CN110760332A - A system for enhanced swirl removal of sulfides in oil - Google Patents

Abstract

The invention belongs to the fields of petrochemical industry and environmental protection, and relates to a system for performing adsorption desulfurization and adsorbent synchronous separation treatment on oil products. The desulfurization method of the system comprises the following steps: step (1) adsorption desulfurization; step (2) separation of adsorbent; step (3) regeneration of adsorbent. Based on the strong adsorption effect between the adsorbent material and the thiophene sulfide, the invention can quickly and efficiently adsorb the sulfide in the oil product under the strengthening effect of the swirl field; at the same time, the adsorbent can be quickly removed from the oil product in the cyclone High-efficiency separation; the separated adsorbent is recovered and recycled by oxidation or extraction regeneration. The system of the invention has the characteristics of rapid adsorption and high-efficiency separation, the operation of the regenerated adsorbent is simple, the equipment operation is simple, the floor area is small, and the traditional hydrodesulfurization high temperature and high pressure and subsequent amine absorption and desulfurization are avoided. The complicated process, high cost and control requirements It can be widely used in oil desulfurization treatment process.

Description

A system for enhanced swirl removal of sulfides in oil

The application of the present invention is the title: A system for swirl enhanced removal of sulfides in oil products, the parent application number: 201710621811.7 The parent application is a child application of the application date of 2017-7-27.

technical field

The invention belongs to the fields of petrochemical industry and environmental protection, and relates to a system for performing adsorption desulfurization and adsorbent synchronous separation treatment on oil products.

Background technique

Petroleum products contain a large amount of sulfide, which will be oxidized and converted into SO _x emissions during the combustion process, forming smog, acid rain, etc., causing huge damage to the environment and ecological balance. At the same time, the presence of sulfides in the oil also deteriorates the quality of the fuel, corrodes the equipment, and causes safety hazards to the oil processing technology. In order to achieve cleaner fuel oil products, countries around the world have formulated a series of fuel oil sulfur content standards, in order to limit sulfur emissions in fuel oil. Developed countries in Europe and the United States and my country's gasoline and diesel national V and national VI standards clearly stipulate that the sulfur content is less than 10ppm. It is a global trend to deeply desulfurize fuel oil to make ultra-clean fuel oil with sulfur content below 10ppm.

The sulfur compounds in petroleum distillate products of different distillation ranges have obvious distribution rules: element sulfur and mercaptans with lower molecular weight and easier removal are mainly distributed in light fractions with lower boiling point (<280°C); Large and difficult to remove aromatic heterocyclic sulfides such as benzothiophene (BT, boiling point of 220 °C), dibenzothiophene (DBT, boiling point of 320 °C) are mainly distributed in higher boiling points ( >280°C), and as the distillation range temperature of the product fraction increases, the content of organic sulfur compounds with high boiling point, large molecular weight and difficult to remove will also increase accordingly. Therefore, it is extremely important for the removal of thiophene sulfur and its complex derivatives in petroleum products.

At present, the relatively mature and widely used desulfurization method in the oil refining industry is hydrodesulfurization. This technology can effectively remove most of the small molecular sulfides in the fuel oil, such as mercaptans, sulfides, disulfides, etc. For organic thiophene sulfur, the reaction has a certain limit. At the same time, because the hydrodesulfurization equipment is expensive and the process is complicated; the reaction process requires the use of precious metal catalysts, which are easy to deactivate; the operating conditions are severe and require high temperature and high pressure; and it will cause a certain loss of octane number. With the increasing demand, it is imperative to develop high-efficiency non-hydrodesulfurization technology based on traditional hydrodesulfurization technology.

Adsorption desulfurization is to use physical or chemical adsorption to enrich the sulfur in fuel oil into the surface and pores of adsorbent materials to achieve desulfurization. The normal temperature and normal pressure method has mild operating conditions, low cost, and environmental protection, and is considered to be a potential deep desulfurization method. In the process of adsorption desulfurization, the enhancement of the adsorption of thiophene sulfur by the adsorbent and the enhancement of the liquid-solid separation of oil/adsorbent are the problems that need to be solved urgently in the development of this technology.

