Device for producing isododecane

Abstract

The utility model relates to a device for producing isododecane, which comprises a mixing tank, a light component removal tower, a heavy component removal tower, a rotary valve and a rectifying tower, and is characterized in that the mixing tank is configured to be used for mixing Fischer-Tropsch refined first-time oil and Fischer-Tropsch cracked first-time oil; the middle part of the light component removal tower is constructed to be communicated with the mixing tank through a first feeding pipeline; the bottom of the light component removal tower is constructed to be communicated with the heavy component removal tower through a first discharging pipeline, and a second discharging pipeline is arranged at the top of the light component removal tower; the heavy component removal tower is communicated with the light component removal tower, and the heavy component removal tower is configured to be used for removing fractions with the carbon number not smaller than 16 in the second raw oil to obtain third raw oil; the rotary valve is communicated with the de-heavy tower, and the rotary valve is configured to be used for removing normal fractions in the third raw oil to obtain fourth raw oil; the rectifying tower is communicated with the rotary valve and is configured to be used for rectifying the fourth raw oil to obtain an isododecane product. The device for producing isododecane provided by the utility model has the advantages that the process is simple, the production cost is saved, and the energy consumption is reduced.

Description

Technical Field

[0001] The present disclosure relates to the field of chemical technology, and more specifically, to a device for producing isododecane. Background Art

[0002] Isododecane is primarily used in the cosmetics industry, where high product quality requirements are required, including harmlessness to the human body. Its characteristics include being clear, colorless, odorless, and virtually free of aromatic hydrocarbons and sulfur. It is easily biodegradable, leaves no residue, and leaves a refreshing skin feel. Its rapid evaporation makes it a perfect replacement for volatile silicone oils, providing water resistance and sweat resistance, making it suitable for dry skin and hair care products. It exhibits excellent compatibility and is completely soluble in silicone oil, mineral oil, other hydrocarbons, and isoparaffins. Its low density and viscosity, combined with a minimal oily feel, improve skin feel and oil solubility, enhancing product spreadability and application. It also serves as a lubricant and softening agent in emulsions, alcohol-water systems, and anhydrous systems, enhancing compatibility across diverse systems. Its high degree of isomerization makes it safe and environmentally friendly. Existing isododecane production equipment is complex, time-consuming, costly, and energy-intensive, and the product also contains a high content of aromatic hydrocarbons. Utility Model Content

[0003] In view of this, an embodiment of the present disclosure provides a device for producing isododecane to solve the technical defects existing in the prior art.

[0004] To achieve the above objectives, the present disclosure adopts the following technical solutions:

[0005] The present disclosure provides a device for producing isododecane, comprising:

[0006] A mixing tank configured to mix Fischer-Tropsch refined conventional first-line oil and Fischer-Tropsch cracked conventional first-line oil, wherein the Fischer-Tropsch refined conventional first-line oil and the Fischer-Tropsch cracked conventional first-line oil are mixed to form a first feedstock oil;

[0007] A light-removal tower, wherein the middle portion of the light-removal tower is configured to communicate with a mixing tank via a first feed pipe; the bottom portion of the light-removal tower is configured to communicate with the heavy-removal tower via a first discharge pipe, and a second discharge pipe is provided on the top portion of the light-removal tower; wherein the first feed pipe is configured to supply the first feed oil in the mixing tank to flow into the light-removal tower; the second discharge pipe is configured to supply the fraction with a carbon number not greater than 9 in the first feed oil to flow out; and the first discharge pipe is configured to supply the fraction with a carbon number greater than 9 in the first feed oil to flow from the bottom portion of the light-removal tower into the heavy-removal tower;

[0008] a heavy removal tower, the heavy removal tower being connected to the light removal tower, the heavy removal tower being configured to remove a fraction having a carbon number of not less than 16 from the second feed oil to obtain a third feed oil;

[0009] a rotary valve, the rotary valve being connected to the deweighting column, and the rotary valve being configured to remove normal fractions from the third feed oil to obtain a fourth feed oil;

[0010] A distillation tower is connected to the rotary valve, and the distillation tower is configured to distill the fourth raw oil to obtain an isododecane product.

