CN111171862A - Preparation method of heat conduction oil base oil - Google Patents
Preparation method of heat conduction oil base oil Download PDFInfo
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- CN111171862A CN111171862A CN202010054616.2A CN202010054616A CN111171862A CN 111171862 A CN111171862 A CN 111171862A CN 202010054616 A CN202010054616 A CN 202010054616A CN 111171862 A CN111171862 A CN 111171862A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
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Abstract
The invention provides a preparation method of heat conduction oil base oil, which comprises the following steps: and mixing the adsorbent with naphthenic base normal second-line distillate oil, refining, and carrying out solid-liquid separation to obtain the heat-conducting oil base oil. The preparation method is simple in process flow, strong in operability and low in production cost, and the prepared heat-conducting oil base oil is high in flash point, good in liquidity, low in toxicity and low in condensation point, so that the economic benefit of an enterprise is improved.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, relates to a preparation method of base oil, and particularly relates to a preparation method of heat conduction oil base oil.
Background
The thermal oil is a medium for transferring heat in a heating apparatus and/or a cooling apparatus, and can be classified into synthetic type thermal oil and mineral type thermal oil according to components and manufacturing industrial processes.
The synthetic heat conducting oil is generally composed of a plurality of isomers or mixtures with similar chemical properties, the main components comprise biphenyl, naphthalene, diphenyl ether and mixtures thereof, and common types comprise alkylbenzene type, alkyl naphthalene type, alkyl biphenyl type, biphenyl and diphenyl ether mixed type, hydrogenated terphenyl type, organosilicon mineral oil type and the like; the mineral heat conduction oil is prepared by taking heat conduction oil base oil as a raw material, standing, adding an antioxidant, a stabilizer and the like, and blending.
The base oil of the mineral oil heat conduction oil is prepared by sequentially carrying out multi-stage processing technologies such as hydrofining, hydro-upgrading, clay refining and rectification on the base oil by taking normal-pressure or vacuum distillate oil as a raw material, and the preparation process is complex in flow, high in cost and not beneficial to reducing the production cost of the heat conduction oil.
CN 106047405A discloses a method for producing heat transfer oil by using naphthenic base crude oil, which comprises the following steps: distilling the original cycloalkyl raw material to obtain raw oil; hydrofining raw oil to obtain hydrofined oil; and (4) performing clay refining on the hydrogenated refined oil to obtain the heat conduction oil. Although the method can meet the requirements of related brand heat-conducting oil products in GB/T23971-2009, the requirements on production equipment are high due to the steps of hydrofining, the production cost of the heat-conducting oil is increased, and the safety risk exists.
CN 1803997A discloses a production method of heat-conducting oil base oil, which comprises the following steps: raw oil and hydrogen are contacted with a hydrogenation pre-refining catalyst in a hydrogenation modification device to remove impurities such as sulfur, nitrogen and the like, and a hydrogenation pre-refining reaction product is contacted with the hydrogenation modification catalyst to react and remove impurities such as sulfur, nitrogen and the like to obtain hydrogenation product oil; and (3) fractionating the hydrogenated oil to obtain different narrow fractions, namely the heat transfer fluid base oil. Although the base oil prepared by the production method has low freezing point, good fluidity and low toxicity, the process flow is more complicated, and the production cost is increased.
Aiming at the defects of multi-stage hydrogenation process, complex process flow, high production cost and high safety risk in the prior art for producing the heat conduction oil base oil, the preparation method of the heat conduction oil base oil with simple process flow, strong operability and low production cost is provided, and the preparation method has important significance for improving the production safety and the economic benefit of enterprises.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide the preparation method of the heat conduction oil base oil, so that the preparation method is simple in process flow and strong in operability, the production cost of the heat conduction oil base oil is reduced, and meanwhile, the obtained heat conduction oil base oil is high in flash point, low in condensation point, good in fluidity and low in toxicity.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a preparation method of heat conduction oil base oil, which comprises the following steps:
and mixing the adsorbent with naphthenic base normal second-line distillate oil, refining, and carrying out solid-liquid separation to obtain the heat-conducting oil base oil.
