Slurry bed residual oil hydrogenation vacuum overhead gas hydrogen enrichment and light hydrocarbon recovery method

Abstract

The invention relates to the technical field of petrochemical engineering, in particular to a slurry bed residual oil hydrogenation vacuum overhead gas hydrogen enrichment and light hydrocarbon recovery method, which comprises the following steps: vacuum overhead gas is sucked out through a primary evacuator and a secondary vacuum overhead gas evacuating cooler, and enters the primary vacuum overhead gas evacuating cooler together with medium-pressure steam; condensed water formed by the cooled steam and vacuum top sump oil enter a vacuum top oil-water separator together, and the vacuum top sump oil and the condensed water are separated; the vacuum overhead gas sucked out by the second-stage evacuator is pressurized and then conveyed to a buffer tank at an inlet of a rich gas compressor through a water-sealed tank, and condensate and the vacuum overhead gas are separated; the vacuum overhead gas separated from the buffer tank at the inlet of the rich gas compressor enters the rich gas compressor, is boosted and then is sent to the absorption-desorption stable fractionation system for treatment, so that hydrogen and light hydrocarbon can be recycled respectively, the utilization rate of resources is improved, a desulfurization system of the vacuum overhead gas is removed, the operation fluctuation of a heating furnace is eliminated, and the energy consumption is reduced. And the pollution to the environment is reduced.

Description

Technical Field

[0001] The invention relates to the technical field of petrochemical industry, and in particular to a method for hydrogen enrichment and light hydrocarbon recovery of slurry bed residue oil hydrogenation and depletion of top gas. Background Art

[0002] Crude oil is becoming increasingly inferior, and it is crucial to make efficient use of heavy fractions in crude oil, such as vacuum residue produced by atmospheric vacuum. The processing of residue oil mainly adopts the decarbonization and hydrocracking technology routes. At present, the fixed bed residue oil hydrogenation process is widely used in industry, and the slurry bed residue oil hydrogenation process is less used in industry. The traditional fixed bed residue oil hydrogenation process has a low residue oil conversion rate, while the boiling bed residue oil hydrogenation and slurry bed residue oil hydrogenation processes have greatly improved the residue oil conversion rate compared with the traditional fixed bed residue oil hydrogenation. Compared with the fixed bed residue oil hydrogenation technology, the slurry bed residue oil hydrogenation technology can process lower-quality residue oil raw materials (metal (nickel + vanadium) mass fraction of more than 700 ug / g, residual carbon of more than 20%), and has a high conversion rate (more than 95%), which can achieve the maximum conversion of residue oil. Slurry bed residue oil hydrocracking treatment is an important oil refining process used to convert residue oil into lighter and better quality oil products. During the production process of the device, gases containing multiple components are produced at the top of the vacuum tower. These gases are usually directly burned as fuel gas in the heating furnace, which not only wastes resources but also pollutes the environment. Therefore, developing a technology to effectively recycle and utilize the vacuum tower top gas has important industrial value and environmental significance, and achieving maximum resource utilization and environmental protection has become a technical problem that needs to be solved urgently. Summary of the invention

[0003] The purpose of the present invention is to overcome the shortcomings of the prior art and propose a slurry bed residue oil hydrogenation and top gas hydrogen enrichment and light hydrocarbon recovery method, which can effectively recycle the hydrogen and hydrocarbons in the vacuum tower top gas, improve the effective utilization rate of resources and reduce environmental pollution.