[0011] In one embodiment of the present disclosure, the lightness removal tower is provided with a heating pipeline, and the heating temperature of the heating pipeline is 205-225°C.

[0012] In one embodiment of the present disclosure, an air cooler is provided in the first discharge pipe, and the fraction with a carbon number greater than 9 in the first feed oil in the first discharge pipe is configured to be sent to the deweighting tower after being cooled by the air cooler.

[0013] In one embodiment of the present disclosure, the upper and middle parts of the deweighting tower are constructed to be connected to the rotary valve through a third discharge pipe; the temperature of the deweighting tower is 130-160°C, and the fraction with a carbon number of not less than 16 in the second raw oil is output from a fourth discharge pipe arranged at the bottom of the deweighting tower, and the fraction with a carbon number of 10-15 in the second raw oil enters the rotary valve from the third discharge pipe in the upper and middle part of the deweighting tower.

[0014] In one embodiment of the present disclosure, a reflux pipe is provided at the top of the deweighting tower, and the position of the third discharge pipe on the deweighting tower is lower than the position of the reflux pipe on the deweighting tower; the fluid at the top of the deweighting tower is configured to flow into the deweighting tower through the reflux pipe.

[0015] In one embodiment of the present disclosure, the apparatus for producing isododecane further comprises:

[0016] A hydrogenation reactor is provided between the de-weighting tower and the rotary valve; the bottom of the hydrogenation reactor is constructed to be connected to the de-weighting tower through a third discharge pipe, the temperature of the hydrogenation reactor is 195-225°C, and the third feed oil enters the bottom of the hydrogenation reactor through the third discharge pipe; the hydrogenation reactor is provided with a hydrogen inlet pipe, and hydrogen is configured to enter the hydrogenation reactor through the hydrogen inlet pipe to undergo a dearomatization reaction with the third feed oil.

[0017] In one embodiment of the present disclosure, a deacidification tank is further provided between the hydrogenation reactor and the rotary valve, a molecular sieve is provided in the deacidification tank, and the material output from the hydrogenation reactor is configured to be sent into the deacidification tank and deacidified by the molecular sieve.

[0018] In one embodiment of the present disclosure, the molecular sieve is a 13X molecular sieve.

[0019] In one embodiment of the present disclosure, the temperature of the distillation tower is 248-268°C, and the upper and middle parts of the distillation tower are configured to be connected to the stripping tower through a fifth discharge pipe; the isododecane product is configured to enter the stripping tower through the fifth discharge pipe for separation; and the fluid at the top of the stripping tower is constructed to reflux into the distillation tower through a sixth discharge pipe.

[0020] In one embodiment of the present disclosure, the fifth discharge pipe is connected to a position on the distillation tower at a temperature range of 210-220°C; the sixth discharge pipe is connected to a position on the distillation tower at a temperature range of 205-215°C.

[0021] The device for producing isododecane provided by the present disclosure simplifies the process, saves production costs and reduces energy consumption.

[0022] Other features and advantages of the present disclosure will become apparent from the following detailed description of exemplary embodiments of the present disclosure with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 1 is a schematic structural diagram of an apparatus for producing isododecane provided in one embodiment of the present disclosure;

[0024] Figure 2 is a schematic structural diagram of an apparatus for producing isododecane provided in another embodiment of the present disclosure;

[0025] Figure 3 It is a schematic structural diagram of an apparatus for producing isododecane provided in another embodiment of the present disclosure.

[0026] 1-Mixing tank; 2-Light-removal tower; 3-Heavy-removal tower; 4-Rotary valve; 5-Distillation tower; 6-First feed pipe; 7-First discharge pipe; 8-Second discharge pipe; 9-Stripping tower; 10-Third discharge pipe; 11-Reflux pipe; 12-Hydrogenation reactor; 13-Hydrogen feed pipe; 14-Deacidification tank; 15-Fourth discharge pipe; 16-Fifth discharge pipe; 17-Sixth discharge pipe. DETAILED DESCRIPTION

[0027] Various exemplary embodiments of the present disclosure will now be described in detail with reference to the accompanying drawings. It should be noted that unless otherwise specifically stated, the relative arrangement of components and steps, numerical expressions and numerical values ​​set forth in these embodiments do not limit the scope of the present disclosure.