Preferably, the cycloalkyl-normal second-line distillate has a distillation range of 270 to 360 ℃, for example 270 to 360 ℃, 280 to 350 ℃, 290 to 340 ℃, 270 to 330 ℃, 275 to 335 ℃, 290 to 350 ℃, 395 to 355 ℃ or 300 to 360 ℃, but not limited to the recited values, and other values not recited within the range of values are equally applicable, preferably 280 to 350 ℃.
The naphthenic base normal second-line distillate oil is naphthenic base normal second-line distillate oil with the distillation range of 270-360 ℃. When the distillation range of the naphthenic base normal second-line distillate oil extracted by the atmospheric tower is in the range of 270-360 ℃, directly mixing the adsorbent with the naphthenic base normal second-line distillate oil, and then carrying out refining treatment to obtain heat-conducting oil base oil meeting the requirements; when the initial boiling point of the naphthenic base normal second-line distillate oil extracted from the atmospheric tower is lower than 270 ℃ and/or the final boiling point is higher than 360 ℃, the naphthenic base normal second-line distillate oil is subjected to distillation cutting treatment to obtain the naphthenic base normal second-line distillate oil with the distillation range of 270-360 ℃.
The preparation method provided by the invention can be used for preparing the heat-conducting oil base oil with high flash point, low condensation point, good fluidity and low toxicity only by two steps of operation including distillation and adsorption at most, and has the advantages of simple process flow, strong operability and low production cost.
Preferably, the adsorbent comprises any one or a combination of at least two of molecular sieve, activated alumina, activated clay, particulate clay, or activated carbon, typical but non-limiting combinations include combinations of molecular sieve and activated alumina, activated alumina and activated clay, activated clay and particulate clay, particulate clay and activated carbon, molecular sieve, activated alumina and activated clay, activated alumina, activated clay and particulate clay, activated alumina, particulate clay and activated carbon, or molecular sieve, activated alumina, activated clay, particulate clay and activated carbon.
Preferably, the molecular sieve comprises any one or a combination of at least two of a ZSM-5 molecular sieve, a 5A molecular sieve or a carbon molecular sieve, typical but non-limiting combinations include a combination of a ZSM-5 molecular sieve and a 5A molecular sieve, a combination of a 5A molecular sieve and a carbon molecular sieve, a combination of a ZSM-5 molecular sieve and a carbon molecular sieve or a combination of a ZSM-5, 5A molecular sieve and a carbon molecular sieve.
Preferably, the adsorbent is added in an amount of 3 to 50% of the mass of the distillate, for example 3%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45% or 50%, but not limited to the recited values, and other values not recited in the range of values are equally applicable, preferably 5 to 30%.
Preferably, the purification treatment temperature is 80-160 ℃, for example can be 80 ℃, 90 ℃, 100 ℃, 110 ℃, 120 ℃, 130 ℃, 140 ℃, 150 ℃ or 160 ℃, but not limited to the enumerated values, within the range of other values are also applicable; the time is 20-40min, for example 20min, 25min, 30min, 35min or 40min, but is not limited to the values listed, and other values not listed in the numerical range are equally applicable.
Further preferably, the temperature of the purification treatment is 100 to 150 ℃, for example, 100 ℃, 110 ℃, 120 ℃, 130 ℃, 140 ℃ or 150 ℃, but not limited to the recited values, and other values not recited in the numerical range are also applicable; the time is 25-35min, for example 25min, 28min, 30min, 32min or 35min, but is not limited to the values listed, and other values not listed in the numerical range are equally applicable.
Preferably, the purification treatment is carried out under stirring.
The stirring can increase the contact effect of the adsorbent and the naphthenic base common second-line distillate oil, thereby improving the adsorption efficiency. The stirring of the invention only needs to stir the adsorbent, and the stirring speed is not limited too much here.
As a preferable technical scheme of the preparation method, the preparation method comprises the following steps:
mixing an adsorbent with naphthenic base normal second-line distillate oil, wherein the distillation range of the naphthenic base normal second-line distillate oil is 270-360 ℃; the addition amount of the adsorbent is 3-50% of the mass of the distillate oil, the refining treatment is completed by stirring for 20-40min at the temperature of 80-160 ℃, and the heat conduction oil base oil is obtained after solid-liquid separation.
