RU2510643C2 - Method of bituminous oils processing - Google Patents

Abstract

FIELD: oil and gas industry.

SUBSTANCE: this invention relates to processing of bituminous oils. The invention includes processes of dewatering, skimming of light oil products, deasphaltising. During processing dewatered bituminous oils is separated in process of skimming into light oil products and skimming residue, which is sent to deasphaltising by solution at temperature of 120-130°C, pressure of 4.0-4.5 MPa and volume ratio of solution and raw stock of (1.5-2):1, processes of light oils skimming and deasphaltising of skimming residue are performed so that after mixing of obtained light oil products and asphalt-free oil sulphur content in it does not exceed 1 % by weight, at that the obtained mixture complies with regulatory requirements to low-sulphur liquid fuel.

EFFECT: production of fuel with sulphur content not exceeding 1%.

1 dwg, 5 tbl

Description

The invention relates to the oil industry, in particular to methods for processing high-viscosity bituminous oils.

Bituminous oils according to GOST 51858-2002 include oils with a density of more than 895 kg / m ³ at 20 ° C / 1 /.

Processing of bituminous oils is not effective according to the classical scheme / 2-5 / due to the low content or absence of fractions of gasoline-kerosene-diesel (hereinafter light oil products) and requires other processing approaches.

The closest in technical essence to the proposed and selected by the authors as a prototype is the method "Improving the processing of heavy oil and bitumen" / 6 /. According to the method / 6 / for the processing of heavy oil and bitumen, processes are used: solvent deasphalting, catalytic processes, delayed coking.

The use of catalytic and hydrocatalytic processes for the processing of bituminous oils is difficult due to the high content of resins, heavy condensed aromatic hydrocarbons, and metals. These compounds contribute to the coking of expensive catalysts.

The present invention considers a method for processing bituminous oils, which can be used in places of extraction of bituminous oils or in oil refineries and does not require the use of catalytic processes or complex technologies. According to the proposed method for processing bituminous oils, low-sulfur liquid fuels and asphalt are obtained.

The technical result achieved is achieved by the use of distillation of light petroleum products and deasphalting processes for the dehydration of bituminous oils. As a result, low-sulfur marine fuels or heating oils with a mass fraction of sulfur up to 1% are obtained. Heavy residue - asphalt can be used as fuel for power units.

The values of the selection of light oil products and deasphalting have a wide range. The selection of light petroleum products is 0-5% by weight, the selection of deasphalting is 60-80% by weight, asphalt is the rest. The composition of the obtained low-sulfur liquid fuel,% mass .:

- light oil products 0-6 - deasphalting agent 94-100

The selection of light petroleum products and deasphalting is determined by the sulfur content in the resulting products. The sulfur content in the components and in the mixture of light petroleum products and deasphalting agent should not exceed 1% of the mass.

The present invention is considered on the example of the processing of bituminous oil deposits of the Komi Autonomous Soviet Socialist Republic, Yarega oil.

Physico-chemical properties of Yarega oil / 5 /:

Density, 20 ° С, kg / m ³ 944.9 Viscosity, 40 ° С, mm ² / s 86.3 Pour point, ° C minus 10 Flash point in a closed crucible, ^о С 108 The content of paraffins,% wt. 1.4 The content of sulfuric acid resins,% ≥50 Coking ability,% 8.44 Sulfur content,% 1,11

The output of fractions,% mass .:

up to 200 ° C 0.4 up to 350 ° C 18.8

Dehydrated bituminous oil is sent to a light oil distillation unit or to a deasphalting unit. The scheme provides for the processing of bituminous oil both with distillation of light oil products at the K-1 column (atmospheric distillation), and without separation of light oil products, i.e. Refining of bituminous oil only at the deasphalting unit.

The residue obtained after atmospheric distillation of light oil products or, if the content of light oil products in the initial bituminous oil is 0-5% by mass, then, bypassing the atmospheric distillation unit, bituminous dehydrated oil enters the deasphalting unit.

Atmospheric distillation of light petroleum products is carried out under the conditions of:

- pressure, MPa 0.20-0.25 - oil temperature at the inlet to the column, ° С 170-280 - top temperature, ° С 120-180 - bottom temperature, ° С 300-360 - steam consumption,% of the mass. on raw materials 0.5-1

The deasphalting process is carried out in an environment of liquid butanes (solvent) at the following process parameters.

