Real moving bed diesel adsorption separation system and method

Abstract

A real moving bed diesel adsorption separation system and method, comprising a feed tank (1), the feed tank (1) being connected by means of a pipeline to a feed inlet at a lower part of a moving bed adsorption chamber (3). An upper end of the moving bed adsorption chamber (3) is connected to an adsorbent storage tank (4), and an outlet of the moving bed adsorption chamber (3) is connected by means of a slide valve to a moving bed regeneration chamber (7). An upper end of the moving bed regeneration chamber (7) is connected to a desorbent storage tank (8), and an outlet of the moving bed regeneration chamber (7) is connected to a distillation column (11). Feed diesel first enters the adsorption chamber (3) to contact an aromatic adsorbent in a countercurrent manner, the aromatic adsorbent adsorbing aromatics from the diesel; the aromatic components adsorbed by the adsorbent are then conveyed to the regeneration chamber (7), and a desorbent in the regeneration chamber (7) displaces the aromatics to obtain the aromatic components, thereby ultimately achieving separation of alkanes and aromatics in diesel.

Description

A real moving bed diesel adsorption separation system and method Technical Field

[0001] This application relates to the field of adsorption separation technology, and in particular to a system and method for separating diesel aromatics and alkane components using a real moving bed process. Background Technology

[0002] Diesel fuel is a light petroleum product, a complex mixture of hydrocarbons, and is used as fuel for diesel engines. Diesel fuel is mainly blended from diesel fractions produced by processes such as crude oil distillation, catalytic cracking, thermal cracking, hydrocracking, and petroleum coking.

[0003] With increasing emphasis on environmental protection, improving diesel quality, just like the trend in gasoline quality development, has become inevitable in order to reduce vehicle exhaust pollution. Countries and regions are almost unanimously committed to significantly reducing the sulfur content of automotive diesel fuel, primarily because the sulfur in diesel directly affects the composition of particulate matter in diesel vehicle exhaust. This particulate matter mainly consists of carbon (smoke), soluble organic matter, and sulfates. Higher sulfur content in diesel fuel leads to more sulfate formation, which can easily cause respiratory diseases and may be carcinogenic. If a diesel vehicle is equipped with a high-efficiency exhaust gas converter, the sulfur in the diesel can easily poison the catalyst, significantly reducing its function and increasing exhaust emissions. Furthermore, aromatic hydrocarbons in diesel fuel are also a direct cause of high concentrations of ammonia oxides and particulate matter in diesel vehicle exhaust. Therefore, it is expected that future standards for automotive diesel fuel will gradually tighten restrictions on the content of aromatic hydrocarbons and polycyclic aromatic hydrocarbons (PAHs). Currently, diesel fuel produced through unit processes such as catalytic cracking, coking, and catalytic pyrolysis contains PAHs far exceeding 11%, which does not comply with the national standard GB19147-2016, which stipulates that the PAH content of automotive diesel fuel should not exceed 11%. Separating aromatics and non-aromatic components from diesel fuel to obtain high-purity alkanes and aromatics not only enables the classified management of diesel fuel components and provides raw materials for efficient diesel conversion and accurate processing, but also reduces the diesel-to-gasoline ratio in refineries, thereby improving the economic and social benefits of enterprises.

[0004] CN1566284A discloses a method for hydrotreating diesel fuel, which increases the cetane number of diesel fuel while reducing its aromatic content. Diesel feedstock and hydrogen enter a first reactor, where they contact a non-precious metal hydrotreating catalyst. The effluent from the first reactor, with or without separation, enters a second reactor, where it contacts a precious metal hydrodearomatics catalyst. The effluent from the second reactor is then separated to obtain the diesel product. While this method achieves good dearomatics removal, the process is complex, and the investment and operating costs are high.

[0005] CN102465029A discloses a method for diesel hydrorefining. Under diesel hydrorefining conditions, feedstock diesel and hydrogen first enter a gas-liquid mixer via a heating furnace to ensure thorough mixing of the hydrogen and feedstock oil. Then, the mixture enters a first reactor, where it contacts a non-precious metal hydrorefining catalyst under hydrorefining conditions for a conventional hydrorefining reaction. The resulting effluent enters a gas stripping and hydrogen mixing unit to remove dissolved hydrogen sulfide and ammonia from the oil, and to saturate the hydrogen in the oil. This effluent is then mixed with supplemental hydrogen and enters a second reactor where it contacts a precious metal hydrorefining catalyst for a deep dearomatics reaction, ultimately yielding a clean diesel product. This method requires both reactors to operate at a high hydrogen-to-oil ratio and low space velocity, resulting in high hydrogen consumption and low throughput.