The recitation of numerical ranges herein includes not only the above-recited numerical values, but also any numerical values between non-recited numerical ranges, and is not intended to be exhaustive or to limit the invention to the precise numerical values encompassed within the range for brevity and clarity.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the invention, at most, only two-stage processing of distillation and adsorption refining is needed, so that impurities such as sulfur, nitrogen, polycyclic aromatic hydrocarbon and the like in the naphthenic base normal second-line distillate oil can be removed, the heat-conducting oil base oil with high flash point, low viscosity, low condensation point, good fluidity and low toxicity is obtained, and the physicochemical properties of the heat-conducting oil base oil are superior to those of GB/T23971-2009;
(2) compared with the existing multistage hydrofining method, the preparation method provided by the invention has the advantages of simple process flow and lower production cost, and realizes high added value utilization of naphthenic base common second-line distillate oil.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments.
Example 1
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
mixing activated clay with middle-sea oil Qinhuang island 32-6 naphthenic base second-line distillate oil with the distillation range of 290-350 ℃, stirring for 30min at 100 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil; the addition amount of the activated clay is 15 percent of the mass of the naphthenic base common second-line distillate oil.
The activated clay has decolorizing power of 182, activity degree of 189mol/kg and specific surface area of 254m2Activated clay/g.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 188 ℃, the closed flash point is 169 ℃, and the kinematic viscosity at 40 ℃ is 17.49mm2S, kinematic viscosity at 100 ℃ of 3.22mm2The color number is 0.7, the sulfur content is 1321mg/kg, the nitrogen content is 23.8mg/kg, the acid value is 0.03mg KOH/g, and the pour point is-42 ℃.
Example 2
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
mixing activated clay with 32-6 cycloalkyl second-line distillate oil of Qinhuang island of middle-sea oil with the distillation range of 280-330 ℃, stirring for 30min at the temperature of 120 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil; the addition amount of the activated clay is 15 percent of the mass of the naphthenic base common second-line distillate oil.
The activated clay has decolorizing power of 185, activity degree of 181mol/kg and specific surface area of 268m2Activated clay/g.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 187 ℃, the closed flash point is 169 ℃, and the kinematic viscosity at 40 ℃ is 17.38mm2S, kinematic viscosity at 100 ℃ of 3.21mm2The color number is 0.7, the sulfur content is 1356mg/kg, the nitrogen content is 22.6mg/kg, the acid number is 0.02mg KOH/g, and the pour point is-42 ℃.
Example 3
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
mixing X-P type active alumina with medium-sea oil Subson 36-1 naphthenic common second-line distillate oil with the distillation range of 290-350 ℃, stirring for 25min at 150 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil; the addition amount of the X-P type active alumina is 5 percent of the mass of distillate oil.
The specific surface area of the X-P type activated alumina is 282m2(g), the particle diameter D90 is 2 mm.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 190 ℃, the closed flash point is 170 ℃, and the kinematic viscosity at 40 ℃ is 17.19mm2S, kinematic viscosity at 100 ℃ of 3.14mm2The color number is 0.6, the sulfur content is 1342mg/kg, the nitrogen content is 21.7mg/kg, the acid number is 0.02mg KOH/g, and the pour point is-42 ℃.
Example 4
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
(1) distilling and cutting 9-3 naphthenic base normal second-line distillate oil of the middle sea oil, removing fractions with the temperature of less than 300 ℃ and more than 360 ℃ to obtain the naphthenic base normal second-line distillate oil with the distillation range of 300-360 ℃;
(2) and (2) mixing a ZSM-5 molecular sieve with the naphthenic base second-line distillate oil with the distillation range of 300-360 ℃ obtained in the step (1), wherein the addition amount of the ZSM-5 molecular sieve is 30% of the mass of the naphthenic base second-line distillate oil, stirring for 35min at the temperature of 100 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 191 ℃, the closed flash point is 172 ℃, and the kinematic viscosity at 40 ℃ is 17.86mm2S, kinematic viscosity at 100 ℃ of 3.25mm2The color number is 0.8, the sulfur content is 1450mg/kg, the nitrogen content is 21.5mg/kg, the acid number is 0.03mg KOH/g, and the pour point is-39 ℃.