[0004] The technical solution adopted by the present invention to solve the technical problem is: A method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed, comprising: The vacuum tower top gas uses medium-pressure steam as the power gas, and under the suction of the first-stage vacuum pump of the vacuum tower top gas, the vacuum top gas is sucked out and enters the first-stage vacuum top gas vacuum cooler together with the medium-pressure steam; the cooled steam becomes condensed water and the vacuum top waste oil and enters the vacuum top oil-water separator together; The pumped out top reduction gas is pumped out by the secondary evacuator of the top gas of the vacuum tower, and enters the secondary top reduction gas evacuation cooler together with the medium-pressure steam. The cooled steam becomes condensed water and the top reduction waste oil and enters the top reduction oil-water separator together; In the top reducing oil-water separator, the top reducing dirty oil and condensed water are separated respectively, and two-stage vacuuming is set to ensure the negative pressure at the top of the vacuum tower; The top-reducing gas sucked out by the secondary evacuator is pressurized by the top-reducing gas water ring vacuum pump, and then passes through the water seal tank to stabilize the top-reducing gas flow and pressure, and then is transported to the inlet buffer tank of the rich gas compressor to separate the condensate and the top-reducing gas; The top-reduced gas separated by the buffer tank at the inlet of the rich gas compressor enters the rich gas compressor, and after being pressurized by the rich gas compressor, is sent to the absorption and analysis stable fractionation system; The absorption tower in the absorption and analysis stable fractionation system carries out a physical absorption reaction of similar dissolution to absorb the light hydrocarbon components of the liquefied gas. The high-purity liquefied gas components are separated through distillation operations in the stripping section and the rectification section in the stabilization tower in the absorption and analysis stable fractionation system. The liquefied gas is further separated in the reflux tank at the top of the fractionation tower and sent to the liquefied gas finished product tank area to produce high value-added petrochemical products. The desorbed gas obtained by desorption in the desorption tower in the absorption and analysis stable fractionation system is absorbed in the absorption tower to form pre-desulfurization dry gas, and the desulfurized dry gas is separated out in the dry gas desulfurization tower and transported to the downstream PSA hydrogen production device. The PSA adsorption tower is filled with an adsorbent that selectively adsorbs impurity gases, thereby realizing the separation of hydrogen and impurity gases. The separated hydrogen is transported to the hydrogenation reaction unit and reused as supplementary hydrogen.

[0005] Furthermore, the evacuator is a steam jet evacuator.

[0006] Furthermore, the first-stage evacuator adopts three steam-jet evacuators, which are operated in parallel; the second-stage evacuator adopts three steam-jet evacuators, which are operated in parallel; and the third-stage evacuator adopts one steam-jet evacuator.

[0007] Furthermore, the top-reducing gas evacuation cooler is a top-reducing condensation cooler, and a circulating water cooler is used.

[0008] Furthermore, the first-stage top gas reduction vacuum cooler adopts three condensing coolers, which are matched with the first-stage vacuum cooler; the second-stage top gas reduction vacuum cooler adopts one condensing cooler, which is matched with the second-stage vacuum cooler; the third-stage top gas reduction vacuum cooler adopts one condensing cooler, which is matched with the third-stage vacuum cooler.

[0009] The present invention also provides another technical solution: A slurry bed residue oil hydrogenation and top gas depletion hydrogen-rich and light hydrocarbon recovery and processing system, used to implement the recovery method, the recovery system comprises a vacuum tower, a first-stage top gas depletion evacuator, a second-stage top gas depletion evacuator, a third-stage top gas depletion evacuator, a first-stage top gas depletion evacuation cooler, a second-stage top gas depletion evacuation cooler, a third-stage top gas depletion evacuation cooler, a top gas depletion oil-water separator, a top gas depletion water ring vacuum pump, a rich gas compressor inlet buffer tank and a rich gas compressor; the top of the vacuum tower is connected to the first-stage top gas depletion evacuator through a pipeline, the first-stage top gas depletion evacuator is connected to the first-stage top gas depletion evacuation cooler, the second-stage top gas depletion evacuator is connected to the first-stage top gas depletion cooler, the second-stage top gas depletion evacuator is connected to the second-stage top gas depletion evacuator The first-stage top gas reduction exhaust cooler is connected, the first-stage top gas reduction exhaust cooler and the second-stage top gas reduction exhaust cooler are both connected to the top gas reduction oil-water separator, the second-stage top gas reduction exhaust cooler is also connected to the top gas reduction water ring vacuum pump, the top gas reduction water ring vacuum pump is connected to a water seal tank, the water seal tank is connected to the rich gas compressor inlet buffer tank, the rich gas compressor inlet buffer tank is connected to the rich gas compressor, the rich gas compressor is connected to the absorption and analysis stable distillation system, the bottom of the rich gas compressor inlet buffer tank is connected to the light dirty oil tank, and the top of the rich gas compressor inlet buffer tank is connected with a venting pipeline; the first-stage top gas reduction exhaust device, the second-stage top gas reduction exhaust device and the third-stage top gas reduction exhaust device are all connected to the medium-pressure steam pipe.