[0006] CN1566284A discloses a method for hydrotreating diesel fuel, which increases the cetane number of diesel fuel while reducing its aromatic content. Diesel feedstock and hydrogen enter a first reactor, where they contact a non-precious metal hydrotreating catalyst. The effluent from the first reactor, with or without separation, enters a second reactor, where it contacts a precious metal hydrodearomatics catalyst. The effluent from the second reactor is then separated to obtain the diesel product. While this method achieves good dearomatics removal, the process is complex, and the investment and operating costs are high.

[0007] CN101328430A discloses a method for catalytic hydrotreating of diesel fuel. Under hydrogen-containing conditions, the reaction temperature is 330–370℃, the hydrogen partial pressure is 6–9 MPa, the hydrogen-to-oil volume ratio is 500:1–1000:1, and the liquid hourly space velocity is 1.0–2.0 h⁻¹. The diesel fuel yield is above 97 wt%, the aromatic hydrocarbon removal rate is above 60%, the total sulfur and total nitrogen removal rate is above 98.5%, and the product density decreases by more than 0.04 g / cm³. However, this method has a relatively low aromatic hydrocarbon removal rate, and the cetane number cannot directly meet the national standard requirements.

[0008] The aforementioned processing methods for upgrading diesel fuel, whether hydrorefining or hydromodification, all suffer from problems such as resource waste, low cetane number of the product, high hydrogen consumption, high energy consumption, and large equipment investment. Summary of the Invention

[0009] In order to solve the above-mentioned technical problems, this application provides a real moving bed diesel adsorption separation system and method, which separates diesel components through a real moving bed to obtain high-purity aromatics and non-aromatic components.

[0010] In a first aspect, the present invention provides a real moving bed diesel adsorption separation system, which is achieved by the following technical solution.

[0011] A real moving bed diesel adsorption separation system includes a feed tank, which is connected to the feed inlet at the bottom of the moving bed adsorption chamber via a pipeline, and the upper end of the moving bed adsorption chamber is connected to an adsorbent storage tank; the outlet of the moving bed adsorption chamber is connected to a moving bed regeneration chamber via a slide valve, and the upper end of the moving bed regeneration chamber is connected to a desorbent storage tank; the outlet of the moving bed regeneration chamber is connected to a distillation column.

[0012] Furthermore, the moving bed adsorption chamber is also connected to a non-aromatic storage tank.

[0013] Furthermore, the moving bed regeneration chamber is also connected to a regenerant storage tank, which is connected to an adsorbent storage tank via a pipeline.

[0014] Furthermore, the outlet of the distillation column is connected to a desorbent storage tank via a pipeline.

[0015] Secondly, the present invention provides a real moving bed diesel adsorption separation method, which is achieved by the following technical solution.

[0016] A real moving bed diesel adsorption separation method includes the following steps:

[0017] S1. The diesel feedstock is fed into the pre-adsorption tower, where sulfur-containing and nitrogen-containing compounds and impurities are removed under the action of the pre-adsorbent;

[0018] S2. The diesel feedstock after impurity removal is fed from the bottom to the moving bed adsorption chamber, and the aromatic adsorbent is fed from the top of the moving bed adsorption chamber. The aromatic adsorbent and the diesel feedstock are in countercurrent contact to obtain the aromatic and non-aromatic components adsorbed by the adsorbent. The processing temperature in the moving bed adsorption chamber is 50-100℃ and the adsorption pressure is 0.5-1.5MPa.

[0019] S3. The adsorbent that adsorbs aromatics is intermittently discharged through a slide valve and enters the moving bed regeneration chamber. The desorbent is fed in from the top of the moving bed regeneration chamber to wash and desorb the aromatic components on the adsorbent, resulting in the desorbed aromatic components, desorbent, and regenerated adsorbent. The processing temperature of the moving bed regeneration chamber is 50-80℃, and the adsorption pressure is 0.5-1.5MPa.

[0020] S4. The desorbed aromatic components and the desorbent are used as extractant to separate the aromatics from the non-aromatic components, thus obtaining the aromatic product.

[0021] Furthermore, the distillation range of the diesel feedstock is 150–400°C.