Example 5
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
(1) distilling and cutting 32-6 naphthenic base normal second-line distillate oil of Qinhuang island of middle sea oil, removing fractions with the temperature of less than 270 ℃ and more than 330 ℃ to obtain the naphthenic base normal second-line distillate oil with the distillation range of 270-330 ℃;
(2) and (2) mixing coconut shell powder-shaped activated carbon with the naphthenic base normal second-line distillate oil with the distillation range of 270-330 ℃ obtained in the step (1), wherein the addition amount of the coconut shell powder-shaped activated carbon is 3% of the mass of the naphthenic base normal second-line distillate oil, stirring for 20min at 160 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil.
The coconut shell powder-shaped activated carbon has a particle size of-200 meshes to +300 meshes.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 186 ℃, the closed flash point is 171 ℃, and the kinematic viscosity at 40 ℃ is 17.98mm2S, kinematic viscosity at 100 ℃ of 3.57mm2The color number is 0.7, the sulfur content is 1758mg/kg, the nitrogen content is 28.5mg/kg, the acid value is 0.03mg KOH/g, and the pour point is-42 ℃.
Example 6
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
mixing activated clay with 32-6 cycloalkyl second-line distillate oil of Qinhuang island of Zhonghai oil with the distillation range of 295-350 ℃, stirring for 40min at 80 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil; the addition amount of the activated clay is 50 percent of the mass of distillate oil.
The activated clay has decolorizing power of 178, activity degree of 183mol/kg and specific surface area of 249m2Activated clay/g.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 187 ℃, the closed flash point is 170 ℃, and the kinematic viscosity at 40 ℃ is 17.65mm2S, kinematic viscosity at 100 ℃ of 3.29mm2The color number is 0.8, the sulfur content is 1354mg/kg, the nitrogen content is 24.1mg/kg, the acid number is 0.03mg KOH/g, and the pour point is-42 ℃.
Example 7
The embodiment provides a preparation method of heat conduction oil base oil, which comprises the following steps:
(1) distilling and cutting 36-1 naphthenic normal second-line distillate of medium marine oil seiulus, and removing fractions with the temperature of less than 275 ℃ and more than 350 ℃ to obtain the naphthenic normal second-line distillate with the distillation range of 275-350 ℃;
(2) mixing particle clay with the naphthenic base normal second-line distillate oil with the distillation range of 275-350 ℃ obtained in the step (1), wherein the addition amount of the particle clay is 15% of the mass of the naphthenic base normal second-line distillate oil, stirring for 30min at 120 ℃, and performing solid-liquid separation to obtain the heat-conducting oil base oil.
The specific surface area of the granular argil is 403m2/g。
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 190 ℃, the closed flash point is 173 ℃, and the kinematic viscosity at 40 ℃ is 17.31mm2S, kinematic viscosity at 100 ℃ of 3.28mm2The color number per second is 0.6, the sulfur content is 1366mg/kg, the nitrogen content is 20.9mg/kg, the acid number is 0.03mg KOH/g, and the pour point is-39 ℃.
Comparative example 1
The comparative example provides a preparation method of heat conduction oil base oil, which comprises the following steps:
mixing activated clay with 32-6 cycloalkyl second-line distillate oil of Qinhuang island of middle sea oil with distillation range of 255-310 deg.C, stirring at 100 deg.C for 30min, and performing solid-liquid separation to obtain heat transfer oil base oil; the addition amount of the activated clay is 15 percent of the mass of the naphthenic base common second-line distillate oil.
The activated clay has decolorizing power of 182, activity degree of 189mol/kg and specific surface area of 254m2Activated clay/g.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 162 ℃, the closed flash point is 153 ℃, and the kinematic viscosity at 40 ℃ is 15.23mm2(s) kinematic viscosity at 100 ℃ of 2.89mm2The color number is 0.7, the sulfur content is 1379mg/kg, the nitrogen content is 19.8mg/kg, the acid number is 0.04mg KOH/g, and the pour point is-36 ℃.
The open flash point of the heat-conducting oil base oil does not meet the requirement that the open flash point is not less than 180 ℃ in GB/T23971-2009.