There are many kinds of adsorbent materials reported [RSC Advances, 2014, 4:35302–35317, Chem SocRev, 2009,38(5):1284–1293], mainly including modified molecular sieves, such as Ag ₂ O developed by Chen Biaohua et al. /NaY (patent number: CN 103191697A), metal oxide/activated carbon composite (patent number: CN 104028208A) developed by Jin Minglin, etc., metal oxide mixture (patent number: CN 103721668A) developed by Li Can, etc., and other new Porous material (patent number: CN 106000297A). Among them, metal-organic frameworks (MOFs) have special structures, which can improve the adsorption performance of sulfur with organic sulfur through acid-base interaction, π complexation, open metal sites (MS bonds) and other interactions, and are expected to become excellent desulfurization adsorption. agent. Improving the pore structure of the adsorbent material, regulating the surface adsorption activity of the adsorbent material, thereby increasing the selective adsorption desulfurization capacity and adsorption rate, and improving the stability and regeneration performance of the adsorbent material are one of the keys to the adsorption desulfurization technology. The currently adopted adsorption process mainly includes fixed bed (patent number: CN104277877A) and fluidized bed (patent number: CN 102839011A), and a new combination method (patent number: CN 105623733A), which has relatively low energy efficiency and small product oil. Some engineering problems such as the entrainment of adsorbent particles have caused great hidden dangers to the work efficiency of engines in the subsequent use of oil products.

The swirl field can continuously collide and rotate between the adsorbent particles and the oil, thereby strengthening the dynamic adsorption. At the same time, the cyclone separation can directionally aggregate the fine adsorbent particles and separate them from the oil. In addition, in view of the high efficiency of the cyclone for the separation of fine particles, the adsorbent can use fine particles, thereby reducing the mass transfer resistance in the adsorption process and further enhancing the adsorption rate, so the cyclone technology is a very potential adsorption A new process coupled with liquid-solid separation. So far, a synergistic system that can effectively realize adsorption desulfurization and adsorbent separation has not been developed in the field, so it is very urgent to develop a new oil desulfurization system with high efficiency, practicability and economy.

SUMMARY OF THE INVENTION

The invention provides a system for strengthening the removal of sulfides in oil products by cyclone, so as to solve the problems existing in the prior art.

The specific technical scheme of the present invention is: a system for strengthening the removal of sulfides in oil products by swirl flow, and the desulfurization method of the system comprises the following steps:

Step (1) Adsorption desulfurization: the adsorbent adsorbs the sulfide in the oil; the adsorbent and the oil are added to the premixed adsorption unit and the liquid-solid suspension conveying unit, and mixed evenly, wherein the premixed adsorption unit includes a belt. The agitated sealed kettle completes mixing and adsorption here; the adsorbent is fully contacted with the sulfide in the oil for adsorption; then it is transported into the swirl system through the material pump;

Step (2) Separation of adsorbent: Separation of fine adsorbent particles by cyclone method; oil product containing adsorbent enters the liquid-solid separation cyclone system unit, and operating parameters such as inlet flow rate and split ratio are adjusted to make the adsorbent particles in the micro-cyclone flow. The rotation and revolution in the field further strengthen the adsorption desulfurization, and at the same time realize the liquid-solid separation of the fine particles of the adsorbent. The low-sulfur refined oil is obtained from the overflow port, and the mixture of high-solid content adsorbent and oil product obtained from the underflow port is partially returned to be mixed for use, and part of it enters the regeneration system;

The liquid-solid separation cyclone system unit includes a single-stage or two-stage series cyclone; wherein the first cyclone of the series system is provided with an inlet to receive the mixed liquid at the outlet of the mixed adsorption unit, and an overflow port to discharge a cyclone. The oil product after stage separation, an underflow port to discharge the adsorbent after the first stage separation; the oil product discharged from the overflow port enters the second cyclone for secondary separation, and an inlet is provided to accept the first cyclone The oil discharged from the overflow port, an overflow port to discharge the oil after secondary separation, and an underflow port to discharge the adsorbent after secondary separation;

