A process for preparing light white oil with low aromatic content from Fischer-Tropsch synthetic waxes

Abstract

This invention provides a process for preparing light white oil with low aromatic content from Fischer-Tropsch synthetic wax, comprising: Fischer-Tropsch synthetic wax undergoing hydrodeoxygenation under hydrorefining conditions to obtain refined Fischer-Tropsch synthetic wax; the refined Fischer-Tropsch synthetic wax entering a hydrocracking reactor undergoing hydrocracking isomerization to obtain wax conversion oil; the wax conversion oil entering a distillation separator undergoing distillation and being cut into diesel fraction and cracking tail oil, the diesel fraction being cut into light white oil, No. 5 industrial white oil, and a 230-290℃ distillate oil; some or all of the cracking tail oil being recycled to the hydrocracking reactor; the refined Fischer-Tropsch synthetic wax passing through a hydrocracking catalyst bed in the hydrocracking reactor, with a refining agent layer at the bottom of the reactor, and refining agent layers above the third and fourth hydrocracking catalyst beds, and quench hydrogen being added above the refining agent layers. This invention reduces the aromatic content in light white oil, achieving the goal of producing high-quality light white oil.

Description

Technical Field

[0001] This invention belongs to the field of coal chemical technology, specifically relating to a process for preparing light white oil with low aromatic content from Fischer-Tropsch synthetic wax. Background Technology

[0002] With increasing calls for environmental protection, the quality requirements for light white oil and diesel products are becoming more stringent, especially for indicators such as aromatic content, sulfur content, and cetane number.

[0003] Currently, to address the issue of deep aromatic removal from light white oil, relevant technologies have been studied to reduce the aromatic content of diesel and light white oil. CN110841701A describes a method for producing light white oil by reacting feedstock with a distillation range of 100℃~600℃ with two different molecular sieve catalysts. This method involves sequentially passing the light white oil feedstock through two reactors packed with different types of molecular sieves, resulting in light white oil with low aromatic content. This method utilizes a combination of precious metal catalysts for isomerization and pour point depletion, which can reduce the aromatic content in the light white oil feedstock. However, the precious metal catalysts used are expensive, leading to high costs.

[0004] CN100422295C discloses a method for producing food-grade light white oil from hydrotreated tail oil through hydrotreating and supplementary refining processes. Specifically, hydrotreated tail oil with an initial boiling point of 320-390℃ and a pour point of -20℃--10℃ is first subjected to isomerization and dewaxing using a molecular sieve hydrogenation catalyst, followed by high-pressure supplementary refining. Food-grade light white oil is obtained under conditions of hydrogen partial pressure of 11-18MPa and operating temperature of 200-300℃. However, this method involves high-pressure operation and harsh reaction conditions.

[0005] The existing technology uses molecular sieve catalysts for production, but the main problem is that the processing cost is high and high-value-added light white oil is not produced when producing diesel. Summary of the Invention

[0006] To overcome the shortcomings of the prior art, the present invention provides a process for obtaining light white oil with low aromatic content (not more than 0.01%), color greater than +30, and yield of more than 30% through a series of catalytic reactions using Fischer-Tropsch synthetic wax as raw material, while producing diesel fraction with by-product yield greater than 55% and pour point less than -20℃.

[0007] To achieve the objectives of this invention, the following technical solution is adopted:

[0008] A process for preparing light white oil with low aromatic content from Fischer-Tropsch synthetic wax includes the following steps:

[0009] (1) Under hydrorefining conditions, Fischer-Tropsch synthetic wax is obtained by hydrodeoxygenation reaction in a hydrorefining reactor.

[0010] (2) The refined wax obtained in step (1) is fed into a hydrocracking reactor and undergoes a hydrocracking isomerization reaction under hydrocracking conditions to obtain wax-to-oil conversion.

[0011] (3) The wax conversion oil obtained in step (2) enters the distillation separator and is then distilled and cut to obtain diesel fraction and cracked tail oil. The obtained diesel fraction is further cut to obtain light white oil, No. 5 industrial white oil and distillate oil at 230-290℃.