[0022] Furthermore, in step S1, the temperature of the adsorbent bed in the pre-adsorption tower is 30–150°C, and the mass hourly space velocity is 0.1–3.0 h⁻¹. -1 The adsorption pressure is 0.1–5.0 MPa.

[0023] Furthermore, in step S1, silica gel or 13X molecular sieve are selected as the pre-adsorbent.

[0024] Furthermore, in step S2, the aromatic adsorbent is selected from one or more of the following: metal-modified MCM-41 molecular sieve, metal-modified silica gel, and metal-modified 13X molecular sieve. The modified metal is selected from one or more of the following: K, Cs, Mg, Ca, Ba, Mo, and Ni.

[0025] Furthermore, in step S3, the desorbent is selected from one or more of benzene, toluene, o-xylene, m-xylene, cyclohexane, and methylcyclohexane.

[0026] Furthermore, the volumetric flow rate ratio of the adsorbent to the diesel feedstock entering the moving bed adsorption chamber is 1:(0.5-2.5); the mass flow rate ratio of the adsorbent to the desorbent entering the moving bed regeneration chamber is 1:(0.5-5).

[0027] This application has the following beneficial effects.

[0028] (1) The real moving bed process used in this invention is a green and efficient separation technology that can achieve efficient conversion of diesel fuel;

[0029] (2) The adsorption separation method of the present invention can separate components in diesel fuel under low pressure and low temperature. The process is a single tower adsorption process, which has the characteristics of being environmentally friendly and pollution-free, having mild reaction conditions, low investment, low energy consumption, and easy control.

[0030] (3) The adsorption separation method of the present invention achieves efficient separation of diesel components with low cost and simple process. The aromatic content in the aromatic product is ≥95wt.%, and the aromatic content in the non-aromatic components is ≤5wt.%.

[0031] (4) The alkanes separated by the adsorption separation method of this invention can be used as high cetane number components or as high-quality feedstock for catalytic ethylene cracking, increasing the production of low-carbon olefins; the separated cycloalkanes can be blended into diesel fuel as clean diesel fuel components or sold directly as non-aromatic solvents; the separated aromatics can be further separated into monocyclic and polycyclic aromatics, among which monocyclic aromatics can be used as feedstock for the lightening of heavy aromatics, and hydrogenated under medium and low pressure to produce light aromatics such as BTX or high-octane gasoline; polycyclic aromatics can be blended into high-aromatic solvent oil, and the market prospects for aromatic solvent oil in my country are broad, especially in the paint industry where the usage is quite considerable. The classified management of diesel components not only achieves the goal of efficient diesel conversion and reduces the diesel-to-gasoline ratio, but also makes reasonable use of the resources of each component of diesel fuel, creating objective economic benefits. Attached Figure Description

[0032] Figure 1 is a connection diagram of the separation system of the present invention;

[0033] The components include: 1. Raw material tank; 2. Pump; 3. Moving bed adsorption chamber; 4. Adsorbent storage tank; 5. Non-aromatic storage tank; 6. Buffer tank; 7. Moving bed regeneration chamber; 8. Desorbent storage tank; 9. Regenerator storage tank; 10. Extraction liquid storage tank; and 11. Distillation column. Detailed Implementation

[0034] The present patent application will be further described below with reference to the accompanying drawings and embodiments.

[0035] Unless otherwise specified, the experimental methods used in the following examples are conventional methods; the materials and reagents used in the following preparation examples and examples are commercially available unless otherwise specified.

[0036] As shown in Figure 1, a real moving bed diesel adsorption separation system includes a feed tank 1, a pump 2, a moving bed adsorption chamber 3, an adsorbent storage tank 4, a non-aromatic storage tank 5, a buffer tank 6, a moving bed regeneration chamber 7, a desorbent storage tank 8, a regenerator storage tank 9, an extract storage tank 10, and a distillation column 11.