[0010] Furthermore, a venting pipeline is connected to the top of the rich gas compressor inlet buffer tank.

[0011] Furthermore, the secondary top gas evacuation cooler is also connected to the tertiary top gas evacuator, the tertiary top gas evacuator is connected to the tertiary top gas evacuation cooler, and the tertiary top gas evacuation cooler is connected to the water seal tank. When the top gas water ring vacuum pump is in an accident state or maintenance state, the tertiary top gas evacuator is put into use to continue to pump the top gas, so as to maximize the negative pressure required at the top of the vacuum tower.

[0012] Furthermore, the bottom of the top-reducing oil-water separator is connected to a top-reducing dirty oil pump and a top-reducing condensate water pump, the top-reducing dirty oil pump is connected to an atmospheric tower inlet buffer tank, and the top-reducing condensate water pump is connected to an acidic water tank.

[0013] Technical effects of the present invention: Compared with the prior art, the method for hydrogenating and reducing top gas to enrich hydrogen and recover light hydrocarbons in a slurry bed residue oil is realized, and the separate recovery and utilization of hydrogen and light hydrocarbons is realized, which not only improves the utilization rate of resources, produces high value-added petrochemical products, reduces production costs, removes the desulfurization system of the vacuum tower top gas, but also eliminates the operating fluctuation of the heating furnace, reduces the pollution to the environment, and has significant economic and environmental benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1This is a structural block diagram of the slurry bed residue oil hydrogenation and top gas hydrogen enrichment and light hydrocarbon recovery system of the present invention.

[0015] In the figure, 1, vacuum tower; 2, first-stage degassing gas evacuator; 3, second-stage degassing gas evacuator; 4, third-stage degassing gas evacuator; 5, first-stage degassing gas evacuation cooler; 6, second-stage degassing gas evacuation cooler; 7, third-stage degassing gas evacuation cooler; 8, degassing oil-water separator; 9, degassing gas water ring vacuum pump; 10, rich gas compressor inlet buffer tank; 11, rich gas compressor; 12, water seal tank; 13, dry gas desulfurization tower; 14, light dirty oil tank; 15, venting pipeline; 16, medium-pressure steam pipe; 17, degassing dirty oil pump; 18, degassing condensate pump; 19, atmospheric tower inlet buffer tank; 20, acid water tank; 21, circulating water supply pipe; 22, circulating water return pipe ; 23. Absorption tower; 24. Desorption tower; 25. Stabilization tower; 26. Distillation tower; 27. PSA hydrogen production device; 28. Air cooler at the top of stabilization tower; 29. ​​Water cooler at the top of stabilization tower; 30. Reflux tank at the top of stabilization tower; 31. Reflux pipeline of stabilization tower; 32. Reflux pump of stabilization tower; 33. Vent pipeline of reflux tank of stabilization tower; 34. Acidic water discharge pipeline of stabilization tower; 35. Liquefied gas discharge pipeline; 36. Air cooler at the top of distillation tower; 37. Water cooler at the top of distillation tower; 38. Reflux tank at the top of distillation tower; 39. Reflux pipeline of distillation tower; 40 Reflux pump of distillation tower; 41. Vent pipeline of reflux tank of distillation tower; 42. Acidic water discharge pipeline of distillation tower; 43. Naphtha discharge pipeline. DETAILED DESCRIPTION

[0016] In order to make the purpose, technical solution and advantages of the embodiments of the present invention more clear, the technical solution in the embodiments of the present invention is clearly and completely described below in conjunction with the accompanying drawings.