[0012] (4) Part or all of the cracked tail oil obtained in step (3) is recycled to the hydrocracking reactor;

[0013] In step (2), the Fischer-Tropsch refined wax passes from top to bottom through four hydrocracking catalyst beds in the hydrocracking reactor. A refining agent layer is provided at the bottom of the hydrocracking reactor, and a refining agent layer is provided above the third and fourth hydrocracking catalyst beds. Quenched hydrogen is added above the refining agent layers.

[0014] In this invention, the catalyst bed in the hydrocracking reactor is filled with four catalyst beds from top to bottom: a first hydrocracking catalyst bed, a second hydrocracking catalyst bed, a third hydrocracking catalyst bed, and a fourth hydrocracking catalyst bed. A refining agent layer is placed at the bottom of the hydrocracking reactor, and refining agent layers are also placed above the third and fourth hydrocracking catalyst beds. Quenched hydrogen is added above all three refining beds, so that the quenched hydrogen entering the hydrocracking reactor passes through the refining agent layer first as it moves downwards. This helps promote the olefin saturation reaction in the refining agent layer, reducing the possibility of aromatic hydrocarbon formation. Furthermore, the low temperature of the quenched hydrogen allows the refining agent layer to cool sufficiently, promoting the olefin saturation reaction. In some specific embodiments, a layer of ceramic balls can be placed above the refining agent layer, and low-temperature quenched hydrogen can be injected between the ceramic balls. The quenched hydrogen then moves downwards to the refining agent layer, providing a low-temperature environment for the olefin saturation reaction.

[0015] In the process of this invention, the mass ratio of the catalyst packed in the third hydrocracking catalyst bed in the hydrocracking reactor to the refining agent packed in the refining agent layer above the third hydrocracking catalyst bed is 10:(1-4), for example, 10:2, 10:2.5, 10:3; similarly, the mass ratio of the catalyst packed in the fourth hydrocracking catalyst bed to the refining agent packed in the refining agent layer above the fourth hydrocracking catalyst bed is 10:(1-4), for example, 10:2, 10:2.5, 10:3.

[0016] In some specific embodiments, a protective agent is placed at the top of the hydrocracking reactor. This protective agent can be selected from the FZC series, such as FZC-100, FZC-105, and FZC-106. By using a reasonably graded protective agent, mechanical impurities and trace metals in the feedstock can be effectively intercepted, protecting the main catalyst in the reactor and delaying the increase in catalyst bed pressure drop, thereby ensuring stable long-term operation of the unit.

[0017] In some specific embodiments, quench hydrogen is added above the second hydrocracking catalyst bed in the hydrocracking reactor.

[0018] In the process method of the present invention, the amount of quenched hydrogen added is 1% to 5% (volume ratio) of the amount of hydrogen recycled in the hydrocracking isomerization reaction in step (2).

[0019] In some specific embodiments of the process method of the present invention, the conditions for the hydrodeoxygenation reaction in step (1) are: reaction pressure of 3-10 MPa, for example, 4 MPa, 5 MPa, or 9 MPa; reaction temperature of 200-350°C, for example, 330°C or 340°C; and volume hourly space velocity of 1.0-3.0 h⁻¹. -1 For example, 1.2h -1 2.5h -1 2.7h -1 The hydrogen-to-oil volume ratio is 200:1 to 1000:1, for example, 300:1, 400:1, or 950:1; in some preferred embodiments, the reaction pressure is 6 to 8 MPa, for example, 7 MPa or 7.5 MPa; the reaction temperature is 200 to 300°C, for example, 250°C or 280°C; and the volume hourly space velocity is 1.5 to 2.0 h⁻¹. -1 For example, 1.5 hours -1 1.8h -1 1.9h -1 The hydrogen-to-oil volume ratio is 500:1 to 900:1, for example, 600:1 or 800:1.

[0020] In some specific embodiments, the catalyst packed in the hydrorefining reactor and the refining agent packed in the refining agent layer in step (2) are both sulfide catalysts, and the support is alumina.

