Aryl rubber plasticizer and preparation method thereof

Abstract

The invention provides an aryl rubber plasticizer and a preparation method thereof, and relates to the technical field of petrochemical engineering, and the preparation method comprises the following steps: (a) carrying out reduced pressure deep drawing on naphthenic base and / or intermediate base vacuum residue to obtain vacuum residue A, and carrying out solvent deasphalting on the vacuum residue A to obtain deasphalted oil as treatment oil B; (b) hydrotreating the naphthenic base vacuum distillate oil to obtain hydrogenated oil, taking the hydrogenated oil, cutting off light fractions to obtain heavy fractions as treated oil C; and (c) blending the obtained treated oil B and treated oil C to obtain the aryl rubber plasticizer. The preparation method disclosed by the invention is short in process flow, the obtained aryl rubber plasticizer is high in product yield and added value, and meanwhile, the product is green and environment-friendly, has relatively high aromatic hydrocarbon content and also has relatively high market competitiveness.

Description

Technical Field

[0001] The present invention relates to the technical field of petrochemical industry, and in particular to an aromatic rubber plasticizer and a preparation method thereof. Background Art

[0002] At present, the production of environmentally friendly rubber plasticizers mainly has two processes, namely solvent refining and hydrorefining, and their combined processes. The production of high-aromatic rubber plasticizers is mostly a solvent refining process, such as furfural refining, solvent deasphalting process and their combined processes; solvent refining is a physical extraction process, which has problems such as low yield of main products, a large amount of by-products with low added value, high processing costs, and environmental pollution risks during the processing, resulting in low overall economic benefits. Therefore, developing a production process for aromatic-based environmentally friendly rubber plasticizers with low cost and high C A value has great practical significance.

[0003] For the production of high-aromatic rubber plasticizers, in the prior art, naphthenic cut 3 vacuum gas oil is used as a raw material, and after two-stage furfural refining, an environmentally friendly rubber oil with a C A value of 10% - 18% is obtained, and at the same time, some low-value primary extract oil or secondary extract oil is produced, resulting in a low yield of the main product. A production method of a heavy environmentally friendly rubber oil disclosed in the prior art obtains an environmentally friendly rubber oil that meets the requirements of the EU REACH regulation through a two-stage propane solvent extraction process. The C A value of the environmentally friendly rubber oil obtained by this process is only 10% - 20%, and the product yield is low; a preparation method of an environmentally friendly rubber oil disclosed in the prior art performs primary propane deasphalting on naphthenic vacuum residue to obtain deasphalted oil, then performs secondary propane deasphalting on the deasphalted oil, and the obtained heavy deasphalted oil is mixed with naphthenic oil to obtain an environmentally friendly rubber oil (rubber plasticizer). The C A value of the obtained product is on the low side. In the prior art, there is also a method that uses inferior naphthenic heavy wax oil as a raw material, first uses a propane deasphalting process to obtain a tower top refined liquid, and then uses different combined processes (such as hydrorefining, single-stage furfural refining, and two-stage furfural refining) respectively to obtain an environmentally friendly rubber oil. The C A value of the rubber plasticizer samples obtained by the hydrorefining and single-stage furfural refining processes is low (only 12% - 18%), while the propane deasphalting and two-stage furfural refining processes have a long process flow and will produce more by-products, resulting in a low yield of the main product. In the prior art, there is also a method that uses naphthenic distillate as a raw material and produces C AThe environmental protection rubber plasticizer with a value of 19% - 26% has good compatibility with rubber and excellent processing performance. However, the entire process flow is relatively long, and a by-product of low-value furfural extract oil is generated. In the prior art, it is also disclosed that a vacuum distillate oil is used as a raw material, and a pretreated oil is obtained by hydrotreating, and then an extract oil is obtained through a furfural refining process. After hydrogenation, a high-aromatic environmental protection rubber oil is obtained. The rubber oil obtained by this process has a relatively high aromatic content, but the process flow is long, more by-products are generated, and the yield of the main product is low.

[0004] In view of this, the present invention is specifically proposed. Summary of the Invention

[0005] One of the purposes of the present invention is to provide a preparation method of an aromatic rubber plasticizer, which not only has a short process flow, but also has a high product yield and added value of the obtained aromatic rubber plasticizer.

[0006] Another purpose of the present invention is to provide an aromatic rubber plasticizer, which is green and environmentally friendly, has a relatively high aromatic content, and also has a relatively high market competitiveness.