[0017] Example like Figure 1 As shown, this embodiment relates to a slurry bed residue oil hydrogenation and top gas hydrogen enrichment and light hydrocarbon recovery method, comprising: The top gas of the vacuum tower 1 is used as the power gas by the medium-pressure steam. Under the suction of the first-stage vacuum pump of the top gas of the vacuum tower 1, the reduced top gas is sucked out and enters the first-stage reduced top gas vacuum cooler 5 together with the medium-pressure steam. The reduced top gas exchanges heat with the circulating water in the first-stage reduced top gas vacuum cooler 5, and the reduced top gas and the power steam are cooled together to form condensed water, reduced top waste oil and low-temperature reduced top gas. The condensed water and the reduced top waste oil enter the reduced top oil-water separator 8 together; The sucked out top gas is sucked out by the secondary top gas evacuator of the vacuum tower 1, and enters the secondary top gas evacuation cooler 6 together with the medium-pressure steam. The cooled steam becomes condensed water and the top waste oil and enters the top oil-water separator 8 together. In the top oil-water separator 8, the top waste oil and condensed water are separated, and two stages of vacuuming are set to ensure the negative pressure at the top of the vacuum tower 1; The reduced top gas sucked out by the secondary evacuator is pressurized by the reduced top gas water ring vacuum pump 9, passes through the water seal tank 12 to stabilize the reduced top gas flow and pressure, and then is transported to the rich gas compressor inlet buffer tank 10 to separate the condensate and the reduced top gas to achieve further gas-liquid separation; The reduced top gas, together with the top oil and gas of the atmospheric tower inlet buffer tank 19 and the top oil and gas of the acid water tank 20, enters the rich gas compressor buffer tank 10 for further separation, and after being pressurized by the rich gas compressor 11, is sent to the absorption and analysis stable fractionation system; In the absorption tower 23 of the absorption and analysis stable fractionation system, a similar phase-soluble physical absorption reaction is carried out to absorb the light hydrocarbon components of the liquefied gas. In the stabilization tower 25 of the absorption and analysis stable fractionation system, a high-purity liquefied gas component is separated through distillation operations in the stripping section and the rectifying section. The liquefied gas is then further separated in the top reflux tank of the fractionation tower 26 and sent to the liquefied gas finished product tank area to produce high value-added petrochemical products. In the desorption tower 24 of the absorption and analysis stable fractionation system, the desorbed gas obtained by desorption is absorbed by the absorption tower 23 to form a pre-desulfurization dry gas, and the desulfurized dry gas is separated by the dry gas desulfurization tower 13 and transported to the downstream PSA hydrogen production device 27. The PSA adsorption tower is filled with an adsorbent that selectively adsorbs impurity gases, thereby realizing the separation of hydrogen and impurity gases. The separated hydrogen is transported to the hydrogenation reaction unit and reused as supplementary hydrogen.

[0018] Specifically, if Figure 1 As shown, the top of the stabilization tower 25 is connected to the stabilization tower top air cooler 28, the stabilization tower top water cooler 29, and the stabilization tower top reflux tank 30 in sequence, and the bottom of the stabilization tower top reflux tank 30 is connected to the liquefied gas discharge pipeline 35. The liquefied gas discharge pipeline 35 is provided with a stabilization tower reflux pump 32 to transport the liquefied gas to the liquefied gas finished product tank area; the side of the stabilization tower 25 is connected to the liquefied gas discharge pipeline 35 through the stabilization tower reflux pipeline 31; the top of the stabilization tower top reflux tank 30 is provided with a stabilization tower reflux tank venting pipeline 33, and the bottom is provided with a stabilization tower acid water discharge pipeline 34 to transport the acid water to the acid water tank. The top of the fractionation tower 26 is connected to the fractionation tower top air cooler 36, the fractionation tower top water cooler 37, and the fractionation tower top reflux tank 38 in sequence. The bottom of the fractionation tower top reflux tank 38 is connected to the naphtha discharge pipeline 43. The naphtha discharge pipeline 43 is provided with a fractionation tower reflux pump 40 to transport the naphtha to the naphtha finished product tank area; the side of the fractionation tower 26 is connected to the naphtha discharge pipeline 43 through the fractionation tower reflux pipeline 39; the top of the fractionation tower top reflux tank 38 is provided with a fractionation tower reflux tank venting pipeline 41, and the bottom is provided with a fractionation tower acid water discharge pipeline 42 to transport the acid water to the acid water tank.

[0019] The evacuator is a steam jet evacuator, which uses water vapor as the evacuation medium to obtain vacuum. Steam of a certain pressure is ejected at supersonic speed through the Laval nozzle, and the pressure energy is converted into velocity energy. At the nozzle outlet, low pressure is formed due to the injection effect of the high-speed steam flow. The working steam and the evacuated air flow are mixed in the mixing chamber and energy exchange is carried out. The mixed air flow is decelerated and pressurized in the diffuser. Specifically, the first-stage evacuator adopts three steam jet evacuators, which are operated in parallel. The design loads of the three steam jet evacuators are 70%, 50%, and 30% of their operating loads respectively; the second-stage evacuator adopts three steam jet evacuators, which are operated in parallel. The design loads of the three steam jet evacuators are 70%, 50%, and 30% of their operating loads respectively; the third-stage evacuator adopts one steam jet evacuator. At the same time, the third-stage evacuator is equipped with one steam jet evacuator as a backup, and the design load is 120% of the operating load.