[0028] The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the present disclosure, its application, or uses.

[0029] Technologies, methods, and equipment known to ordinary technicians in the relevant art may not be discussed in detail, but where appropriate, the technologies, methods, and equipment should be considered part of the specification.

[0030] It should be noted that like reference numerals and letters refer to like items in the following figures, and therefore, once an item is defined in one figure, it need not be further discussed in subsequent figures.

[0031] The specific embodiments of the present disclosure are described below with reference to the accompanying drawings.

[0032] In this document, “upper”, “lower”, “front”, “back”, “left”, “right”, etc. are only used to indicate the relative position relationship between related parts, rather than to limit the absolute positions of these related parts.

[0033] In this article, "first", "second", etc. are only used to distinguish each other, and do not indicate the importance and order, or the prerequisite for each other's existence.

[0034] In this document, “equal”, “same”, etc. are not strictly limited in a mathematical and / or geometric sense, but also include errors that can be understood by those skilled in the art and are allowed in manufacturing or use.

[0035] The present disclosure provides an apparatus for producing isododecane, comprising a mixing tank, a light-removing tower, a heavy-removing tower, a rotary valve, and a distillation tower, wherein the mixing tank is configured to mix Fischer-Tropsch refined conventional first-line oil and Fischer-Tropsch cracked conventional first-line oil, and the Fischer-Tropsch refined conventional first-line oil and the Fischer-Tropsch cracked conventional first-line oil are mixed to form a first raw material oil; the middle portion of the light-removing tower is configured to be connected to the mixing tank through a first feed pipe; the bottom portion of the light-removing tower is configured to be connected to the heavy-removing tower through a first discharge pipe, and a second discharge pipe is provided on the top of the light-removing tower; wherein the first feed pipe is configured to supply the first raw material oil in the mixing tank to flow into the light-removing tower ; The second discharge pipe is configured to allow the fraction with a carbon number not greater than 9 in the first raw oil to flow out; the first discharge pipe is configured to allow the fraction with a carbon number greater than 9 in the first raw oil to flow from the bottom of the light removal tower into the heavy removal tower; the heavy removal tower is connected to the light removal tower, and the heavy removal tower is configured to remove the fraction with a carbon number not less than 16 in the second raw oil to obtain a third raw oil; the rotary valve is connected to the heavy removal tower, and the rotary valve is configured to remove the normal fraction in the third raw oil to obtain a fourth raw oil; the distillation tower is connected to the rotary valve, and the distillation tower is configured to distill the fourth raw oil to obtain an isododecane product.

[0036] The isododecane production device provided by the present disclosure can shorten the isododecane processing flow, save production costs and reduce energy consumption.

[0037] For ease of understanding, refer to Figures 1 to 3, the specific structure and working principle of the device for producing isododecane disclosed in the present invention are explained in detail with reference to an embodiment.

[0038] like Figure 1 As shown, the present disclosure provides a device for producing isododecane, comprising a mixing tank 1, a light-removing tower 2, a heavy-removing tower 3, a rotary valve 4 and a distillation tower 5, and the mixing tank 1, the light-removing tower 2, the heavy-removing tower 3, the rotary valve 4 and the distillation tower 5 are connected in sequence. Among them, the mixing tank 1 is configured to mix Fischer-Tropsch refined regular first-line oil and Fischer-Tropsch cracked regular first-line oil, and the Fischer-Tropsch refined regular first-line oil and the Fischer-Tropsch cracked regular first-line oil are mixed to form a first raw material oil. In order to ensure that the isomeric components can meet the load of the device and ensure the smooth progress of the subsequent production process, it is necessary to mix the Fischer-Tropsch refined regular first-line oil and the Fischer-Tropsch cracked regular first-line oil, so a mixing tank 1 is provided, and the Fischer-Tropsch refined regular first-line oil and the Fischer-Tropsch cracked regular first-line oil are mixed in the mixing tank 1 according to (60±5)%: (40±5)% to obtain the first raw material oil.