[0007] In order to achieve the above purposes of the present invention, the following technical solutions are specifically adopted:

[0008] In the first aspect, a preparation method of an aromatic rubber plasticizer includes the following steps:

[0009] (a) Subjecting naphthenic and / or intermediate base vacuum residue to vacuum deep distillation to obtain vacuum residue A, and taking the vacuum residue A for solvent deasphalting to obtain deasphalted oil as treated oil B;

[0010] (b) Subjecting naphthenic vacuum distillate oil to hydrotreating to obtain a hydrogenated product oil, and taking the hydrogenated product oil to cut off light fractions to obtain a heavy fraction as treated oil C;

[0011] (c) Blending the treated oil B and the treated oil C to obtain an aromatic rubber plasticizer.

[0012] Further, in step (a), the distillation temperature of the vacuum deep distillation is not lower than 500 °C.

[0013] Further, in step (a), the solvent used in the solvent deasphalting includes at least one of pentane, hexane, and heptane, and preferably pentane.

[0014] Further, the top temperature of the extraction column in the solvent deasphalting is 130 °C - 170 °C, and the bottom temperature is 120 °C - 160 °C;

[0015] Preferably, the internal pressure of the extraction column in the solvent deasphalting is 2.0 MPa - 4.5 MPa;

[0016] Preferably, the agent-oil ratio used in the solvent deasphalting is 4:1 to 10:1.

[0017] Furthermore, the naphthenic vacuum gas oil includes at least one of the second-stage vacuum distillate oil, the third-stage vacuum distillate oil, and the fourth-stage vacuum distillate oil obtained by vacuum distillation of naphthenic crude oil;

[0018] Preferably, the kinematic viscosity of the naphthenic vacuum gas oil at 100 °C ≥ 6 mm 2 / s, and the C A ≥ 18%.

[0019] Furthermore, the reaction temperature of the hydrotreating is 300 °C to 400 °C;

[0020] Preferably, the volume ratio of hydrogen to naphthenic vacuum gas oil in the hydrotreating is (600 - 1200):1;

[0021] Preferably, the volume space velocity in the hydrotreating is 0.3 h -1 ~1.8 h -1 , and the hydrogen partial pressure is greater than 10 MPa.

[0022] Furthermore, the heavy distillate is a distillate fraction greater than 360 °C;

[0023] Preferably, the open flash point of the heavy distillate is greater than 230 °C.

[0024] Furthermore, the mass ratio of the blending of treating oil B and treating oil C is 1:9 to 5:5;

[0025] Preferably, the blending temperature is 60 °C to 180 °C, and the blending time is not less than 15 min.

[0026] In a second aspect, an aromatic rubber plasticizer prepared by the preparation method described in any one of the above.

[0027] Furthermore, the C A value of the aromatic rubber plasticizer is above 25%;

[0028] Preferably, the kinematic viscosity of the aromatic rubber plasticizer at 100 °C ≥ 20 mm 2 / s, the flash point ≥ 240 °C, and the aniline point ≤ 75 °C;

[0029] Preferably, the content of benzo[a]pyrene in the aromatic rubber plasticizer is less than 1 mg / kg, the content of PAHs is less than 10 mg / kg, and the content of PCA is less than 3%.

[0030] Compared with the prior art, the present invention has at least the following beneficial effects:

[0031] The preparation method of the aromatic rubber plasticizer provided by the present invention adopts a single-stage solvent (pentane) deasphalting process and a single-stage hydrotreating process for distillate oil. After blending, an environmentally friendly rubber plasticizer product is obtained. The process flow of the present invention is short, and the product yield can reach more than 75%. The present invention converts low-value asphalt products into high-value rubber plasticizers. The obtained products meet the rubber plasticizer GB / T33322-2016 standard, are tax-free products, and have high market competitiveness.

[0032] The aromatic rubber plasticizer provided by the present invention is green and environmentally friendly, and at the same time has a high aromatic hydrocarbon content, meeting the limited substance requirements for environmentally friendly processing oils in the "Technical Specification for Green Design Product Evaluation - Automotive Tires", that is, the BaP content ≤ 1 mg / kg and the PAHs content ≤ 10 mg / kg. The C A value of the aromatic rubber plasticizer product of the present invention is above 25%, and the PCA content is less than 3%. It has better compatibility with rubber compounds, carbon black, etc. during tire preparation, and can endow tires with more excellent performance. Specific Embodiments