[0037] The raw material tank 1 is connected to the feed inlet at the bottom of the moving bed adsorption chamber 3 via a pipeline, and a pump 2 is installed on the pipeline. The upper end of the moving bed adsorption chamber 3 is connected to the adsorbent storage tank 4, and the upper part of the moving bed adsorption chamber 3 is also connected to the non-aromatic storage tank 5. The discharge port of the moving bed adsorption chamber 3 is connected to the moving bed regeneration chamber 7 via a slide valve. A buffer tank 6 may also be provided between the moving bed adsorption chamber 3 and the moving bed regeneration chamber 7. The upper end of the moving bed regeneration chamber 7 is connected to the desorbent storage tank 8. The moving bed regeneration chamber 7 is also connected to the regenerator storage tank 9, and the regenerator storage tank 9 is connected to the adsorbent storage tank 4 via a pipeline. The discharge port of the moving bed regeneration chamber 7 is connected to the distillation column 11, and an extractant storage tank 10 may also be provided between the moving bed regeneration chamber 7 and the distillation column 11. The discharge port of the distillation column 11 is connected to the desorbent storage tank 8 via a pipeline.

[0038] The actual moving bed of this invention consists of an adsorption chamber, a regeneration chamber, and a solid particle feeding and feed liquid delivery pipeline. The adsorption chamber and the regeneration chamber are connected in series via a slide valve. An adsorbent storage tank is located at the top of the adsorption chamber, connected via a delivery pipeline, and feed liquid delivery pipes are located at both ends of the bottom. The adsorbent enters the adsorption chamber from the storage tank downwards, while the feed liquid enters the adsorption chamber through the delivery pipeline, flowing upwards to the top. At this point, it forms a countercurrent contact with the falling adsorbent, allowing for adsorption, separation, regeneration, adsorption, and desorption processes to be performed at different temperatures according to process requirements. The relative movement direction between the liquid and particles in the reaction chamber is countercurrent, achieved using a special pressure control method.

[0039] Example 1

[0040] A real moving bed diesel adsorption separation method includes the following steps:

[0041] (1) The diesel feedstock first enters the pre-adsorption tower, where sulfur-containing, nitrogen-containing compounds and gum-like impurities are removed by the pre-adsorbent. Silica gel is selected as the pre-adsorbent, the adsorbent bed temperature is 50℃, and the mass hourly space velocity is 0.1 h⁻¹. -1 The adsorption pressure is 0.5 MPa;

[0042] (2) The diesel feedstock after impurity removal is pumped to the moving bed adsorption chamber 3 by pump 2, and fed from the bottom. At the same time, the aromatic adsorbent is fed into the moving bed adsorption chamber 3 from the top and moves downward under the action of gravity, achieving countercurrent contact with the diesel feedstock. The aromatic components in the diesel are adsorbed by the adsorbent and carried downward, while the remaining non-aromatic components are collected as raffinate at the top of the adsorption chamber to obtain the non-aromatic product;

[0043] In this embodiment, the aromatic adsorbent is a metal-modified MCM-41 molecular sieve, which is modified by impregnation to introduce metal oxides. After preparing a metal salt solution, it is placed in a beaker, with the MCM-41 molecular sieve as the support. The impregnation temperature is 80℃, and the impregnation time is 6 hours. Finally, the impregnated molecular sieve is washed, dried at 120℃ for 4 hours, and calcined at 550℃ for 6 hours. The modified metals are K, Cs, and Mg, with K₂O content of 0.5 wt%, Cs₂O content of 0.5 wt%, and MgO content of 0.5 wt%. The specific surface area is 920 m². 2 / g, pore volume 0.75cm 3 / g, with an average pore size of 4.8nm; the mass flow rate ratio of adsorbent to raw material is 1:0.8; the reaction temperature and adsorption pressure of moving bed adsorption chamber 3 are shown in Table 2;

[0044] (3) The adsorbent that adsorbs aromatics deposits at the bottom of the moving bed adsorption chamber 3 and is intermittently discharged through a slide valve into the moving bed regeneration chamber 7. A desorbent is introduced into the top of the moving bed regeneration chamber 7 to flush and desorb the aromatic components from the adsorbent, thus regenerating the adsorbent. The desorbed aromatic components, along with the desorbent, are discharged from the bottom of the moving bed regeneration chamber 7 as extractant. The regenerated adsorbent is then fed back into the top of the moving bed adsorption chamber 3 via a conveying hopper for reuse.

[0045] The switching time of the slide valve in this embodiment is shown in Table 2; the desorbent is 70% methylcyclohexane and 30% toluene; the mass flow rate ratio of the adsorbent to the desorbent after adsorption is 1:1; the reaction temperature in the moving bed regeneration chamber 7 is 60℃ and the adsorption pressure is 0.8MPa.

[0046] (4) The extract is used to cut the desorbent, and finally the aromatic product is obtained.