[0039] Since the first raw oil contains mixed components of various carbon numbers, the first raw oil needs to be treated with light removal, heavy removal and acid removal. First, the first raw oil needs to be treated with light removal.

[0040] like Figures 2 to 3 As shown, the lightness removal tower 2 is connected to the mixing tank 1, and the lightness removal tower 2 is configured to remove the fraction with a carbon number not greater than 9 in the first raw oil to obtain the second raw oil. Specifically, the lightness removal tower 2 is provided with a first feed pipe 6, a first discharge pipe 7 and a second discharge pipe 8. The middle part of the lightness removal tower 2 is configured to be connected to the mixing tank 1 through the first feed pipe 6, and the first raw oil in the mixing tank 1 flows into the lightness removal tower 2 through the first feed pipe 6. The bottom of the lightness removal tower 2 is configured to be connected to the de-weight removal tower 3 through the first discharge pipe 7. The second discharge pipe 8 is provided at the top of the lightness removal tower 2, and the second discharge pipe 8 is configured to supply the fraction with a carbon number not greater than 9 in the first raw oil to flow out; the first discharge pipe 7 is configured to supply the fraction with a carbon number greater than 9 in the first raw oil to flow from the bottom of the lightness removal tower 2 into the de-weight removal tower 3. A heating pipeline is provided in the light-removing tower 2, and the heating temperature of the heating pipeline is 205-225°C. In this embodiment, 211°C is preferably used as the heating temperature of the heating pipeline, and the pressure of the light-removing tower 2 is 25-35kPa. Under this temperature and pressure, the light component will be output from the top of the light-removing tower 2, that is, the fraction with a carbon number not greater than 9 in the first raw oil is output from the second discharge pipe 8 provided at the top of the light-removing tower 2, and the heavy component will enter the heavy-removing tower 3 from the bottom of the light-removing tower 2, that is, the fraction with a carbon number greater than 9 in the first raw oil enters the heavy-removing tower 3 from the first discharge pipe 7 at the bottom of the light-removing tower 2.

[0041] After the light oil removal treatment, the first raw oil also needs to be subjected to heavy oil removal treatment to remove the heavier components in the first raw oil.

[0042] like Figures 2 to 3 As shown, the de-weighting tower 3 in this embodiment is connected to the de-lightening tower 2, and the de-weighting tower 3 is configured to remove the fraction with a carbon number of not less than 16 in the second raw oil to obtain the third raw oil. Specifically, the middle and upper part of the de-weighting tower 3 is constructed to be connected to the rotary valve 4 through the third discharge pipe 10. In order to achieve a better de-weighting effect, it is also necessary to reasonably set the temperature and pressure of the de-weighting tower 3. In this embodiment, the temperature of the de-weighting tower 3 is 130-160°C and the pressure is 6-16kPa. In this embodiment, 11kPa is preferably used as the pressure of the de-weighting tower 3. Under this temperature and pressure, the fraction with a carbon number of not less than 16 in the second raw oil is output from the fourth discharge pipe 15 set at the bottom of the de-weighting tower 3, and the fraction with a carbon number of 10-15 in the second raw oil enters the rotary valve 4 from the third discharge pipe 10 in the middle and upper part of the de-weighting tower 3.

[0043] After the light and heavy fraction removal treatments, the third raw oil only contains fractions with a carbon number of 10-15, and the third raw oil then needs to be denormalized.

[0044] like Figures 2 to 3 As shown, in this embodiment, rotary valve 4 is connected to deweighting column 3 and is configured to remove normal fractions from the third feedstock to produce a fourth feedstock. Specifically, a desorbent is disposed within rotary valve 4 to remove the normal fractions from the third feedstock to produce the fourth feedstock.

[0045] In order to obtain high-purity isododecane products, the fourth raw oil needs to be distilled. Figures 2 to 3 As shown, the distillation tower 5 in this embodiment is connected to the rotary valve 4, and the distillation tower 5 is configured to be used for distilling the fourth raw oil to obtain an isododecane product.