[0033] The technical solutions of the present invention will be clearly and completely described below in conjunction with the embodiments. Obviously, the described embodiments are some, but not all, of the embodiments of the present invention. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0034] According to the first aspect of the present invention, a preparation method of an aromatic rubber plasticizer is provided, including the following steps:

[0035] (a) Subjecting naphthenic and / or intermediate-base vacuum residue to deep vacuum distillation to obtain vacuum residue A, and subjecting the vacuum residue A to solvent deasphalting to obtain deasphalted oil as treated oil B;

[0036] (b) Subjecting naphthenic vacuum distillate oil to hydrotreating to obtain hydroprocessed oil, and removing light fractions from the hydroprocessed oil to obtain heavy fractions as treated oil C;

[0037] (c) Blending the obtained treated oil B and treated oil C to obtain an aromatic rubber plasticizer.

[0038] In the present invention, a single-stage solvent deasphalting process and a single-stage hydrotreating process for distillate oil are adopted. After blending, an environmentally friendly rubber plasticizer product is obtained. The process flow is short, and the product yield can reach more than 75%. Low-value asphalt products are converted into high-value rubber plasticizers. The obtained products meet the rubber plasticizer GB / T33322-2016 standard, are tax-free products, and have high market competitiveness.

[0039] In the present invention, naphthenic and / or intermediate-base vacuum residue refers to the vacuum residue obtained by vacuum distillation of naphthenic and / or intermediate-base crude oil.

[0040] In a preferred embodiment, in step (a), the distillation temperature for deep vacuum distillation is not lower than 500 °C.

[0041] In a preferred embodiment, in step (a), the solvent used in solvent deasphalting includes but is not limited to at least one or a mixture of pentane, hexane, and heptane, and pentane can be further preferably used, which is more conducive to further improving the effect of solvent deasphalting.

[0042] In a preferred embodiment, the top temperature of the extraction column in solvent deasphalting can be 130 °C to 170 °C, and its typical but non-limiting temperatures are, for example, 130 °C, 140 °C, 150 °C, 160 °C, 170 °C; the bottom temperature can be 120 °C to 160 °C, and its typical but non-limiting temperatures are, for example, 120 °C, 130 °C, 140 °C, 150 °C, 160 °C.

[0043] In a preferred embodiment, the internal pressure of the extraction column in solvent deasphalting can be 2.0 MPa to 4.5 MPa, and its typical but non-limiting internal pressures are, for example, 2.0 MPa, 2.5 MPa, 3.0 MPa, 3.5 MPa, 4.0 MPa, 4.5 MPa; meanwhile, the solvent-to-oil ratio used can be 4:1 to 10:1.

[0044] In the present invention, the process parameters of solvent deasphalting cooperate synergistically, which is more conducive to further improving the effect of solvent deasphalting, and further ensures the blending of deasphalted light oil and single-stage high-pressure hydrogenation products of naphthenic fraction oil to produce a high-C rubber plasticizer product with qualified PCA content. A value

[0045] In a preferred embodiment, naphthenic vacuum distillate includes but is not limited to at least one of the second-stage vacuum distillate, third-stage vacuum distillate, and fourth-stage vacuum distillate obtained by vacuum distillation of naphthenic crude oil.

[0046] In the present invention, the kinematic viscosity of naphthenic vacuum distillate at 100 °C ≥ 6 mm 2 / s, C A ≥ 18%.

[0047] In a preferred embodiment, the reaction temperature of the hydrotreating can be 300°C to 400°C, and its typical but non-limiting reaction temperatures are, for example, 300°C, 320°C, 340°C, 360°C, 380°C, 400°C; the volume ratio of hydrogen to naphthenic vacuum gas oil in the hydrotreating can be (600 - 1200):1, and its typical but non-limiting volume ratios are, for example, 600:1, 700:1, 800:1, 900:1, 1000:1, 1100:1, 1200:1.

[0048] In the present invention, the catalyst used in the hydrotreating reaction can be at least one of a molybdenum-nickel type hydrotreating catalyst, a tungsten-nickel type hydrotreating catalyst, a molybdenum-cobalt type hydrotreating catalyst, and a molybdenum-tungsten-nickel type hydrotreating catalyst.

[0049] In the present invention, the volume hourly space velocity in the hydrotreating can be 0.3 h -1 ~1.8 h -1 , and its typical but non-limiting volume hourly space velocities are, for example, 0.3 h -1 , 0.6 h -1 , 0.9 h -1 , 1.2 h -1 , 1.4 h -1 , 1.6 h -1 , 1.8 h -1 , and the hydrogen partial pressure can be greater than 10 MPa.