[0021] In some specific embodiments of the process method of the present invention, the conditions for the hydrocracking isomerization reaction in step (2) are: reaction pressure of 3-10 MPa, for example, 4 MPa, 5 MPa, 9 MPa; reaction temperature of 280-400℃, for example, 290℃, 300℃; and volume hourly space velocity of 0.5-3 h⁻¹. -1 For example, 2.2h-1 2.6h -1 The hydrogen-to-oil volume ratio is 300:1 to 1000:1, for example, 350:1 or 900:1; in some preferred embodiments, the reaction pressure is 6 to 8 MPa, for example, 7 MPa or 7.5 MPa; the reaction temperature is 320 to 380°C, for example, 340°C or 370°C; and the volume hourly space velocity is 0.5 to 2 h⁻¹. -1 For example, 0.8h -1 1.5h -1 The hydrogen-to-oil volume ratio is 400:1 to 800:1, for example, 500:1 or 600:1.

[0022] In the process provided by this invention, the hydrocracking catalyst bed is filled with a hydrocracking catalyst, wherein the average pore size of the hydrocracking catalyst is 3-15 nm and the specific surface area is 200-500 m². 2 / g; the hydrocracking catalyst comprises a cracking component, a hydrogenation component, and a support; wherein the cracking component comprises amorphous silica-alumina and / or molecular sieves; the hydrogenation component is selected from non-precious metal components, preferably a combination of tungsten and molybdenum, or tungsten and nickel; the support is selected from alumina or silica. This hydrogenation component has weak acidity, effectively preventing secondary cracking of large-molecule oils to generate naphtha during the cracking reaction, thus improving the yield of light white oil and diesel fractions.

[0023] In the process step (3) provided by the present invention, the wax conversion oil is distilled and then cut to obtain diesel fraction (distillation range of 160-365℃) and cracked tail oil (fraction with a temperature greater than 365℃). The diesel fraction is further cut to obtain light white oil (distillation range of 160-230℃), No. 5 industrial white oil (distillation range of 290-365℃) and distillate oil with a temperature of 230-290℃.

[0024] In step (3) of the process method of the present invention, the aromatic content of the obtained light white oil is not greater than 0.01%, the color is greater than +30, and the yield is greater than 30%; the yield of the obtained diesel fraction is greater than 55%, and the pour point is less than -20℃; the aromatic content of the obtained No. 5 industrial white oil is not greater than 0.2%, and the yield is greater than 15%.

[0025] The above technical solution achieves the following technical effects:

[0026] The process of this invention simultaneously loads two catalysts with different functions into a hydrocracking reactor. By adjusting the positions of the hydrocracking catalyst and the refining agent, and by adding quench hydrogen above the refining agent layer, the aromatic content in light white oil is significantly reduced to below 0.01%, resulting in a color greater than +30 and a yield of over 30%, thus achieving the goal of producing high-quality light white oil. Attached Figure Description

[0027] Figure 1 : Process flow diagram of producing light white oil with low aromatic content used in Example 1 of this invention;

[0028] Figure 2 This is a specific embodiment of the internal packing structure of the hydrocracking reactor in Example 1 of the present invention. Detailed Implementation

[0029] To facilitate understanding of the present invention, the following description, in conjunction with embodiments, will further illustrate the invention. It should be understood that the following embodiments are merely for a better understanding of the invention and do not imply that the invention is limited to these embodiments.

[0030] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains.

[0031] Where specific experimental steps or conditions are not specified in the examples, the corresponding conventional experimental steps or conditions in this technical field can be followed. Reagents or instruments whose manufacturers are not specified are all commercially available conventional products.

[0032] The sources of raw materials used in the following embodiments and comparative examples of this invention are as follows:

[0033] The hydrorefining reactor is packed with hydrorefining / olefin refining catalyst: catalyst FF26, with an average pore size of 8.4 nm and a specific surface area of ​​160 m². 2 / g;

[0034] The hydrocracking catalyst packed in the hydrocracking reactor is a catalyst with nickel and tungsten as active components, wherein the mass fraction of NiO is 5% and the mass fraction of WO3 is 26%; the specific preparation method can be found in CN107661756A; the refining agent is the commercial catalyst FZC-204.

