower (1), and superheated steam is introduced from the lower part of the stripping tower (1). After passing through the stripping tower (1), the diesel feedstock and other heavy components are discharged into the fractionation tower (5) through the heat exchanger (2) to fractionate the diesel feedstock. The diesel and wax oil at the bottom enter the heater (4) through the suction pump (3) and are then discharged into the fractionation tower (5) again. The light components are discharged into the reflux tank (6) through the top of the fractionation tower (5). After condensation, the part enters the top of the fractionation tower (5) as reflux liquid, and the raw materials in the fractionation tower (5) are repeatedly separated.

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