[0046] Considering that in the production process of isododecane, temperature is a very important parameter affecting the reaction process. Too high or too low temperature will affect the progress of the reaction, resulting in the final isododecane product being impure.

[0047] like Figures 2 to 3 As shown, in one embodiment of the present disclosure, an air cooler is provided in the first discharge pipe 7, and the fraction with a carbon number greater than 9 in the first feed oil in the first discharge pipe 7 is configured to be sent to the de-weighting tower 3 after being cooled by the air cooler. Specifically, the components with a carbon number of 10 or above after the light removal treatment are cooled by the air cooler at the bottom of the light removal tower 2 before entering the de-weighting tower 3. Since the maximum temperature of the de-weighting tower 3 is 160°C in this embodiment, it is necessary to cool the components after the light removal treatment to 160°C through the air cooler so as not to affect the de-weighting process.

[0048] like Figures 2 to 3As shown, in one embodiment of the present disclosure, a reflux pipe 11 is provided at the top of the deweighting tower 3, and the position of the third discharge pipe 10 on the deweighting tower 3 is lower than the position of the reflux pipe 11 on the deweighting tower 3; the fluid at the top of the deweighting tower 3 is configured to flow into the deweighting tower 3 through the reflux pipe 11. Specifically, during the deweighting process, a small amount of heavier components may also be discharged from the top. In order to avoid waste of resources, a reflux pipe 11 is further provided on the deweighting tower 3. The reflux pipe 11 is used to reflux the fluid at the top of the deweighting tower 3. Since the third discharge pipe 10 mainly outputs a fraction with a carbon number of 10-15, and the reflux pipe 11 at the top of the deweighting tower 3 is mainly used to output a fraction with a carbon number less than 10, the position of the third discharge pipe 10 on the deweighting tower 3 is set to be lower than the position of the reflux pipe 11 on the deweighting tower 3.

[0049] Considering that the fraction after the dehydrogenation treatment still has a high aromatic content, it is necessary to perform dearomatization on the components after the dehydrogenation treatment.

[0050] like Figures 2 to 3 As shown, in one embodiment of the present disclosure, the device for producing isododecane also includes a hydrogenation reactor 12, which is arranged between the deweighting tower 3 and the rotary valve 4; the bottom of the hydrogenation reactor 12 is constructed to be connected to the deweighting tower 3 through a third discharge pipe 10, the temperature of the hydrogenation reactor 12 is 195-225°C, and the third raw oil enters the bottom of the hydrogenation reactor 12 through the third discharge pipe 10; a hydrogen inlet pipe 13 is provided on the hydrogenation reactor 12, and hydrogen is configured to enter the hydrogenation reactor 12 through the hydrogen inlet pipe 13 to undergo a dearomatization reaction with the third raw oil.

[0051] Specifically, the third feedstock, after being deweighted, enters the bottom of the hydrogenation reactor 12 from the deweighting tower 3 through the third discharge pipe 10. The temperature of the hydrogenation reactor 12 is 195-225°C. At this temperature, the third feedstock undergoes a dearomatization reaction with hydrogen, resulting in the final isododecane product being free of aromatics. In addition, the provision of the hydrogen inlet pipe 13 on the hydrogenation reactor 12 ensures a sufficient source of hydrogen in the hydrogenation reactor 12, ensuring the smooth progress of the dearomatization reaction.

[0052] like Figures 2 to 3 As shown, in one embodiment of the present disclosure, a deacidification tank 14 is further provided between the hydrogenation reactor 12 and the rotary valve 4, and a molecular sieve is provided in the deacidification tank 14. The material output from the hydrogenation reactor 12 is configured to be sent to the deacidification tank 14 and deacidified by the molecular sieve. In this embodiment, the molecular sieve is a 13X type molecular sieve. Specifically, in this embodiment, the oxygen-containing compounds in the intermediate product can be adsorbed and separated by the 13X molecular sieve. The 13X molecular sieve has excellent adsorption performance for oxygen-containing compounds and polar substances, and has low cost, mild operating conditions, and is easy to remove and recycle.

