KR102616393B1 - A Pressure-refined Oil Manufacturing Method - Google Patents

Abstract

The present invention relates to a method for producing vacuum refined oil, which consists of a first step of distilling C1 to C4 hydrocarbons from naphtha, and a second step of distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the hydrocarbons remaining in the first step. A third step of distilling C6 to C8 hydrocarbons from the hydrocarbons remaining in the first step, a fourth step of distilling C10 to C12 hydrocarbons from the remaining hydrocarbons of the third step, and the second step A fifth step of mixing the waste oil of the remaining hydrocarbons with the by-product oil of the hydrocarbons of the fourth step, a sixth step of filtering the mixture of the fifth step, and a seventh step of distilling and separating the mixture of the sixth step. It is characterized by including.

Description

A Pressure-refined Oil Manufacturing Method}

The present invention relates to a method for producing vacuum refined oil, and more specifically, to a method for producing vacuum refined oil for producing vacuum refined oil with low kinematic viscosity and high calorific value.

Reduced pressure refined oil is an environmentally friendly product with no odor and uniform quality made by distilling waste oil under high vacuum. It is a clean fuel oil that can replace indoor kerosene and diesel oil.

Distillation technology is a technology that uses the difference in boiling points of components in waste oil to separate it into light oil, heavy oil, asphalt oil, and solids. In contrast, vacuum distillation is a technology that separates waste oil in a vacuum to prevent thermal decomposition. It is operated at low temperature, so unlike high-temperature thermal decomposition technology, there are no problems such as tar formation or odor due to decomposition of waste oil, and the viscosity of the resulting oil is reduced. Although it is relatively high, it is a technology that can produce relatively high quality fuel oil.

However, the prior art had the following problems.

There was a problem of increased storage and distribution costs due to the high kinematic viscosity.

In addition, there was a problem in that the amount of air pollutants increased due to the high content of sulfur and nitrogen.

Registered Patent No. 10-0521407

In order to solve the above-mentioned problems, the purpose of the present invention is to provide vacuum refined oil with low kinematic viscosity and low generation of air pollutants such as sulfur oxides and nitrogen oxides.

In order to achieve the above-described object, the present invention's method for producing vacuum refined oil includes a first step of distilling C1 to C4 hydrocarbons from naphtha, and distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons in the first step. A second step of distilling C6 to C8 hydrocarbons from the hydrocarbons remaining in the first step, a fourth step of distilling C10 to C12 hydrocarbons from the remaining hydrocarbons of the third step, and A fifth step of mixing the waste oil of the remaining hydrocarbons of the second step with the by-product oil of the hydrocarbons of the fourth step, a sixth step of filtering the mixture of the fifth step, and distillation and separation of the mixture of the sixth step. It is characterized by including a 7th step.

In the fifth step, the hydrocarbon of the fourth step is mixed at a ratio of 40 to 65 vol% with respect to the remaining hydrocarbon of the second step of 35 to 60 vol%.

In the seventh step, the mixture is distilled at 200°C and a pressure of 30 Torr.

The method for producing vacuum refined oil according to the present invention has the following effects.

In the process of distillation and separation from naphtha, waste oil and by-product oil are mixed at a certain ratio, so the kinematic viscosity is low and the amount of nitrogen and sulfur oxides generated is low, making it easy to store and distribute, and has the advantage of being environmentally friendly.

Figure 1 is a flow chart showing the manufacturing process of vacuum refined oil according to the present invention.
Figure 2 is a flow chart showing the process of mixing and refining waste oil and by-product oil during the manufacturing process of reduced pressure refined oil according to the present invention.
Figure 3 is a diagram showing the physical properties of pressure refined oil produced by the manufacturing process of vacuum refined oil according to the present invention.

Hereinafter, a preferred embodiment of the method for producing vacuum refined oil according to the present invention will be described in detail with reference to the attached drawings.

As shown in FIG. 1, the vacuum refined oil production method according to the present invention includes the first step (S10) of distilling C1 to C4 hydrocarbons from naphtha, and C5 hydrocarbons and A second step (S20) of distilling C8 to C10 hydrocarbons, a third step (S30) of distilling C6 to C8 hydrocarbons from the hydrocarbons remaining in the first step (S10), and the third step (S30) A fourth step (S40) of distilling C10 to C12 hydrocarbons among the remaining hydrocarbons, and a fifth step of mixing waste oil from the remaining hydrocarbons of the second step (S20) and by-product oil of the hydrocarbons of the fourth step (S40). It includes a step (S50), a sixth step (S60) of filtering the mixture of the fifth step (S50), and a seventh step (S70) of distilling and separating the mixture of the sixth step (S60). You can.