Step (3) Regeneration of adsorbent: according to the mechanism of oxidative desulfurization, add the adsorbent adsorbed with thiophene sulfur into oxidant, oxidize thiophene sulfur into sulfone, and then wash with water to dissolve and elute the sulfone; or according to the principle of extraction, use organic The solvent dissolves and removes the adsorbed sulfur; after drying, a regenerated adsorbent is obtained, which is added to the adsorbent recovery and regeneration unit for recycling;

The adsorbent recovery and regeneration unit includes a roller centrifugal filter separation kettle with a feeding port, an oxidant solution or extractant solution storage tank and a solvent recovery tank; the adsorbent and oil discharged from the bottom flow port of the cyclone are separated, and an oxidant is added. The solution or extractant is used for oxidative regeneration or extraction regeneration of the adsorbent.

Further, the liquid-solid suspension conveying unit adopts a mud pump.

Further, the adsorbent selected in the step (1) is Y-type molecular sieve, 13X molecular sieve, mesoporous molecular sieve, activated carbon, metal organic framework material MOFs, porous organic polymer POPs, polyporous ionic liquid PILs, etc.

Further, the adsorption saturated sulfur capacity of the adsorbent selected in the step (1) is 15-40 g/kg.

Further, the specific surface agent of the adsorbent selected in the step (1) is 150-1800m2/g, the pore volume is 0.35-1.1cm3/g, the density is 1.5-2.5g/cm3, and the average particle size is greater than 30um.

Further, the premixing kettle in the step (1) is stirred, which can realize liquid-solid homogenization and mixing, and both the premixing kettle and the conveying system are sealed.

Further, the cyclone separation system in the step (2) may be a single-stage cyclone with a cone angle of 5°-25°.

Further, the cyclone separation system in the step (2) can also combine the cyclones in two stages in series. It is carried out by means of small-angle cyclone in series with large-angle cyclone, large-angle cyclone in series with small-angle cyclone, and equal-angle cyclone in series.

Further, in the adsorption cyclone separation process of the step (2), the particle concentration of the feed adsorbent is 2%-10%, the inlet flow rate is 0.2-1.0m3/h, and the split ratio between the underflow port and the overflow port is 5%. -12%.

Further, the ratio of backmixing and regeneration of the high solid content adsorbent and the oil product mixture obtained from the underflow port of the step (2) is 1:3-1:1.

Further, in order to meet the treatment capacity requirement in the adsorption cyclone separation process of the step (2), the cyclone system can be used to perform parallel multiple groups.

Further, the regeneration of the adsorbent in the step (3) is carried out in batches; oil products are first filtered and separated by a centrifugal kettle, and then oxidized or regenerated by extraction; the oil products obtained by separation are low-sulfur refined oil.

Further, in the oxidative regeneration of the adsorbent described in the step (3), H2O2, NaClO, etc. are used as oxidizing agents, and according to the adsorption sulfur capacity (n mol/g), the dosage of the oxidizing agent is (1-3) times n mol/g. adsorbent.

Further, in the oxidative regeneration of the adsorbent described in the step (3), an oxidant is added to the adsorbent for removing oil products to react for 5-10 minutes, centrifugal filtration, and then rinsed and filtered with water, and repeated three times.

Further, the extraction and regeneration of the adsorbent described in the step (3) can be extracted and washed with solvents such as toluene, xylene, and petroleum ether. The amount of extractant is 3-5L/kg adsorbent, and the filtration is repeated three times.

Further, after the adsorbent described in the step (3) is regenerated by oxidation or extraction, it is dried at 120-150 degrees for recycling.

Further, in the unit-two cyclone separation system, according to the processing capacity, a plurality of two-stage series-connected cyclone units are selected for parallel operation.

Further, the unit 2 cyclone separation system unit includes two secondary separation sections of cyclones, each section is provided with a flow control valve and a pressure gauge, and a collector and a liquid level gauge are provided at the adsorbent outlet.