[0020] The reduced top gas evacuation cooler is a reduced top condensation cooler, and both use circulating water coolers. Specifically, the first-stage reduced top gas evacuation cooler 5 uses three condensation coolers, and the capacities match the first-stage evacuator, which are 70%, 50%, and 30% respectively; the second-stage reduced top gas evacuation cooler 6 uses one condensation cooler, and the capacity matches the second-stage evacuator, which is 150%; the third-stage reduced top gas evacuation cooler 7 uses one condensation cooler, which matches the third-stage evacuator, and the capacity is 120%.

[0021] In the top-reducing oil-water separator 8, due to the different densities of the oil and water phases, the top-reducing dirty oil and condensed water are separated. The top-reducing dirty oil is transported to the atmospheric tower inlet buffer tank 19 through the top-reducing dirty oil pump 17. The oil in the atmospheric tower inlet buffer tank 19 enters the atmospheric tower to separate a small amount of light hydrocarbons and some heavy hydrocarbons, such as naphtha, diesel, etc. The condensed water is pressurized by the top-reducing condensate pump 18 and transported to the acid water tank 20. When adjusting the oil phase and water phase liquid levels in the top-reducing oil-water separator 8, the relationship between the two-phase liquid levels and the pump outlet flow can be set in series so that the oil phase and water phase liquid levels are stable.

[0022] The medium-pressure steam pressure described in this embodiment is controlled at 1.0-1.5MPa, and the temperature is controlled at 210-330°C; the top pressure of the vacuum tower 1 is controlled at 0-5KPa (A), and the temperature is controlled at 45-60°C; the oil phase liquid level of the top-reducing oil-water separator 8 is controlled at 30-80%, and the water phase liquid level is controlled at 30-70%; the flow rate of the top-reducing gas to the rich gas compressor inlet buffer tank 10 is controlled at 300-1200Nm3 / h; the liquid level of the rich gas compressor inlet buffer tank 10 is controlled at 3-10%; the inlet pressure of the rich gas compressor 11 is controlled at 0.03-0.06MPa, and the outlet pressure is controlled at 1.0-1.4MPa.

[0023] The components separated by chemical analysis in this embodiment are shown in Table 1: Table 1 Composition of vacuum tower top gas

[0024] The present invention can separate the top gas of the slurry bed residue oil hydrocracking vacuum tower 1 through a reasonably optimized process flow and equipment combination, effectively recover hydrogen and light hydrocarbons, improve the utilization rate of hydrogen, reduce waste gas emissions, and have good economic and environmental benefits. The present invention can recover more than 90% of the hydrogen components in the reduced top gas, reduce the demand for external hydrogen, and reduce production costs; a stable hydrogen supply helps to improve the operating stability and product quality of the hydrocracking unit. The present invention can remove the top gas of the vacuum tower 1 as fuel gas for the heating furnace, reduce pollution to the environment, and achieve the effect of energy conservation and emission reduction. The present invention removes the desulfurization system of the top gas of the vacuum tower 1, saving a lot of production costs.

[0025] The present invention removes the desulfurization system of the vacuum tower top gas, eliminates the operation fluctuation of the heating furnace, reduces the pollution to the environment, and has significant economic and environmental benefits. The desulfurization system of the vacuum tower top gas removed includes the equipment and corresponding pipelines as shown in Table 2: Table 2 Saving equipment and materials

[0026] Embodiment 2: like Figure 1 As shown, this embodiment relates to a processing system for a slurry bed residue oil hydrogenation and top gas hydrogen enrichment and light hydrocarbon recovery method, which is used to implement the recovery method described in Example 1, and the recovery system includes a vacuum tower 1, a first-stage top gas evacuator 2, a second-stage top gas evacuator 3, a third-stage top gas evacuator 4, a first-stage top gas evacuation cooler 5, a second-stage top gas evacuation cooler 6, a third-stage top gas evacuation cooler 7, a top gas oil-water separator 8, a top gas water ring vacuum pump 9, a rich gas compressor inlet buffer tank 10 and a rich gas compressor 11.