First, in the vacuum refined oil production method according to the present invention, the first step (S10) of separating C1 to C4 hydrocarbons from naphtha in the extract obtained by rectifying crude oil is performed. The process of separating the C1 to C4 hydrocarbons from the naphtha may be carried out through various general processes, including distillation.

The second step (S20) of separating C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons after separating C1 to C4 hydrocarbons from the naphtha is performed. The process of separating C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons in the first step may be performed through various general processes, including distillation.

Meanwhile, the third step (S30) of separating C6 to C8 hydrocarbons from the hydrocarbons remaining in the first step (S10) is performed. In the first step (S10), C6 to C8 hydrocarbons are separated from the remaining hydrocarbons after separating C1 to C4 hydrocarbons. The process of separating C6 hydrocarbons to C8 hydrocarbons can be performed through various general processes, including distillation.

The fourth step (S40) of separating C10 to C12 hydrocarbons from the hydrocarbons remaining in the third step (S30) is performed. In the third step (S30), C10 to C12 hydrocarbons are separated from the remaining hydrocarbons after separating C6 to C8 hydrocarbons. The process of separating C10 hydrocarbons to C12 hydrocarbons may be carried out as a general process including distillation.

Next, the fifth step (S50) is performed in which the waste oil from the remaining hydrocarbons of the second step (S20) and the byproduct oil from the remaining hydrocarbons of the fourth step (S40) are mixed. This is to achieve physical properties comparable to kerosene by using the heavy oil remaining after refining in the second step (S20) and the fourth step (S40).

In order to achieve the above-mentioned purpose, the remaining hydrocarbons of the fourth step (S40) can be mixed in a ratio of 40 to 65 vol% with respect to the remaining hydrocarbons of the second step (S20) of 35 to 65 vol%. . This is to satisfy the range of 0.9 to 4.1 mm2/S, which is the standard for GR viscosity.

When the amount of the remaining hydrocarbons in the fourth step (S40) is mixed in an amount of less than 40% by volume with respect to the remaining hydrocarbons in the second step (S20), the kinematic viscosity is less than 0.8, making it difficult to use as fuel, and if it is more than 65% by volume. This is because when mixed, the kinematic viscosity becomes too high and it cannot be used as fuel.

As a result, it is preferable to mix 50 to 60% by volume of by-product oil, which is the remaining hydrocarbon of the fourth step (S40), with 40 to 50% by volume of waste oil, which is the remaining hydrocarbon of the second step (S20).

The sixth step (S60) of pre-treating the mixture of the fifth step (S50) is performed. The pretreatment is a process of removing foreign substances from the mixture in the fifth step (S50). The pretreatment process may be performed using a strainer. Solid foreign substances contained in the mixture are filtered.

Then, the seventh step (S70) is performed, in which the mixture of the sixth step (S60) is distilled and separated. For distillation in the seventh step (S70), the mixture in the sixth step (S60) can first be preheated. The mixture in the sixth step (S60) is heated to 150°C in the preheating unit, changes phase into vapor and gas, and is transferred to the distillation unit.

The gaseous hydrocarbons of the sixth step (S60) transferred to the distillation unit are distilled at a temperature of 200° C. and a pressure of 200 Torr.

Then, the refined oil distilled in the seventh step (S70) is produced as a reduced-pressure refined oil with a total calorific value of 10,150 Kcal/L, a kinematic viscosity of 1.5 mm2/S, and a flash point of 45°C, as shown in FIG. 3.

Hereinafter, the change in kinematic viscosity according to the mixing ratio of the remaining hydrocarbons of the second step and the remaining hydrocarbons of the fourth step in the vacuum refined oil production process according to the present invention will be explained through experiments.

[Example 1]

After distilling C1 to C4 hydrocarbons from naphtha, 60 liters of hydrocarbons remaining after distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons, and 60 liters of hydrocarbons remaining after distilling C1 to C4 hydrocarbons from naphtha, and C6 to C8 hydrocarbons from the remaining hydrocarbons. Hydrocarbons are distilled, C10 to C12 hydrocarbons are distilled out of the remaining hydrocarbons, and 40 liters of the remaining hydrocarbons are mixed, filtered, preheated to 150°C, and purified by distillation at 200°C at a pressure of 30 Torr.