[0047] The composition analysis of diesel feedstock is shown in Table 1 (No. 1 diesel), the actual moving bed adsorption separation process conditions are shown in Table 2, and the evaluation results are shown in Table 3.

[0048] Example 2

[0049] A real moving bed diesel adsorption separation method, the difference between this embodiment and Embodiment 1 is:

[0050] (1) The aromatic adsorbent was metal-modified silica gel. Sodium silicate was dissolved in water, and then NaOH was added to form a gel. After the gel was formed, a metal salt solution was prepared, and it was continuously added while stirring. After filtration, it was dried and calcined to remove moisture and organic matter, and finally metal-modified silica gel was obtained. The reaction temperature was 80℃, the stirring time was 12h, and the final drying was at 120℃ for 4h and calcined at 550℃ for 6h. The modified metals were K, Cs, and Ba, with K2O content of 0.5wt%, Cs2O content of 0.5wt%, and BaO content of 0.5wt%. The desorbent was 50% methylcyclohexane and 50% o-xylene.

[0051] (2) The mass flow rate ratio of adsorbent to raw material is 1:1.2; the mass flow rate ratio of adsorbent to desorbent after adsorption is 1:1.3.

[0052] The composition analysis of diesel feedstock is shown in Table 1 (No. 1 diesel), the actual moving bed adsorption separation process conditions are shown in Table 2, and the evaluation results are shown in Table 3.

[0053] Example 3

[0054] A real moving bed diesel adsorption separation method, the difference between this embodiment and Embodiment 1 is:

[0055] (1) The aromatic adsorbent is a metal-modified 13X molecular sieve. The modification method is the same as in Example 1. The support is 13X molecular sieve, and the modified metals are K, Cs, and Mo, wherein the K2O content is 0.5wt%, the Cs2O content is 0.5wt%, and the MoO3 content is 0.5wt%. The desorbent is 50% cyclohexane and 50% toluene.

[0056] (2) The mass flow rate ratio of adsorbent to raw material is 1:1.5; the mass flow rate ratio of adsorbent to desorbent after adsorption is 1:1.8.

[0057] The composition analysis of diesel feedstock is shown in Table 1 (2# diesel), the actual moving bed adsorption separation process conditions are shown in Table 2, and the evaluation results are shown in Table 3.

[0058] Example 4

[0059] A real moving bed diesel adsorption separation method, the difference between this embodiment and Embodiment 1 is:

[0060] (1) The aromatic adsorbent is a metal-modified MCM-41 molecular sieve. The modification method is the same as in Example 1. The modified metals are Mg, Ca, and Mo, with MgO content of 0.5wt%, CaO content of 0.5wt%, and MoO3 content of 1wt%. The support is the same as in Example 1, using MCM-41 molecular sieve. The desorbent is 50% cyclohexane-50% methylcyclohexane (70% alkane portion) and benzene (30%).

[0061] (2) The mass flow rate ratio of adsorbent to raw material is 1:1.9; the mass flow rate ratio of adsorbent to desorbent after adsorption is 1:2.2.

[0062] The composition analysis of diesel feedstock is shown in Table 1 (2# diesel), the actual moving bed adsorption separation process conditions are shown in Table 2, and the evaluation results are shown in Table 3.

[0063] Example 5

[0064] A real moving bed diesel adsorption separation method, the difference between this embodiment and Embodiment 1 is:

[0065] (1) The aromatic adsorbent is a metal-modified MCM-41 molecular sieve. The modification method is the same as in Example 1. The modified metals are Mg, Ca, and Ni, with MgO content of 0.5wt%, CaO content of 0.5wt%, and NiO content of 1wt%. The support is the same as in Example 1, using MCM-41 molecular sieve. The desorbent is 50% cyclohexane-50% methylcyclohexane (70% alkane portion) and toluene (30%).

[0066] (2) The mass flow rate ratio of adsorbent to raw material is 1:2.2; the mass flow rate ratio of adsorbent to desorbent after adsorption is 1:3.2.

[0067] The composition analysis of diesel feedstock is shown in Table 1 (2# diesel), the actual moving bed adsorption separation process conditions are shown in Table 2, and the evaluation results are shown in Table 3.