Comparative example 2
The comparative example provides a preparation method of heat conduction oil base oil, which comprises the following steps:
mixing activated clay with middle-sea oil Qinhuang island 32-6 naphthenic base second-line distillate oil with the distillation range of 290-350 ℃, stirring for 30min at 100 ℃, and performing solid-liquid separation to obtain heat-conducting oil base oil; the addition amount of the activated clay is 1 percent of the mass of the naphthenic base common second-line distillate oil.
The activated clay has decolorizing power of 182, activity degree of 189mol/kg and specific surface area of 254m2Activated clay/g.
The closed flash point, the open flash point, the kinematic viscosity, the sulfur content, the nitrogen content, the acid value, the pour point and the chromaticity of the heat transfer oil base oil are measured according to the methods disclosed in GB/T261-2008, GB/T3536-2008, GB/T265-1988, GB/T17040-2008, SH/T0657-2007, GB/T7304-2014, GB/T3535-2006 and GB/T6540-1986 respectively, and the obtained results are as follows:
the open flash point is 190 ℃, the closed flash point is 172 ℃, and the kinematic viscosity at 40 ℃ is 14.52mm2/s，100℃Kinematic viscosity of 2.79mm2The color number is 1.2, the sulfur content is 2132mg/kg, the nitrogen content is 29.13mg/kg, the acid number is 0.07mg KOH/g, and the pour point is-39 ℃.
The sulfur content and acid value of the heat-conducting oil base oil do not meet the requirements that the sulfur content in GB/T23971-2009 is not more than 2000mg/kg and the acid value is not more than 0.05mg KOH/g.
From examples 1 to 7, it can be known that the preparation method provided by the invention can remove sulfur, nitrogen, polycyclic aromatic hydrocarbon and other impurities in the naphthenic base common second-line distillate oil only by two processing technologies of distillation cutting and adsorption refining at most, so as to obtain the heat-conducting oil base oil with high flash point, low viscosity, low condensation point, good fluidity and low toxicity, and the physicochemical properties of the heat-conducting oil base oil are all superior to the GB/T23971-2009 index requirements. Compared with the existing multistage hydrofining method, the preparation method provided by the invention has the advantages of simple process flow and lower production cost, and realizes high added value utilization of naphthenic base common second-line distillate oil.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention, and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The preparation method of the heat conduction oil base oil is characterized by comprising the following steps: and mixing the adsorbent with naphthenic base normal second-line distillate oil, refining, and carrying out solid-liquid separation to obtain the heat-conducting oil base oil.
2. The process according to claim 1, wherein the distillation range of the naphthenic normal second-line distillate is 270-360 ℃.
3. The process according to claim 1 or 2, wherein the distillation range of the naphthenic normal second-line distillate is 280-350 ℃.
4. The method of any one of claims 1 to 3, wherein the adsorbent comprises any one of or a combination of at least two of molecular sieve, activated alumina, activated clay, granular clay, or activated carbon.
5. The method of claim 4, wherein the molecular sieve comprises any one of or a combination of at least two of a ZSM-5 molecular sieve, a 5A molecular sieve, or a carbon molecular sieve.
6. The process according to any one of claims 1 to 5, wherein the adsorbent is added in an amount of 3 to 50%, preferably 5 to 30%, based on the mass of the naphthenic common second-line distillate.
7. The production method according to any one of claims 1 to 6, wherein the temperature of the refining treatment is 80 to 160 ℃ and the time is 20 to 40 min.
8. The method according to claim 7, wherein the refining treatment is carried out at a temperature of 100 to 150 ℃ for 25 to 35 min.
9. The production method according to any one of claims 1 to 8, wherein the refining treatment in step (2) is carried out under stirring.
10. The production method according to any one of claims 1 to 9, characterized by comprising the steps of: mixing an adsorbent with naphthenic base normal second-line distillate oil, wherein the distillation range of the naphthenic base normal second-line distillate oil is 270-360 ℃; the addition amount of the adsorbent is 3-50% of the mass of the distillate oil, the refining treatment is completed by stirring for 20-40min at the temperature of 80-160 ℃, and the heat conduction oil base oil is obtained after solid-liquid separation.
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