[0050] In a preferred embodiment, the heavy fraction of the hydrotreated product oil after removing the light fraction can be a fraction greater than 360°C, and its open flash point can be greater than 230°C.

[0051] In a preferred embodiment, the mass ratio of blending treatment oil B and treatment oil C can be 1:9 to 5:5, and its typical but non-limiting mass ratios are, for example, 1:9, 2:8, 3:7, 4:6, 5:5; the blending temperature can be 60°C to 180°C, and its typical but non-limiting temperatures are, for example, 60°C, 70°C, 80°C, 90°C, 100°C, 120°C, 140°C, 160°C, 180°C, and the blending time is not less than 15 min.

[0052] Blending treatment oil B and treatment oil C according to a specific mass ratio can ensure that the C A value of the obtained aromatic rubber plasticizer product is above 25%.

[0053] A typical preparation method of an aromatic rubber plasticizer includes the following steps:

[0054] (1) Subjecting naphthenic and / or intermediate base vacuum residue to a vacuum deep drawing process to obtain vacuum residue A after deep drawing;

[0055] The naphthenic and / or intermediate-base vacuum residue is the vacuum residue obtained by vacuum distillation of naphthenic and / or intermediate-base crude oil;

[0056] Among them, the distillation temperature for deep vacuum distillation is not lower than 500 °C;

[0057] (2) Using vacuum residue A as raw material, through the solvent deasphalting process, the deasphalted oil is obtained as treated oil B;

[0058] Among them, the solvent used in the solvent deasphalting is pentane, hexane and / or heptane;

[0059] In the solvent deasphalting, the top temperature of the extraction column is 130 °C to 170 °C, the bottom temperature is 120 °C to 160 °C, the internal pressure of the extraction column is 2.0 MPa to 4.5 MPa, and the solvent-to-oil ratio used is 4:1 to 10:1;

[0060] (3) Subjecting the naphthenic vacuum distillate oil to a hydrotreating reaction to obtain a hydrotreated product oil, and removing the light fractions from the obtained hydrotreated product oil to obtain a heavy fraction as treated oil C;

[0061] The naphthenic vacuum distillate oil is the second-stage reduced crude oil fraction, third-stage reduced crude oil fraction and / or fourth-stage reduced crude oil fraction obtained by vacuum distillation of naphthenic crude oil;

[0062] Among them, the reaction temperature of the hydrotreating is 300 °C to 400 °C, and the volume ratio of hydrogen to the naphthenic vacuum distillate oil is (600 - 1200):1;

[0063] The volume space velocity in the hydrotreating is 0.3 h -1 ~1.8 h -1 , and the hydrogen partial pressure is greater than 10 MPa;

[0064] The heavy fraction is the fraction greater than 360 °C, and the open flash point of the heavy fraction is greater than 230 °C;

[0065] (4) Blending treated oil B and treated oil C to obtain an aromatic rubber plasticizer;

[0066] Among them, the mass ratio of treated oil B and treated oil C for blending is 1:9 to 5:5, the blending temperature is 60 °C to 180 °C, and the blending time is not less than 15 min.

[0067] According to the second aspect of the present invention, there is provided an aromatic rubber plasticizer prepared by the preparation method described in any one of the above.

[0068] In a preferred embodiment, the C A value of the aromatic rubber plasticizer is above 25%, and the kinematic viscosity at 100 °C ≥ 20 mm 2 / s, flash point ≥ 240 °C, aniline point ≤ 75 °C.

[0069] In the present invention, analyzed by the GC-MS method, the content of benzo[a]pyrene in the aromatic rubber plasticizer is less than 1 mg / kg, and the content of PAHs is less than 10 mg / kg (the content of PAHs is the content of 8 aromatic hydrocarbons including benzo[a]pyrene, benzo[e]pyrene, benzo[a]anthracene, chrysene, benzo[b]fluoranthene, benzo[j]fluoranthene, benzo[k]fluoranthene, and dibenzo[a,h]anthracene), and the content of PCA is less than 3%.

[0070] In summary, the aromatic rubber plasticizer product of the present invention is green and environmentally friendly, and at the same time has a high aromatic hydrocarbon content, meeting the requirements of the limited substances for environmentally friendly processing oils in the "Technical Specification for Green Design Product Evaluation - Automotive Tires", that is, the content of BaP ≤ 1 mg / kg and the content of PAHs ≤ 10 mg / kg; the C A value of this aromatic rubber plasticizer product is above 25%, and the content of PCA is less than 3%. It has better compatibility with rubber compounds, carbon black, etc. during the tire preparation process, and can endow the tire with more excellent use performance.