[0053] In one embodiment of the present disclosure, the temperature of the distillation tower 5 is 248-268°C. The upper and middle portions of the distillation tower 5 are connected to the stripping tower 9 via a fifth discharge pipe 16. The isododecane product is configured to enter the stripping tower 9 through the fifth discharge pipe 16 for separation. The fluid at the top of the stripping tower 9 is configured to flow back into the distillation tower 5 via a sixth discharge pipe 17. The fifth discharge pipe 16 is connected to the distillation tower 5 at a location within the temperature range of 210-220°C. The sixth discharge pipe 17 is connected to the distillation tower 5 at a location within the temperature range of 205-215°C.

[0054] Specifically, the IC after being processed by the rotary valve 4 10 -IC 15 The fraction enters distillation tower 5. In this embodiment, the temperature at the bottom of distillation tower 5 is 248-268°C, preferably 262.8°C. The pressure at the top of distillation tower 5 is controlled at 75-85 kPa, preferably 80 kPa. A fifth discharge pipe 16 is connected to distillation tower 5 at a temperature range of 210-220°C. The isododecane product flows from distillation tower 5 through fifth discharge pipe 16 to stripping tower 9 for separation, yielding high-quality, pure isododecane product. Considering that some isododecane product may be distilled to the top of stripping tower 9 during the distillation process, resulting in resource waste, a sixth discharge pipe 17 is provided at the top of stripping tower 9. This sixth discharge pipe 17 is connected to a temperature range of 205-215°C on distillation tower 5. Fluid from the top of stripping tower 9 flows back into distillation tower 5 through sixth discharge pipe 17.

[0055] The apparatus for producing isododecane provided herein simplifies the process, reduces production costs, and lowers energy consumption. The use of a mixing tank also avoids the problem of insufficient normal isomerization loading in subsequent adsorption separation equipment. Furthermore, the use of 13X molecular sieve effectively removes impurities such as oxygenates from isododecane, resulting in a high-quality, high-purity isododecane product.

[0056] It should be noted that for the aforementioned method embodiments, for ease of description, they are all expressed as a series of action combinations, but those skilled in the art should be aware that the present disclosure is not limited by the order of the actions described, because according to the present disclosure, certain steps can be performed in other orders or simultaneously. Secondly, those skilled in the art should also be aware that the embodiments described in the specification are all preferred embodiments, and the actions and modules involved are not necessarily required by the present disclosure.

[0057] In the above embodiments, the description of each embodiment has its own focus. For parts that are not described in detail in a certain embodiment, reference can be made to the relevant descriptions of other embodiments.

[0058] The preferred embodiments of the present disclosure disclosed above are intended only to help illustrate the present disclosure. The optional embodiments do not describe all details in detail, nor do they limit the invention to the specific embodiments described. Obviously, many modifications and variations can be made based on the content of the present disclosure. The present disclosure selects and specifically describes these embodiments in order to better explain the principles and practical applications of the present disclosure, so that those skilled in the art can better understand and utilize the present disclosure. The present disclosure is limited only by the claims and their full scope and equivalents.

Claims

1. A device for producing isododecane, characterized in that: include: A mixing tank (1), wherein the mixing tank (1) is configured to mix Fischer-Tropsch refined conventional first-line oil and Fischer-Tropsch cracked conventional first-line oil, wherein the Fischer-Tropsch refined conventional first-line oil and the Fischer-Tropsch cracked conventional first-line oil are mixed to form a first feedstock oil; A lightness removal tower (2), wherein the middle portion of the lightness removal tower (2) is configured to be in communication with a mixing tank (1) via a first feed pipe (6); the bottom portion of the lightness removal tower (2) is configured to be in communication with a weight removal tower (3) via a first discharge pipe (7); a second discharge pipe (8) is provided at the top of the lightness removal tower (2); wherein the first feed pipe (6) is configured to allow the first crude oil in the mixing tank (1) to flow into the lightness removal tower (2); the second discharge pipe (8) is configured to allow the fraction with a carbon number not greater than 9 in the first crude oil to flow out; and the first discharge pipe (7) is configured to allow the fraction with a carbon number greater than 9 in the first crude oil to flow from the bottom portion of the lightness removal tower (2) into the weight removal tower (3); a de-weighting tower (3), the de-weighting tower (3) being connected to the de-lighting tower (2), the de-weighting tower (3) being configured to remove a fraction having a carbon number of not less than 16 from the second raw oil to obtain a third raw oil; a rotary valve (4), the rotary valve (4) being connected to the deweighting tower (3), the rotary valve (4) being configured to remove the normal fraction from the third raw oil to obtain a fourth raw oil; A distillation tower (5), the distillation tower (5) is connected to the rotary valve (4), and the distillation tower (5) is configured to distill the fourth raw material oil to obtain an isododecane product.