[0027] The top of the vacuum tower 1 is connected to the first-level top gas evacuator 2 through a pipeline, the first-level top gas evacuator 2 is connected to the first-level top gas evacuation cooler 5, the second-level top gas evacuator 3 is connected to the first-level top gas evacuation cooler 5, the second-level top gas evacuator 3 is connected to the second-level top gas evacuation cooler 6, the first-level top gas evacuation cooler 5 and the second-level top gas evacuation cooler 6 are both connected to the top oil-water separator 8, the second-level top gas evacuation cooler 6 is also connected to the top gas water ring vacuum pump 9, the top gas water ring vacuum pump 9 is connected to the water seal tank 12, the water seal tank 12 is connected to the rich gas compressor inlet buffer tank 10, the rich gas compressor inlet buffer tank 10 is connected to the rich gas compressor 11, the rich gas compressor 11 is connected to the absorption and analysis stable fractionation system, the bottom of the rich gas compressor inlet buffer tank 10 is connected to the light dirty oil tank 14, and the top of the rich gas compressor inlet buffer tank 10 is connected with a venting pipeline 15. The first-stage top gas reducing evacuator 2 , the second-stage top gas reducing evacuator 3 and the third-stage top gas reducing evacuator 4 are all connected to the medium-pressure steam pipe 16 .

[0028] The secondary top gas evacuation cooler 6 is also connected to the tertiary top gas evacuator 4, the tertiary top gas evacuator 4 is connected to the tertiary top gas evacuation cooler 7, and the tertiary top gas evacuation cooler 7 is connected to the water seal tank 12. When the top gas water ring vacuum pump 9 is in an accident state or a maintenance state, the tertiary top gas evacuator 4 is put into use to continue to pump the top gas to maximize the negative pressure required at the top of the vacuum tower 1. The bottom of the top gas oil-water separator 8 is connected to the top waste oil pump 17 and the top condensate pump 18, the top waste oil pump 17 is connected to the atmospheric tower inlet buffer tank 19, and the top condensate pump 18 is connected to the acid water tank 20. The primary top gas evacuation cooler 5, the secondary top gas evacuation cooler 6, and the tertiary top gas evacuation cooler 7 are all connected to the circulating water upper water pipe 21 and the circulating water return water pipe 22.

[0029] The above-mentioned specific implementation modes are only specific cases of the present invention. The patent protection scope of the present invention includes but is not limited to the above-mentioned specific implementation modes. Any appropriate changes or modifications made thereto by any ordinary technician in the technical field in accordance with the claims of the present invention shall fall within the patent protection scope of the present invention.

Claims

1. A method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed, characterized in that: include: The vacuum tower top gas uses medium-pressure steam as the power gas, and under the suction of the first-stage vacuum pump of the vacuum tower top gas, the vacuum top gas is sucked out and enters the first-stage vacuum top gas vacuum cooler together with the medium-pressure steam; the cooled steam becomes condensed water and the vacuum top waste oil and enters the vacuum top oil-water separator together; The pumped out top reduction gas is pumped out by the secondary evacuator of the top gas of the vacuum tower, and enters the secondary top reduction gas evacuation cooler together with the medium-pressure steam. The cooled steam becomes condensed water and the top reduction waste oil and enters the top reduction oil-water separator together; In the top-reducing oil-water separator, the top-reducing dirty oil and condensed water are separated into two phases; The top-reducing gas sucked out by the secondary evacuator is pressurized by the top-reducing gas water ring vacuum pump, and then passes through the water seal tank to stabilize the top-reducing gas flow and pressure, and then is transported to the inlet buffer tank of the rich gas compressor to separate the condensate and the top-reducing gas; The top-reduced gas separated by the buffer tank at the inlet of the rich gas compressor enters the rich gas compressor, and after being pressurized by the rich gas compressor, is sent to the absorption and analysis stable fractionation system; The absorption tower in the absorption and analysis stable fractionation system carries out a physical absorption reaction of similar dissolution to absorb the light hydrocarbon components of the liquefied gas. The liquefied gas components are separated through distillation operations in the stripping section and the rectification section in the stabilization tower in the absorption and analysis stable fractionation system. The liquefied gas is further separated in the reflux tank at the top of the fractionation tower and sent to the liquefied gas finished product tank area. The desorbed gas obtained by desorption in the desorption tower in the absorption and analysis stable fractionation system is absorbed in the absorption tower to form pre-desulfurization dry gas, and the desulfurized dry gas is separated out through the dry gas desulfurization tower and transported to the downstream PSA hydrogen production device. The PSA adsorption tower is filled with an adsorbent that selectively adsorbs impurity gases to achieve separation of hydrogen and impurity gases. The separated hydrogen is transported to the hydrogenation reaction unit and reused as supplementary hydrogen.

2. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 1, characterized in that: The evacuator is a steam jet evacuator.

3. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 2, characterized in that: The first-stage vacuum pump adopts three steam-jet vacuum pumps, which are operated in parallel; the second-stage vacuum pump adopts three steam-jet vacuum pumps, which are operated in parallel; and the third-stage vacuum pump adopts one steam-jet vacuum pump.

4. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 1, characterized in that: The reduced top gas evacuation cooler is a reduced top condensation cooler, and both use a circulating water cooler.

5. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 4, characterized in that: The first-stage top gas reduction vacuum cooler adopts three condensing coolers, which are matched with the first-stage vacuum cooler; the second-stage top gas reduction vacuum cooler adopts one condensing cooler, which is matched with the second-stage vacuum cooler; the third-stage top gas reduction vacuum cooler adopts one condensing cooler, which is matched with the third-stage vacuum cooler.

6. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to any one of claims 1 to 5, characterized in that: A hydrogen-rich and light hydrocarbon recovery system based on slurry bed residue oil hydrogenation and top gas reduction is realized, and the recovery system comprises a vacuum tower, a first-stage top gas reduction evacuator, a second-stage top gas reduction evacuator, a third-stage top gas reduction evacuator, a first-stage top gas reduction evacuation cooler, a second-stage top gas reduction evacuation cooler, a third-stage top gas reduction evacuation cooler, a top gas reduction oil-water separator, a top gas reduction water ring vacuum pump, a rich gas compressor inlet buffer tank and a rich gas compressor; the top of the vacuum tower is connected to the first-stage top gas reduction evacuator through a pipeline, the first-stage top gas reduction evacuator is connected to the first-stage top gas reduction evacuation cooler, the second-stage top gas reduction evacuator is connected to the first-stage top gas reduction evacuation cooler, the second-stage top gas reduction evacuator is connected to the second-stage top gas reduction The first-stage degassing gas degassing cooler and the second-stage degassing gas degassing cooler are both connected to the degassing oil-water separator, the second-stage degassing gas degassing cooler is also connected to the degassing gas water ring vacuum pump, the degassing gas water ring vacuum pump is connected to a water seal tank, the water seal tank is connected to the rich gas compressor inlet buffer tank, the rich gas compressor inlet buffer tank is connected to the rich gas compressor, the rich gas compressor is connected to the absorption and analysis stable fractionation system, the bottom of the rich gas compressor inlet buffer tank is connected to the light dirty oil tank, and the top of the rich gas compressor inlet buffer tank is connected with a venting pipeline; the first-stage degassing gas degassing evacuator, the second-stage degassing gas degassing evacuator and the third-stage degassing gas degassing evacuator are all connected to the medium-pressure steam pipe.

7. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 6, characterized in that: A venting pipeline is connected to the top of the rich gas compressor inlet buffer tank.

8. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 6, characterized in that: The second-stage top gas reduction evacuation cooler is also connected to the third-stage top gas reduction evacuation cooler, the third-stage top gas reduction evacuation cooler is connected to the third-stage top gas reduction evacuation cooler, and the third-stage top gas reduction evacuation cooler is connected to the water seal tank.

9. The method for hydrogen enrichment and light hydrocarbon recovery of residue oil by hydrogenation and depletion of top gas in a slurry bed according to claim 6, characterized in that: The bottom of the top-reducing oil-water separator is connected to a top-reducing dirty oil pump and a top-reducing condensate water pump. The top-reducing dirty oil pump is connected to an atmospheric tower inlet buffer tank, and the top-reducing condensate water pump is connected to an acidic water tank.

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