[0035] The top of the hydrocracking reactor is filled with FZC-100 series protective agent;

[0036] The properties of the raw material—Fischer-Tropsch synthetic wax—used in the following embodiments and comparative examples of this invention are shown in the table below:

[0037]

[0038]

[0039] The evaluation methods for the products obtained in the following embodiments and comparative examples are as follows:

[0040] Cetane number: GB / T386;

[0041] Sulfur content: SH / T0689;

[0042] Colorimetry: GB / T3555;

[0043] Aromatic hydrocarbon content: NB / SH / T 0966-2017;

[0044] Yield of light white oil (%) = {mass of fraction (distillation range 160-230℃) / mass of total product} × 100%;

[0045] Diesel fraction yield (%) = {(mass of fraction with distillation range of 160-365℃) / mass of total product} × 100%;

[0046] Yield (%) of No. 5 industrial white oil = {mass of fraction (distillation range 290-365℃) / mass of total product} × 100%.

[0047] The following embodiments of the present invention use a hydrocracking reactor having the following loading method:

[0048] The hydrocracking reactor is packed with four hydrocracking catalyst beds (all packed with the hydrocracking catalysts as described above). A refining agent bed is set at the bottom of the hydrocracking reactor. A refining agent bed (hydrocracking refining catalyst / olefin refining catalyst) is set above the third and fourth hydrocracking catalyst beds from top to bottom. Quenching hydrogen is added above the refining agent bed and above the second hydrocracking catalyst bed.

[0049] Example 1

[0050] (1) The Fischer-Tropsch synthetic wax is pumped to a preheating mixer and mixed with hydrogen. Then it is added to a hydrorefining reactor and hydrodeoxygenated under the catalysis of a catalyst to obtain the Fischer-Tropsch synthetic refined wax.

[0051] The conditions for the hydrodeoxygenation reaction were: reaction pressure (hydrogen partial pressure) of 7.4 MPa, reaction temperature of 260 °C, and volume hourly space velocity of 2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 500:1;

[0052] (2) The Fischer-Tropsch refined wax obtained in step (1) is transferred to a hydrocracking reactor and undergoes a hydrocracking isomerization reaction under the catalysis of a hydrocracking catalyst to obtain wax-converted oil; wherein, the mass ratio of the catalyst filled in the third hydrocracking catalyst bed in the hydrocracking reactor to the refined agent filled in the refined agent bed above it is 10:1, the mass ratio of the catalyst filled in the fourth hydrocracking catalyst bed to the refined agent filled in the refined agent bed above it is 10:2, and the amount of quench hydrogen added is 1% of the amount of hydrogen circulated in the hydrocracking isomerization reaction;

[0053] The conditions for the hydrocracking isomerization reaction are: reaction pressure (hydrogen partial pressure) of 7.4 MPa, reaction temperature of 350 °C, and volume hourly space velocity of 1.6 h⁻¹. -1 The hydrogen-to-oil volume ratio is 800:1;

[0054] (3) The wax conversion oil obtained in step (2) is transferred to a distillation separator. After distillation, it is cut to obtain diesel fraction (fraction range 160-365℃) and cracked tail oil (fraction >365℃). The obtained diesel fraction is further cut to obtain light white oil (fraction range 160-230℃), No. 5 industrial white oil (fraction range 290-365℃) and 230-290℃ distillate oil.

[0055] (4) Part or all of the cracked tail oil obtained in step (3) is recycled to the above-mentioned hydrocracking reactor.

[0056] Example 2

[0057] The difference between this embodiment and embodiment 1 is that: in step (2), the mass ratio of the catalyst filled in the third hydrocracking catalyst bed in the hydrocracking reactor to the refining agent filled in the refining agent layer above it is 10:2, and the mass ratio of the catalyst filled in the fourth hydrocracking catalyst bed to the refining agent filled in the refining agent layer above it is 10:3.

[0058] Example 3

[0059] The difference between this embodiment and embodiment 1 is that: in step (2), the mass ratio of the catalyst filled in the third hydrocracking catalyst bed in the hydrocracking reactor to the refining agent filled in the refining agent layer above it is 10:3, and the mass ratio of the catalyst filled in the fourth hydrocracking catalyst bed to the refining agent filled in the refining agent layer above it is 10:4.

[0060] Comparative Example 1

[0061] (1) The Fischer-Tropsch synthetic wax is pumped to a preheating mixer and mixed with hydrogen. Then it is added to a hydrorefining reactor and hydrodeoxygenated under the catalysis of a catalyst to obtain the Fischer-Tropsch synthetic refined wax.