2. The device for producing isododecane according to claim 1, characterized in that The lightness removal tower (2) is provided with a heating pipeline, and the heating temperature of the heating pipeline is 205-225°C.

3. The device for producing isododecane according to claim 2, characterized in that An air cooler is provided in the first discharge pipe (7), and the fraction with a carbon number greater than 9 in the first feed oil in the first discharge pipe (7) is configured to be sent to the deweighting tower (3) after being cooled by the air cooler.

4. The device for producing isododecane according to claim 1, characterized in that The middle and upper part of the de-weighting tower (3) is constructed to be connected to the rotary valve (4) through a third discharge pipe (10); the temperature of the de-weighting tower (3) is 130-160°C, the fraction with a carbon number of not less than 16 in the second raw oil is discharged from a fourth discharge pipe (15) arranged at the bottom of the de-weighting tower (3), and the fraction with a carbon number of 10-15 in the second raw oil enters the rotary valve (4) from the third discharge pipe (10) in the middle and upper part of the de-weighting tower (3).

5. The device for producing isododecane according to claim 4, characterized in that A reflux pipe (11) is provided at the top of the deweighting tower (3); the position of the third discharge pipe (10) on the deweighting tower (3) is lower than the position of the reflux pipe (11) on the deweighting tower (3); and the fluid at the top of the deweighting tower (3) is configured to flow into the deweighting tower (3) through the reflux pipe (11).

6. The device for producing isododecane according to claim 1, characterized in that: Also includes: A hydrogenation reactor (12), the hydrogenation reactor (12) being arranged between the de-weighting tower (3) and the rotary valve (4); the bottom of the hydrogenation reactor (12) being configured to be connected to the de-weighting tower (3) via a third discharge pipe (10); the temperature of the hydrogenation reactor (12) being 195-225° C., the third raw oil entering the bottom of the hydrogenation reactor (12) via the third discharge pipe (10); the hydrogenation reactor (12) being provided with a hydrogenation pipe (13), the hydrogen being configured to enter the hydrogenation reactor (12) via the hydrogenation pipe (13) to carry out a dearomatization reaction with the third raw oil.

7. The device for producing isododecane according to claim 6, characterized in that A deacidification tank (14) is also provided between the hydrogenation reactor (12) and the rotary valve (4), and a molecular sieve is provided in the deacidification tank (14). The material output from the hydrogenation reactor (12) is configured to be sent into the deacidification tank (14) and deacidified by the molecular sieve.

8. The device for producing isododecane according to claim 7, characterized in that: The molecular sieve is 13X molecular sieve.

9. The device for producing isododecane according to claim 1, characterized in that: The temperature of the distillation tower (5) is 248-268°C. The middle and upper parts of the distillation tower (5) are configured to be connected to the stripping tower (9) through a fifth discharge pipe (16); the isododecane product is configured to enter the stripping tower (9) through the fifth discharge pipe (16) for separation; and the fluid at the top of the stripping tower (9) is configured to flow back into the distillation tower (5) through a sixth discharge pipe (17).

10. The device for producing isododecane according to claim 9, characterized in that: The fifth discharge pipe (16) is connected to a position on the distillation tower (5) at a temperature range of 210-220° C.; the sixth discharge pipe (17) is connected to a position on the distillation tower (5) at a temperature range of 205-215° C.

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