Further, in the unit three adsorbent recovery and regeneration unit, the extraction solvent and the washing solvent can be selected and used for secondary purification according to the requirements of environmental protection.

beneficial effect

The adsorption and separation system adopted in the system of the invention is firstly based on the strong adsorption effect between the adsorption material and the organic sulfide, and can quickly and efficiently adsorb the sulfide in the oil under the strengthening effect of the cyclone field; The oil can be quickly and efficiently separated from the oil in the flow device; the separated adsorbent can be recovered and recycled by oxidation or extraction regeneration. In a preferred embodiment, when the thiophene sulfur-containing oil is subjected to adsorption desulfurization-cyclone separation by using HKUST-1 with a mass fraction of 5%, the sulfur content in the exported oil is less than 10 ppm, and the separation of adsorbent HKUST-1 particles The efficiency is over 99%, and the processing cycle is less than 1 minute.

The system of the invention has the characteristics of rapid adsorption and high-efficiency separation, the operation of the regenerated adsorbent is simple, the equipment operation is simple, the floor area is small, and the traditional hydrodesulfurization high temperature and high pressure and subsequent amine absorption and desulfurization are avoided. The complicated process, high cost and control requirements It can be widely used in oil desulfurization treatment process.

Description of drawings

Accompanying drawing 1 is a schematic diagram of a cyclone-enhanced oil desulfurization system.

Symbol Description:

1 stirring premix kettle; 2 primary cyclone; 3 secondary cyclone; 4 centrifugal filter kettle;

5 oxidant or extractant storage tank; 6 buffer tank; 7 mud pump; 8 liquid transfer pump.

Detailed ways

There are many factors affecting adsorption desulfurization efficiency, such as adsorbent type, adsorbent pore structure and surface composition, sulfur concentration in oil, adsorbent dosage, adsorption time, adsorption temperature, etc.; factors affecting cyclone separation include cyclone structure , cyclone series connection, inlet flow rate, split ratio, density difference between adsorbent and oil, adsorbent particle size distribution, temperature, etc.; factors affecting adsorbent regeneration include oxidant (extractant) type, oxidant (extractant) addition Dosage, oxidation (extraction) time, oxidation (extraction) temperature, etc. The present invention will be described in detail below with reference to specific embodiments. The examples are only used to illustrate the present invention and do not limit the scope of the present invention. The method and device for the adsorption and removal of sulfide in oil products and the cyclone separation of adsorbents in the present invention have similar treatment methods and principles for different adsorbents and different oil products. Therefore, for the convenience of description, this specification mainly provides a brief description by taking the novel porous organic framework material HKUST-1 for the adsorption and removal of dibenzothiophene sulfur in oil products as an example. The test methods that do not specify specific conditions in the following examples are generally in accordance with conventional conditions.

Example 1 Analysis of sulfur content

Take 1 microliter of oil containing a certain amount of dibenzothiophene sulfur and add it to gas chromatography, the detector is a flame photometric detector (FPD), and the chromatography column is a capillary column (HP-5, 15m×0.53mm×1.5μm). The carrier gas was nitrogen, the column temperature was 200 degrees, the vaporization temperature was 340 degrees, the FPD temperature was 340 degrees, the column pressure was 0.1 MPa, the air flow was 50 ml/min, and the hydrogen flow was 40 ml/min. The desulfurization amount can be calculated by formula (1):

where q _t represents the amount of sulfur adsorbed by the adsorbent (unit: g sulfur/kg adsorbent, gS/kg), V represents the model oil volume (milliliter, mL), M represents the mass of the adsorbent (g, g), M _WA represents the molecular weight of dibenzothiophene, M _WS represents the sulfur molecular weight, and C ₀ and C _i (mg sulfur/liter, mgS/L) represent the sulfide concentration in the simulated oil before and after adsorption, respectively.