[0062] The conditions for the hydrodeoxygenation reaction were: reaction pressure (hydrogen partial pressure) of 7.4 MPa, reaction temperature of 360 °C, and volume hourly space velocity of 2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 500:1;

[0063] (2) The Fischer-Tropsch refined wax obtained in step (1) is transferred to a hydrocracking reactor and undergoes hydrocracking isomerization reaction under the catalysis of a hydrocracking catalyst to obtain wax-to-oil conversion. In this step, the hydrocracking reactor has the same packing structure of each bed as the hydrocracking reactor used in Example 1 and the same hydrocracking isomerization reaction conditions. The only difference is that no quench hydrogen is added.

[0064] The conditions for the hydrocracking isomerization reaction are: reaction pressure (hydrogen partial pressure) of 7.4 MPa, reaction temperature of 350 °C, and volume hourly space velocity of 1.6 h⁻¹. -1 The hydrogen-to-oil volume ratio is 800:1;

[0065] (3) The wax conversion oil obtained in step (2) is transferred to a distillation separator and distilled to obtain diesel fraction (distillation range 160-365℃) and cracked tail oil (distillation range >365℃); the obtained diesel fraction is further divided to obtain light white oil (distillation range 160-230℃), No. 5 industrial white oil (distillation range 290-365℃) and distillate oil at 230-290℃;

[0066] (4) Part or all of the cracked tail oil obtained in step (3) is recycled to the above-mentioned hydrocracking reactor.

[0067] Comparative Example 2

[0068] The only difference between this comparative example and Example 1 is the packing structure of the catalyst bed in the hydrocracking reactor in step (2) and the location of the quench hydrogen replenishment: the hydrocracking reactor in this comparative example has four hydrocracking catalyst beds, a refining agent layer is set at the bottom of the hydrocracking reactor, and a refining agent layer is set below the third and fourth hydrocracking catalyst beds; specifically, the mass ratio of the catalyst filled in the third hydrocracking catalyst bed to the refining agent filled in the refining agent layer below it is 10:2, and the mass ratio of the catalyst filled in the fourth hydrocracking catalyst bed to the refining agent filled in the refining agent layer below it is 10:3.

[0069] Quenched hydrogen is added above the third, fourth, and second hydrocracking catalyst beds (the amount added is 1% of the amount of hydrogen recycled in the hydrocracking isomerization reaction).

[0070] The properties of the light white oil, diesel fraction, and No. 5 industrial white oil obtained in the above examples and comparative examples were tested, and the results are shown in the table below:

[0071] Table 1 Light White Oil

[0072] Yield (wt%) chromaticity Aromatic hydrocarbon content (wt%) Example 1 30～35 30～33 0.008～0.01 Example 2 30～35 30～33 0.008～0.009 Example 3 30～35 30～33 0.007～0.009 Comparative Example 1 30～35 25～27 0.040～0.065 Comparative Example 2 30～35 26～28 0.023～0.035

[0073] Table 2 Diesel fractions

[0074] Yield (wt%) Pour point (°C) Example 1 55～65 -20～-25 Example 2 55～65 -20～-25 Example 3 55～65 -20～-25 Comparative Example 1 45～53 -20～-25 Comparative Example 2 55～65 -20～-25

[0075] Table 3 No. 5 Industrial White Oil

[0076] Yield (wt%) Aromatic hydrocarbon content (wt%) Example 1 15～20 0.18 Example 2 15～20 0.16 Example 3 15～20 0.12 Comparative Example 1 10～15 0.40 Comparative Example 2 15～18 0.30

[0077] As can be seen from the data in Tables 1-3, the process of the present invention, by simultaneously loading two catalysts with different functions into the hydrocracking reactor, adjusting the positions of the hydrocracking catalyst and the refining agent, and adding quench hydrogen above the refining agent layer, significantly reduces the aromatic content in light white oil to below 0.01%, the color to greater than +30, and the yield to over 30%. At the same time, it can also produce diesel fractions with a pour point below -20℃ and a yield of over 55% as byproducts.