[0068] Table 1. Composition of Diesel Feedstock

[0069] Table 2 Actual moving bed adsorption separation process conditions

[0070] Table 3 Evaluation Results of Real Mobile Beds Note: Alkane yield = Product alkane mass / Alkane mass in feed diesel fuel × 100%; Aromatics yield = Product aromatics mass / Feed alkane-aromatics mass × 100%; Alkane content = Alkane mass of alkane components / Total mass of alkane components × 100%; Aromatics content = Aromatics mass of aromatics components / Total mass of aromatics components × 100%.

[0071] The embodiments described in this specific implementation are preferred embodiments of this application and are not intended to limit the scope of protection of this application. Therefore, all equivalent changes made in accordance with the structure, shape and principle of this application should be covered within the scope of protection of this application.

Claims

1. A real moving bed diesel adsorption separation system, comprising a feed tank (1), characterized in that: The raw material tank (1) is connected to the feed inlet at the bottom of the moving bed adsorption chamber (3) via a pipeline, and the upper end of the moving bed adsorption chamber (3) is connected to the adsorbent storage tank (4); the outlet of the moving bed adsorption chamber (3) is connected to the moving bed regeneration chamber (7) via a slide valve, and the upper end of the moving bed regeneration chamber (7) is connected to the desorbent storage tank (8); the outlet of the moving bed regeneration chamber (7) is connected to the distillation column (11).

2. The real moving bed diesel adsorption separation system according to claim 1, characterized in that: The moving bed adsorption chamber (3) is also connected to the non-aromatic storage tank (5).

3. The real moving bed diesel adsorption separation system according to claim 1, characterized in that: The moving bed regeneration chamber (7) is also connected to the regenerant storage tank (9), which is connected to the adsorbent storage tank (4) via a pipeline.

4. The real moving bed diesel adsorption separation system according to claim 1, characterized in that: The outlet of the distillation column (11) is connected to the desorbent storage tank (8) via a pipeline.

5. A real moving bed diesel adsorption separation method, characterized in that: Includes the following steps: S1. The diesel feedstock is fed into the pre-adsorption tower, where sulfur-containing and nitrogen-containing compounds and impurities are removed under the action of the pre-adsorbent; S2. The diesel feedstock after impurity removal is sent from the bottom to the moving bed adsorption chamber (3), and the aromatic adsorbent is sent from the top of the moving bed adsorption chamber (3). The aromatic adsorbent and the diesel feedstock are in countercurrent contact to obtain the aromatic and non-aromatic components adsorbed by the adsorbent. The processing temperature in the moving bed adsorption chamber (3) is 50-100℃ and the adsorption pressure is 0.5-1.5MPa. S3. The adsorbent that adsorbs aromatics is intermittently discharged through a slide valve and enters the moving bed regeneration chamber (7). The desorbent is fed from the top of the moving bed regeneration chamber (7) to rinse and desorb the aromatic components on the adsorbent, thus obtaining the desorbed aromatic components, the desorbent, and the regenerated adsorbent. The processing temperature of the moving bed regeneration chamber (7) is 50-80℃, and the adsorption pressure is 0.5-1.5MPa. S4. The desorbed aromatic components and the desorbent are used as extractant to separate the aromatics from the non-aromatic components, thus obtaining the aromatic product.

6. The method for diesel adsorption and separation in a real moving bed according to claim 5, characterized in that: The distillation range of diesel feedstock is 150–400℃.

7. The method for diesel adsorption and separation in a real moving bed according to claim 5, characterized in that: In step S1, the temperature of the adsorbent bed in the pre-adsorption tower is 30–150℃, and the mass hourly space velocity is 0.1–3.0 h⁻¹. -1 The adsorption pressure is 0.1–5.0 MPa.

8. The method for diesel adsorption and separation in a real moving bed according to claim 5, characterized in that: In step S2, the aromatic adsorbent is selected from one or more of the following: metal-modified MCM-41 molecular sieve, metal-modified silica gel, and metal-modified 13X molecular sieve.

9. The method for diesel adsorption and separation in a real moving bed according to claim 5, characterized in that: In step S3, the desorbent is selected from one or more of benzene, toluene, o-xylene, m-xylene, cyclohexane, and methylcyclohexane.

10. The method for diesel adsorption and separation in a real moving bed according to claim 5, characterized in that: The volume flow rate ratio of the adsorbent to the diesel feedstock entering the moving bed adsorption chamber (3) is 1:(0.5~2.5); the mass flow rate ratio of the adsorbent to the desorbent entering the moving bed regeneration chamber (7) is 1:(0.5~5).

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