[0071] The present invention will be further described below through examples. Unless otherwise specified, the materials in the examples are prepared according to existing methods or directly purchased from the market.

[0072] Example 1

[0073] A preparation method of an aromatic rubber plasticizer includes the following steps:

[0074] (1) Perform a vacuum deep drawing process on the Suizhong 36-1 vacuum residue (penetration 62 1 / 10 mm) produced by a refinery under the China National Offshore Oil Corporation to obtain a fraction greater than 500 °C, denoted as vacuum residue A1;

[0075] (2) Using vacuum residue A1 as the raw material, through a solvent deasphalting process, obtain deasphalted oil as treated oil B1;

[0076] In the solvent deasphalting process, the solvent used is pentane, the volume ratio of the solvent to the oil is 8:1, the top temperature of the extraction column is 155 °C, the bottom temperature of the column is 145 °C, and the operating pressure is 4.0 MPa;

[0077] (3) Using the Suizhong 36-1 second reduced-line distillate oil (kinematic viscosity at 100 °C ≥ 6 mm 2 / s, C A ≥ 18%) as the raw material, perform high-pressure hydrogenation treatment at a reaction pressure of 15 MPa, a reaction temperature of 340 °C, and a volume space velocity of 0.35 h -1React under the condition of a hydrogen - to - oil volume ratio of 1000:1 to obtain hydrogenated product oil. Cut off the light fraction from the obtained hydrogenated product oil to obtain a heavy fraction above 360°C as treated oil C1;

[0078] (4) Heat treated oil B1 and treated oil C1 to 80°C, then mix them according to a mass ratio of 30:70 for blending, and stir for 20 min to obtain an aromatic rubber plasticizer, the properties of which are shown in Table 1.

[0079] Example 2

[0080] A preparation method of an aromatic rubber plasticizer includes the following steps:

[0081] (1) Perform a vacuum deep - drawing process on the Suizhong 36 - 1 vacuum residue (penetration 62 1 / 10 mm) produced by a refinery under the China National Offshore Oil Corporation to obtain a fraction above 500°C, denoted as vacuum residue A2;

[0082] (2) Use vacuum residue A2 as raw material, and through a solvent deasphalting process, obtain deasphalted oil as treated oil B2;

[0083] In the solvent deasphalting process, the solvent used is pentane, the solvent - to - oil volume ratio is 8:1, the top temperature of the extraction column is 155°C, the bottom temperature is 145°C, and the operating pressure is 4.0 MPa;

[0084] (3) Use the Suizhong 36 - 1 second - stage reduced crude fraction oil (kinematic viscosity at 100°C ≥ 6 mm 2 / s, C A ≥ 18%) as raw material, perform high - pressure hydrogenation treatment, and react under the reaction pressure of 15 MPa, reaction temperature of 340°C, volume space velocity of 0.35 h -1 and a hydrogen - to - oil volume ratio of 1000:1 to obtain hydrogenated product oil. Cut off the light fraction from the obtained hydrogenated product oil to obtain a heavy fraction above 360°C as treated oil C2;

[0085] (4) Heat treated oil B2 and treated oil C2 to 80°C, then mix them according to a mass ratio of 28:72 for blending, and stir for 20 min to obtain an aromatic rubber plasticizer, the properties of which are shown in Table 1.

[0086] Table 1 Aromatic rubber plasticizer

[0087]

[0088] Comparative Example 1

[0089] The difference between this comparative example and Example 1 is that in step (1), the vacuum deep - drawing process is not carried out;

[0090] The remaining steps and their parameters are the same as those in Example 1;

[0091] Compared with Example 1, the defect of this comparative example is that without the vacuum deep distillation process, there are more light components in the raw materials, and the environmental protection indicators of the final product do not meet the requirements. Among them, the BaP content is 1.5 mg / kg, which is higher than the required index of not more than 1.0 mg / kg.

[0092] Comparative Example 2

[0093] The difference between this comparative example and Example 1 is that in step (2), the solvent deasphalting process is not carried out;

[0094] The remaining steps and their parameters are the same as those in Example 1;

[0095] Compared with Example 1, the defect of this comparative example is that without the solvent deasphalting process and directly carrying out blending, it will contain a large amount of gum and asphaltene, and the PCA content of the final product cannot be measured.