Claims

1. A process for preparing light white oil with low aromatic content from Fischer-Tropsch synthetic wax, characterized in that, Includes the following steps: (1) Under hydrorefining conditions, Fischer-Tropsch synthetic wax is obtained by hydrodeoxygenation reaction in a hydrorefining reactor; (2) The Fischer-Tropsch refined wax obtained in step (1) enters the hydrocracking reactor and undergoes a hydrocracking isomerization reaction under hydrocracking conditions to obtain wax-to-oil conversion. (3) The wax conversion oil obtained in step (2) enters the distillation separator and is then distilled and cut to obtain diesel fraction and cracked tail oil. The obtained diesel fraction is further cut to obtain light white oil, No. 5 industrial white oil and distillate oil at 230-290℃. (4) Part or all of the cracked tail oil obtained in step (3) is recycled to the hydrocracking reactor; In step (2), the Fischer-Tropsch refined wax passes from top to bottom through four hydrocracking catalyst beds in the hydrocracking reactor. A refining agent layer is provided at the bottom of the hydrocracking reactor, and a refining agent layer is provided above the third and fourth hydrocracking catalyst beds. Quenched hydrogen is added above the refining agent layers.

2. The process according to claim 1, characterized in that, In the hydrocracking reactor, the mass ratio of the catalyst filled in the third hydrocracking catalyst bed to the refining agent filled in the refining agent bed above it is 10:(1~4). The mass ratio of the catalyst filling the fourth hydrocracking catalyst bed to the refining agent filling the refining agent layer above it is 10:(1~4).

3. The process according to claim 1, characterized in that, A protective agent is placed on top of the hydrocracking reactor.

4. The process according to claim 3, characterized in that, Quenched hydrogen is added above the second hydrocracking catalyst bed in the hydrocracking reactor.

5. The process according to claim 3, characterized in that, The amount of quenched hydrogen added is 1% to 5% of the amount of hydrogen recycled in the hydrocracking isomerization reaction in step (2).

6. The process according to any one of claims 1 to 5, characterized in that, The conditions for the hydrodeoxygenation reaction described in step (1) are: reaction pressure of 3~10 MPa, reaction temperature of 200~350℃, and volume hourly space velocity of 1.0~3.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 200:1 to 1000:

1.

7. The process according to claim 6, characterized in that, The reaction pressure was 6–8 MPa, the reaction temperature was 200–300 °C, and the volume hourly space velocity was 1.5–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 500:1 to 900:

1.

8. The process according to claim 6, characterized in that, The catalyst packed in the hydrogenation refining reactor and the refining agent packed in the refining agent layer in step (2) are both sulfide catalysts, and the support is alumina.

9. The process according to any one of claims 1-5 and 7-8, characterized in that, The conditions for the hydrocracking isomerization reaction described in step (2) are: reaction pressure of 3~10 MPa, reaction temperature of 280~400℃, and volume hourly space velocity of 0.5~3h. -1 The hydrogen-to-oil volume ratio is 300:1 to 1000:

1.

10. The process according to claim 9, characterized in that, The reaction pressure was 6–8 MPa, the reaction temperature was 320–380 °C, and the volume hourly space velocity was 0.5–2 h⁻¹. -1 The hydrogen-to-oil volume ratio is 400:1 to 800:

1.

11. The process according to claim 9, characterized in that, The hydrocracking catalyst bed is filled with a hydrocracking catalyst, which has an average pore size of 3-15 nm and a specific surface area of ​​200-500 m². 2 / g; The hydrocracking catalyst includes a cracking component, a hydrogenation component, and a support; The cracking component includes amorphous silica-alumina and / or molecular sieves; the hydrogenation component is selected from non-precious metal components. The carrier is selected from alumina or silicon dioxide.

12. The process according to claim 11, characterized in that, The hydrogenation component is selected from tungsten and molybdenum, or a combination of tungsten and nickel.

13. The process according to any one of claims 1-5, 7-8, and 10-12, characterized in that, In step (3), the distillation range of the diesel fraction is 160~365℃, wherein the distillation range of the light white oil is 160~230℃, and the distillation range of the No. 5 industrial white oil is 290~365℃. The cracked tail oil has a distillation range of >365℃.

14. The process according to any one of claims 1-5, 7-8, and 10-12, characterized in that, The light white oil obtained in step (3) has an aromatic content of no more than 0.01%, a color greater than +30, and a yield of more than 30%. The yield of the diesel fraction is greater than 55%, and the pour point is less than -20°C. The No. 5 industrial white oil has an aromatic content of no more than 0.2% and a yield of more than 15%.

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