[Example 2]

After distilling C1 to C4 hydrocarbons from naphtha, 50 liters of hydrocarbons remaining after distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons, and 50 liters of hydrocarbons remaining after distilling C1 to C4 hydrocarbons from naphtha, and C6 to C8 hydrocarbons from the remaining hydrocarbons. Hydrocarbons are distilled, C10 to C12 hydrocarbons are distilled out of the remaining hydrocarbons, and 50 liters of the remaining hydrocarbons are mixed, filtered, preheated to 150°C, and purified by distillation at 200°C at a pressure of 30 Torr.

[Example 3]

After distilling C1 to C4 hydrocarbons from naphtha, 40 liters of hydrocarbons remaining after distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons, and 40 liters of hydrocarbons remaining after distilling C1 to C4 hydrocarbons from naphtha, and C6 to C8 hydrocarbons from the remaining hydrocarbons. Hydrocarbons are distilled, C10 to C12 hydrocarbons are distilled out of the remaining hydrocarbons, and 60 liters of the remaining hydrocarbons are mixed, filtered, preheated to 150°C, and purified by distillation at 200°C at a pressure of 30 Torr.

[Example 4]

After distilling C1 to C4 hydrocarbons from naphtha, 35 liters of hydrocarbons remaining after distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons, and 35 liters of hydrocarbons remaining after distilling C1 to C4 hydrocarbons from naphtha, and C6 to C8 hydrocarbons from the remaining hydrocarbons. Hydrocarbons are distilled, C10 to C12 hydrocarbons are distilled out of the remaining hydrocarbons, and 65 liters of the remaining hydrocarbons are mixed, filtered, preheated to 150°C, and purified by distillation at 200°C at a pressure of 30 Torr.

[Example 5]

After distilling C1 to C4 hydrocarbons from naphtha, 30 liters of hydrocarbons remaining after distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons, and 30 liters of hydrocarbons remaining after distilling C1 to C4 hydrocarbons from naphtha, and C6 to C8 hydrocarbons from the remaining hydrocarbons. Hydrocarbons are distilled, C10 to C12 hydrocarbons are distilled out of the remaining hydrocarbons, and 70 liters of the remaining hydrocarbons are mixed, filtered, preheated to 150°C, and then purified by distillation at 200°C at a pressure of 30 Torr.

Example 1 Example 2 Example 3 Example 4 Example 5 Kinematic viscosity (mm2/S) 0.8 1.2 1.7 3.4 4.3 Kinematic viscosity standard
(GR standard) 0.9 to 4.1 quality △ 0 0 0 ×

As shown in Table 1, Examples 1 to 4 appear to meet the kinematic viscosity standards, and in particular, Examples 2 to 4 show kinematic viscosity in a safe range under the GR standard.

As such, a person skilled in the art will understand that the technical configuration of the present invention described above can be implemented in other specific forms without changing the technical idea or essential features of the present invention.

Therefore, the embodiments described above should be understood in all respects as illustrative and not restrictive, and the scope of the present invention is indicated by the claims described later rather than the detailed description above, and the meaning and scope of the claims and All changes or modified forms derived from the equivalent concept should be construed as falling within the scope of the present invention.

S10: First step of distilling C1 to C4 hydrocarbons from naphtha
S20: Second step of distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the remaining hydrocarbons in the first step.
S30; A third step of distilling C6 to C8 hydrocarbons from the hydrocarbons remaining in the first step.
S40; The fourth step of distilling C10 to C12 hydrocarbons from the remaining hydrocarbons in the third step.
S50; The fifth step of mixing the waste oil from the remaining hydrocarbons of the second step and the by-product oil of the hydrocarbons from the fourth step.
S60; Step 6: Filtering the mixture from Step 5
S70; 7th step of distilling and separating the mixture of 6th step

Claims (3)

A first step of distilling C1 to C4 hydrocarbons from naphtha;
A second step of distilling C5 hydrocarbons and C8 to C10 hydrocarbons from the hydrocarbons remaining in the first step;
A third step of distilling C6 to C8 hydrocarbons from the hydrocarbons remaining in the first step;
A fourth step of distilling C10 to C12 hydrocarbons from the hydrocarbons remaining in the third step;
A fifth step of mixing the waste oil of the hydrocarbons remaining in the second step with the by-product oil of the hydrocarbons in the fourth step;
A sixth step of filtering the mixture of the fifth step;
It includes a seventh step of distilling and separating the mixture of the sixth step,
In the fifth step,
A method for producing vacuum refined oil, characterized in that the hydrocarbon of the fourth step is mixed in a ratio of 50 vol% with respect to the remaining hydrocarbon of the second step. delete According to clause 1,
In the 7th step above,
A method for producing vacuum refined oil, characterized in that the mixture is distilled at 200°C at a pressure of 30 Torr.