Example 2 The adsorption performance of HKUST-1 for dibenzothiophene

The self-scaled synthesis of HKUST-1 was used as the adsorbent. Its main property parameters are: the specific surface area is 1500m ² g ^-1 , the pore volume is 0.5cm ³ g ^-1 , the average pore diameter is 1.2nm, the average particle size is about 30um, and the skeleton density is about 2.10g cm ^-3 . The adsorbent HKUST-1 powder was activated in a 150-degree oven for 4 hours to remove impurities and moisture adsorbed in its pores. The activated HKUST-1 powder was added to a sealed container storing oil, and the mixture was evenly mixed. The oil had a density of 0.75g cm ^-3 and a viscosity of 1.43cp. After a certain period of adsorption at 25°C, the adsorbent HKUST-1 and the oil were centrifuged, and 1 microliter of the upper clear oil was taken and injected into the gas chromatography, and the sulfur content was analyzed by a flame photometric detector. The changes of the adsorption amount with time were obtained, and the results are shown in Table 1. It can be seen that the adsorption rate is very fast, and the adsorption equilibrium is reached within 1 minute. By changing the initial dibenzothiophene concentration (10ppm-500ppm) in the oil, the variation of the adsorption capacity with the equilibrium concentration was obtained. The results are shown in Table 2, and the equilibrium saturated adsorption capacity of HKUST-1 was calculated to be as high as 33gS/kg adsorbent.

Table 1. Variation of adsorption capacity with time at 25 degrees

Table 2. Variation of adsorption capacity with equilibrium concentration at 25 degrees

Example 3 Determination of solid-liquid separation efficiency and optimal working area of single-stage cyclone system with a cone angle of 8 degrees

The solid-liquid separation efficiency and the optimal working area of the cyclone system were determined by the clear water experiment, and a simulated solid ^- liquid system with glass powder as the solid phase and water as the liquid phase was used. about 35 microns.

Correctly assemble each interface and valve of the single-stage cyclone separation system with a cone angle of 8 degrees. Before the test, the system is cleaned, emptied, and confirmed to be dry before the formal test. Inject more than 1/3 of the volume of water into the feed tank, and adjust the various valve nodes required by the working conditions. Start the mud pump, adjust the valve to take the inlet pressure as the adjustment parameter, and keep other working parameters (including temperature, flow rate, split ratio, etc.) stable.

The glass powder was added to the feeding tank according to the mass fraction of 2%, 4% and 8%, mixed evenly, and the system was preheated until the material temperature was constant at 25 degrees. Turn on the pump to run, adjust each valve according to the required working conditions, and send the glass powder-water mixed liquid from the mud pump into the cyclone separation system. After the system runs stably, samples are taken from the inlet, overflow port and underflow port of the cyclone, and the solid content of the liquid mixture of each sample is analyzed separately. Among them, the solid content analysis adopts gravimetric analysis method: vacuum filtration is performed on the sampling suspension sample, wherein the filter membrane is a nylon (Nylon) disc filter membrane (pore size is 0.22 microns). After drying the collected solid samples, the outlet solid content under each working condition was calculated.

The regulation of the feed concentration, inlet flow and split ratio of the cyclone system has a significant impact on the separation efficiency of the 8-degree single-stage cyclone. For low solid content, such as 2%, the inlet flow rate in the optimal working area is 0.8-1.0 m ³ h ^-1 , the split ratio is 8-12%, and the separation efficiency is 71.2%. The higher the concentration, the lower the separation efficiency.

Example 4 Determination of solid-liquid separation efficiency and optimal working area of single-stage cyclone system with a cone angle of 22 degrees

Similar to Example 3, the separation efficiency and optimal working area of the single-stage cyclone system with a cone angle of 22 degrees were tested. The glass beads were added to the feed tank according to the mass fraction of 4%, 8% and 10%. Mix well, preheat the system until the material temperature is constant at 25 degrees. Turn on the pump to run, and take samples from the inlet, overflow port and underflow port of the cyclone. The influence of the control of the feed concentration, inlet flow and split ratio of the cyclone system on the separation efficiency of the 22-degree single-stage cyclone was investigated. For a solid content of 8%, the flow rate in the optimal working range was 0.5-0.6m ³ h ^{- 1} , the split ratio is 12%, and its separation efficiency is 65%. The lower the concentration, the higher the separation efficiency, and vice versa, the separation efficiency is reduced.

