RU1587911C - Method for processing bottom petroleum products - Google Patents

Abstract

FIELD: petrochemistry, in particular, thermal treatment of bottom products. SUBSTANCE: this method prescribes viscosity breaking bottom products in presence of 0.001 to 0.05 percent by mass polar additive to be introduced portionwise, first, at temperature of phase transition of bottom petroleum product from structurized to molecular state, then at asphaltene destruction initiation temperature and finally at asphaltene nuclear disintegration initiation temperature. Disclosed method prescribes using acetone as most preferable additive. Prescribed conditions reduce viscosity breaking bottom product viscosity from 16.4 to 11.3 degrees of specific viscosity, enhance stability up to 2.5 poinst against 2.1 and minimize environmental contamination due to reduction in amount of contaminating discharges with excluding water condensate. EFFECT: lower viscosity and higher stability of liquid products. 2 cl, 2 dwg, 2 tbl

Description

 The invention relates to methods for thermal processing of residual oil products and can be used in the oil refining industry.

 The aim of the invention is to reduce the viscosity and increase the stability of visbreaking products, as well as reducing environmental pollution by reducing the amount of harmful emissions by eliminating water condensate.

 1 and 2 illustrate the proposed method.

 Acetone is best used as a polar compound, since it is the cheapest polar compound, in addition, for other types of polar compounds, no sufficiently narrow quantitative range is found in which they are used, but their use is also possible.

 The essence of the method is as follows.

Raw materials — residual oil products (fuel oil, tars, asphalts, etc.) are heated to a temperature corresponding to the phase transition of the raw material from a structured state to a molecular state, determined graphically (see Fig. 1), and mixed with the first portion of acetone. Next, the residual oil is heated to the temperature of the beginning of the destruction of asphaltenes, determined graphically (see figure 2), and mixed with a second portion of acetone. Then the residual oil is heated to a temperature beginning decay polycondensed asphaltene nuclei (> 380 ^C) and mixed with a third portion of acetone. Next crack in the reaction apparatus.

 The chemistry of acetone is as follows.

 Acetone reduces the reactivity of asphaltenes during association, polymerization, polycondensation due to the compensation of active paramagnetic centers responsible for the course of these reactions due to the interaction of these centers with the CO group, which is part of acetone.

 As a result of acetone supply at characteristic stages of the change in the properties of residual oil products during their heating, asphaltenes are maintained in a finely dispersed state, which prevents the structuring of residual oil products and, as a result, contributes to a more effective decrease in viscosity and an increase in the stability of visbreaking residues.

The first portion of acetone is supplied at the phase transition temperature of the residual oil products from the structured to the molecular state. The temperature of the phase transition is determined by the change in the angle of inclination of the graphs (see figure 1) in the coordinates
(1 / t, 1n ν), where t is the temperature, ^о С;
ν is the kinematic viscosity of the residual oil product, ost.

 The second portion of acetone is supplied at the initial temperature of the destruction of asphaltenes (see Fig. 2), which is determined by the data of derivatographic analysis of the thermal destruction of residual oil products.

A third portion of acetone is fed at a temperature of beginning degradation polycondensed asphaltene nuclei (> 380 ^C).

 The method is illustrated by the following examples.

PRI me R 1. Tar containing 3 wt.% Fractions, boiling up to 500 ^about With 10 wt. % Asphaltenes coking 17.1 wt.%, A specific weight of 995.8 kg / m ^3, viscosity 430 conditional ^{on the} slave at ⁸⁰ ° C, is subjected to visbreaking at t = ⁴⁵⁰ ° C and P = 0.6 MPa.

From the reaction products emit gas, gasoline fraction and a residue above 180 ^about C.

Conditional viscosity fr. > ¹⁸⁰ ° C was 43.3 BV at 80 ° ^C, the stability of 1.65.

PRI me R 2. The same tar as in example 1, mixed with 0.006 wt.% Acetone at 150 ^about C and subjected to visbreaking under the conditions of example 1.

Isolated from reaction products fr. > ¹⁸⁰ ° C has a viscosity of 16.4 ^on conventional slave at 80 ° ^C, the stability of 2.10.

PRI me R 3. The tar is the same as in example 1, mixed with 0.006 wt.% Acetone at 280 ^about C and subjected to visbreaking in the conditions of example 1.