[0096] Comparative Example 3

[0097] The difference between this comparative example and Example 1 is that in step (3), the hydrotreating process is not carried out;

[0098] The remaining steps and their parameters are the same as those in Example 1;

[0099] Compared with Example 1, the defect of this comparative example is that without the hydrotreating process, the second reduced-line fraction oil contains a large amount of eight carcinogenic aromatic hydrocarbons. For the product obtained through the blending process, both the BaP content and the PAHs content do not meet the index requirements.

[0100] Comparative Example 4

[0101] The difference between this comparative example and Example 1 is that in step (3), the light fractions are not removed from the hydrogenated product oil;

[0102] The remaining steps and their parameters are the same as those in Example 1;

[0103] Compared with Example 1, the defect of this comparative example is that the hydrogenated product oil contains more light components. For the product obtained through the blending process, its open flash point is relatively low, only 174 °C, which does not meet the index and user requirements.

[0104] In summary, it can be seen that for the preparation method of the aromatic rubber plasticizer of the present invention, with the coordinated cooperation of each step, a high-C A value aromatic-based environmentally friendly rubber plasticizer with a high yield is obtained. It has excellent processing performance during the tire processing process, and is a non-toxic green product, which is beneficial to improving the overall economic efficiency.

[0105] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements for some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A preparation method of an aromatic rubber plasticizer, characterized in that Comprising the following steps: (a) Deep vacuum distillation of naphthenic and / or intermediate base vacuum residue to obtain vacuum residue A, and subjecting the obtained vacuum residue A to solvent deasphalting to obtain deasphalted oil as treated oil B; (b) Hydrotreating naphthenic vacuum distillate oil to obtain hydrotreated product oil, and removing light fractions from the obtained hydrotreated product oil to obtain heavy fractions as treated oil C; (c) Blending the treated oil B and treated oil C to obtain an aromatic rubber plasticizer.

2. The preparation method according to claim 1, characterized in that, In step (a), the distillation temperature of the deep vacuum distillation is not lower than 500 °C.

3. The preparation method according to claim 1, wherein In step (a), the solvent used in the solvent deasphalting includes at least one of pentane, hexane, and heptane, preferably pentane.

4. The preparation method according to claim 3, wherein The top temperature of the extraction column in the solvent deasphalting is 130 °C to 170 °C, and the bottom temperature is 120 °C to 160 °C; Preferably, the internal pressure of the extraction column in the solvent deasphalting is 2.0 MPa to 4.5 MPa; Preferably, the solvent-to-oil ratio used in the solvent deasphalting is 4:1 to 10:

1.

5. The preparation method according to any one of claims 1-4, characterized in that, In step (b), the naphthenic vacuum distillate oil includes at least one of the second reduced line distillate oil, the third reduced line distillate oil, and the fourth reduced line distillate oil obtained by vacuum distillation of naphthenic crude oil; Preferably, the kinematic viscosity of the naphthenic vacuum distillate at 100 °C is ≥ 6 mm 2 / s, and the C A ≥ 18%.

6. The preparation method according to claim 5, wherein The reaction temperature of the hydrotreating is 300 °C to 400 °C; Preferably, the volume ratio of hydrogen to naphthenic vacuum distillate oil in the hydrotreating is (600 - 1200):1; Preferably, the hourly space velocity in the hydrotreating is 0.3 h -1 ~1.8 h -1 , and the hydrogen partial pressure is greater than 10 MPa.

7. The preparation method according to claim 5, characterized in that, The heavy fractions are fractions greater than 360 °C; Preferably, the open flash point of the heavy fractions is greater than 230 °C.

8. The preparation method according to claim 1, characterized in that, The mass ratio of the treated oil B and treated oil C for blending is 1:9 to 5:5; Preferably, the blending temperature is 60 °C to 180 °C, and the blending time is not less than 15 min.

9. An aromatic rubber plasticizer prepared by the preparation method according to any one of claims 1 - 8.

10. The aromatic rubber plasticizer according to claim 9, characterized in that, The C of the aromatic rubber plasticizer A value is above 25%; Preferably, the kinematic viscosity of the aromatic rubber plasticizer at 100 °C ≥ 20 mm 2 / s, flash point ≥ 240 °C, aniline point ≤ 75 °C; Preferably, the benzo[a]pyrene content of the aromatic rubber plasticizer is less than 1 mg / kg, the PAHs content is less than 10 mg / kg, and the PCA content is less than 3%.

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