Embodiment 5 Determination of solid-liquid separation efficiency of two-stage series cyclone system

Connect a single cyclone in series to form a large-angle cone-angle cyclone in series with a small-angle cone-angle cyclone (such as 22-8), or a small-angle cone-angle cyclone in series with a large-angle cone-angle cyclone (8-22 ) of the secondary cyclone separation system. The liquid discharged from the overflow port of the first cyclone flows into the second cyclone for secondary separation, and the liquid obtained from the overflow port of the second cyclone is the separation product. Samples were taken from the overflow and underflow ports of the two cyclones, respectively, and the solid content of the liquid mixture was analyzed for each sample. The high-efficiency working range of the 22-8 series cyclone is determined as follows: the flow rate is 0.8m ³ h ^-1 , the first-stage split ratio is 12%, the second-stage split ratio is 12%, and the separation efficiency is 80%. The separation efficiency of the 8-22 series cyclone is slightly lower, which is 75%.

Example 6 Determination of adsorption desulfurization efficiency of two-stage series cyclone system

Correctly connect each interface and valve of the secondary cyclone separation system according to the 20-6 series connection. Before the test, the system should be cleaned and emptied for many times, and the formal test should be carried out after confirming that it is dry. The oil product containing 50ppm sulfur was injected into the feed tank, and the volume was more than 1/3; 5w.t% of HKUST-1 adsorbent was added to the system using a 1:20 agent-oil ratio. Adjust each valve node required by the working condition, start the mud pump, keep the temperature constant, adjust the inlet pressure, flow rate, and split ratio, collect the material of the underflow and overflow outlet for filtration, and analyze the solid content. The oil is analyzed by the method of Example 1. Sulfur content.

When the flow rate is 0.8m ³ h ^-1 , the primary split ratio is 12%, the secondary split ratio is 8%, the separation rate of adsorbent particles exceeds 99.5%, and the sulfur content in the final clarified oil is less than 10ppm.

Embodiment 7 Sorbent solvent extraction regeneration

Toluene was selected as the solvent, and the HKUST-1 adsorbent adsorbed sulfur was subjected to solvent extraction and regeneration.

Add 25 liters of toluene solvent to 5 kg of used adsorbent HKUST-1 powder, stir evenly, and filter after about 10 minutes to obtain solid powder. Repeat the extraction operation 3 times. The extracted solid powder was dried in a 150°C vacuum oven to remove the solvent. The regenerated HKUST-1 was subjected to adsorption desulfurization again, and it was recycled 20 times, and the adsorption performance remained basically unchanged.

Similarly, when xylene and petroleum ether were selected as solvents, the extraction effect was similar.

Example 8 Oxidative regeneration of adsorbent

Hydrogen peroxide was selected as the oxidant to oxidize the dibenzothiophene sulfur adsorbed in the HKUST-1 adsorbent to generate dibenzothiosulfone. The sulfone was easily soluble in water, and the adsorbent was regenerated after washing with water.

Add 5 liters of aqueous solution containing 3% hydrogen peroxide to 5 kg of used adsorbent HKUST-1 powder, stir well, and wash with water after about 10 minutes. Repeat washing 3 times. The solid powder obtained after separation was put into a 150°C vacuum oven to dry. The regenerated HKUST-1 was subjected to adsorption desulfurization again, and it was recycled 20 times, and the adsorption performance remained basically unchanged.

Similarly, the use of sodium hypochlorite as the oxidant can also be oxidatively regenerated, and the effect is similar.

Claims (10)