Isolated from reaction products fr. > ¹⁸⁰ ° C has a viscosity of 18.5 ^on conventional slave at 80 ° ^C, the stability of 1.98.

PRI me R 4. The tar is the same as in example 1, mixed with 0.006 wt.% Acetone at 385 ^about C and subjected to visbreaking in the conditions of example 1.

Isolated from reaction products fr. > ¹⁸⁰ ° C has a viscosity of 22.1 ^on conventional slave at 80 ° ^C, the stability of 1.95.

PRI me R 5. The same tar as in example 1, mixed with 0.006 wt.% Acetone supplied in equal portions at 150, 280 and 385 ^about C, and subjected to visbreaking in the conditions of example 1.

Isolated from reaction products fr. > ¹⁸⁰ ° C has a viscosity of 11.3 ^on conventional slave at 80 ° ^C, the stability of 2.50.

PRI me R 6. The same tar as in example 1, mixed with 0.001 wt.% Acetone supplied in equal portions at 150, 280 and 385 ^about C, and subjected to visbreaking in the conditions of example 1.

Isolated from products of visbreaking fr. > ¹⁸⁰ ° C has a viscosity of 30.0 ^on conventional slave at 80 ° ^C, the stability of 1.88.

PRI me R 7. The same tar as in example 1, mixed with 0.05 wt.% Acetone supplied in equal portions at 150, 280 and 385 ^about C, and subjected to visbreaking in the conditions of example 1.

Isolated from products of visbreaking fr. > ¹⁸⁰ ° C has a viscosity of 15.9 ^on conventional slave at 80 ° ^C, the stability of 2.7.

 PRI me R 8. The same tar as in example 1, mixed with 0.003 wt.% Polymethylsiloxane and subjected to visbreaking in the conditions of example 1.

Isolated from products of visbreaking fr. > ¹⁸⁰ ° C has a viscosity of 35.6 ^on conventional slave at 80 ° ^C, the stability of 1.73.

 PRI me R 9. The tar is the same as in example 1, mixed with 0.007 wt.% Polymethylsiloxane and subjected to visbreaking in the conditions of example 1.

Isolated from products of visbreaking fr. > ¹⁸⁰ ° C has a viscosity of 31.4 ^on conventional slave at 80 ° ^C, the stability of 1.80.

 PRI me R 10. The tar is the same as in example 1, mixed with 0.01 wt.% Polymethylsiloxane and subjected to visbreaking in the conditions of example 1.

Isolated from products of visbreaking fr. > ¹⁸⁰ ° C has a viscosity of 32.5 ^on conventional slave at 80 ° ^C, the stability of 1.85.

The amount of acetone supplied to the process during the processing of a particular raw material is determined experimentally and varies symbatically with the content of asphaltenes in the residual oil products. An increase of more than 0.05 wt.% The amount of acetone supplied to the process is irrational, since it is not completely spent on the reaction, which is confirmed by the presence of it in light visbreaking products. In addition, an increase in the amount of acetone supplied to the process increases the viscosity of fr. > 180 ^about S.

 The addition of acetone of less than 0.001 wt.% Is not effective, since it does not give the desired result.

 The experimental results are shown in table 1.

As can be seen from table 1, due to the portioned injection of acetone, the conditional viscosity of the visbreaking residue decreases from 16.4 (example 2) to 11.3 ^about WU (example 5) and stability increases from 2.1 to 2.5. Comparison with the prototype (examples 8-10) shows that the introduction of 0.006 wt.% Acetone (example 5) is three times more effective.

 The use of other polar compounds is illustrated in Table 2.

Claims (2)

 1. METHOD FOR PROCESSING RESIDUAL OIL PRODUCTS by visbreaking in the presence of 0.001 - 0.05 wt. % additives, characterized in that, in order to reduce the viscosity and increase the stability of the liquid products of the process and reduce environmental pollution, the polar compound introduced in portions is used as an additive: at the temperature of the phase transition of the residual oil product from the structured to the molecular state, at the temperature at which the destruction begins asphaltenes and at the temperature of the onset of decay of asphaltene nuclei.  2. The method according to claim 1, characterized in that acetone is used as the polar compound.

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