1. a system of swirl strengthening to remove sulfide in oil product, the desulfurization method of this system may further comprise the steps: Step (1) Adsorption desulfurization: the adsorbent adsorbs the sulfide in the oil; the adsorbent and the oil are added to the premixed adsorption unit and the liquid-solid suspension conveying unit, and mixed evenly, wherein the premixed adsorption unit includes a belt. The agitated sealed kettle completes mixing and adsorption here; the adsorbent is fully contacted with the sulfide in the oil for adsorption; then it is transported into the cyclone system through the material pump; the selected adsorbent is Y-type molecular sieve, 13X molecular sieve, mesoporous Molecular sieves, activated carbons, metal organic frameworks MOFs, porous organic polymers POPs or polyporous ionic liquids PILs; Step (2) Separation of adsorbent: Separation of fine adsorbent particles by cyclone method; oil product containing adsorbent enters the liquid-solid separation cyclone system unit, and operating parameters such as inlet flow rate and split ratio are adjusted to make the adsorbent particles in the micro-cyclone flow. The rotation and revolution in the field further strengthen the adsorption desulfurization, and at the same time realize the liquid-solid separation of the fine particles of the adsorbent; the low-sulfur refined oil is obtained from the overflow port, and the mixture of high-solid content adsorbent and oil product obtained from the underflow port is partially back-mixed back used, and part of it enters the regeneration system; The liquid-solid separation cyclone system unit includes a single-stage or two-stage series cyclone; wherein the first cyclone of the series system is provided with an inlet to receive the mixed liquid at the outlet of the mixed adsorption unit, and an overflow port to discharge a cyclone. The oil product after stage separation, an underflow port to discharge the adsorbent after the first stage separation; the oil product discharged from the overflow port enters the second cyclone for secondary separation, and an inlet is provided to accept the first cyclone The oil discharged from the overflow port, an overflow port to discharge the oil after secondary separation, and an underflow port to discharge the adsorbent after secondary separation; the sulfur content of the separated oil is less than 10ppm; Step (3) Regeneration of adsorbent: according to the mechanism of oxidative desulfurization, add the adsorbent adsorbed with thiophene sulfur into an oxidant, oxidize the thiophene sulfur into a water-soluble sulfone, and then rinse with water to dissolve the eluted sulfone; or according to the extraction principle, The adsorbed sulfur is dissolved and removed by using organic solvent; after drying, a regenerated adsorbent is obtained, which is added to the adsorbent recovery and regeneration unit for recycling; The adsorbent recovery and regeneration unit includes a roller centrifugal filter separation kettle with a feeding port, an oxidant solution or extractant solution storage tank and a solvent recovery tank; the adsorbent and oil discharged from the bottom flow port of the cyclone are separated, and an oxidant is added. The solution or extractant is used for oxidative regeneration or extraction regeneration of the adsorbent. 2 . The system for enhanced swirl flow removal of sulfides in oil products according to claim 1 , wherein the adsorption saturated sulfur capacity of the adsorbent selected in the step (1) is 15-40 g/kg. 3 . 3. the system of a kind of swirl strengthening removing sulfide in oil product according to claim 1, is characterized in that, the specific surface agent of described step (1) selected adsorbent is 150-1800m2/g, pore volume 0.35-1.1cm3/g, density 1.5-2.5g/cm3, average particle size greater than 30um. 4. the system of a kind of cyclone intensified removal of sulfide in oil product according to claim 1, is characterized in that, described step (2) described cyclone separation system is single-stage cyclone, and the cone angle is 5°-25°. 5. a kind of cyclone-enhanced system for removing sulfide in oil product according to claim 1, is characterized in that, described step (2) described cyclone separation system carries out two-stage series combination of cyclone, Respectively, the small-angle cyclone is connected with the large-angle cyclone, the large-angle cyclone is connected with the small-angle cyclone, and the angle cyclone is connected in series. 6 . The system of cyclone-enhanced removal of sulfides in oil products according to claim 1 , wherein the concentration of the feed adsorbent particles in the adsorption cyclone separation process in the step (2) is 2%. 7 . -10%, the inlet flow is 0.2-1.0m3/h, and the split ratio of the underflow port and the overflow port is 5%-12%. 7. a kind of swirl strengthening system for removing sulfide in oil product according to claim 1, is characterized in that, described step (2) described underflow port gained high solid content adsorbent and oil product mixture are backmixed The ratio with regeneration is 1:3-1:1. 8 . The system for cyclone-enhanced removal of sulfides in oil products according to claim 1 , wherein, the adsorption cyclone separation process in the step (2) is in parallel with multiple groups in parallel. 9 . 9 . The system for enhanced swirl removal of sulfides in oil products according to claim 1 , wherein the adsorbent oxidation regeneration described in the step (3) adopts H ₂ O ₂ and NaClO as the Oxidant, according to the adsorption sulfur capacity (n mol/g), the dosage of oxidant is (1-3) times of n mol/g adsorbent. 10. the system of a kind of swirl strengthening removing sulfide in oil product according to claim 1, is characterized in that, described step (3) described adsorbent extraction regeneration, adopts toluene, xylene, petroleum ether Solvent extraction and washing, the amount of extractant is 3-5L/kg adsorbent, repeated three times.

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