The technological mode of the deasphalting process:

- volumetric multiplicity solvent: raw materials (1.5-2): 1 - temperature, ° С 120-130 - pressure, MPa 4.0-4.5 - the yield of deasphalting oil,% 60-80

Tables 1-5 show the physicochemical characteristics of the products: light oil products, deasphalting agent, a mixture of light oil products with deasphalting agent, asphalt and atmospheric distillation residue obtained from Yarega oil.

Table 1 Physico-chemical characteristics of light petroleum products obtained from Yarega oil No pp Indicators Actual Values one Density at 15 ° C 0.840-0.850 2 Flash point in a closed crucible, ° С 45-50 3 Pour point, ° C Minus 64 four Cetane index 41 5 The sulfur content,% of the mass. 0.15-0.4

table 2 Requirements for bunkering fuel and the quality of deasphalting from Yarega oil No pp The name of indicators G / F 35 requirements (ISO-F 8217 Directive 1999/32 / EC) Actual quality of deasphalting - bunkering fuel from Yarega oil one Density at 15 ° С, kg / m ³ No more than 991 928 2 Kinematic viscosity, cSt 3 - at 40 ° C - 185.3 four - at 50 ° C 380 103.27 5 - at 100 ° C - 14.2 6 Flash point closed crucible, ° C Not lower than 60 144 7 The total sulfur content,% of the mass. No more than 1,0 0.92 8 Coking ability,% of the mass. No more than 18 3.17 9 The pour point / pour point, ° C Not higher than 27 minus 15 10 Total acid number, mg KOH / g - 0.11 eleven Content, ppm - vanadium No more than 300 9.0 - nitrogen - 1900 - asphaltenes - Ots. - aluminum + silicon No more than 80 55 12 The water content, vol.% No more than 0.5 0.2 13 Ash content,% No more than 0.15 0,037 fourteen Total potential balance,% No more than 0.1 Ots.

Obtained in the process of deasphalting - deasphalting according to its characteristics meets the regulatory requirements for bunker fuel according to the requirements of G / F 35 (ISO-F 8217 Directive 1999/32 / EC) (table 2), a mixture of light petroleum products and deasphalting agent meets the regulatory requirements for fuels for ships IFO TU 0252-014-00044434-2001 and fuel oil M100 GOST 10585-99 (table 3). Resinous residue - asphalt can be used as fuel of the power unit directly at the site of oil refining (table 4). Table 5 presents the quality indicators of the atmospheric residue - the raw material of the deasphalting process.

Table 3 Requirements for marine fuels, heating oil and the quality of a mixture of light petroleum products and deasphalting from Yarega oil No pp Indicators Technical requirements according to TU 0252-014-00044434-2001 Fuel oil M100 (GOST 10585-99) The actual quality of the mixture of light petroleum products (0-6% wt.) And deasphalting agent (94-100% wt.) IFO-30 IFO-180 IFO-380

one Density at 15 ° С, kg / m ³ No more than 960 No more than 991 No more than 991 Not standardized 928-948 2 Fractions yield Up to 200 ° C - - - - 0 Up to 300 ° C - - - - 0 3 Sulfur content. % of the mass. Not more than I - 1.5 II - 3.5 0.5-3.5 0.92-1 four Coking ability,% of the mass. No more than 10 No more than 15 No more than 18 No more than 6 1.7-3.17 5 Flash point in a closed crucible, ^о С Not lower than 60 80-90 80-144 6 Content, ppm: vanadium No more than 150 No more than 200 No more than 300 - 2.5-9.0 7 Ash content,% No more than 0.1 No more than 0.1 No more than 0.15 - 0,037-0,05

Table 4 Physico-chemical characteristics of asphalt obtained from Yarega oil No pp Indicators Actual Values one Softening temperature according to KISH, ° С 35-75 2 The content of asphaltenes,% mass. 7.3-9.8 3 Kinematic viscosity at 250 ° С, cSt 8-22 four Density at 15 ° С, kg / m ³ 1.013-1.043 5 Conradson coke content,% 20,4-25,0 6 The sulfur content,% of the mass. 1.6-1.85 7 Calorific value (lower), kcal / kg 9703-10050

Table 5 Physico-chemical characteristics of the residue of atmospheric distillation obtained from Yarega oil No pp Indicators Actual Values one Density at 15 ° С, kg / m ³ 940-946 2 Kinematic viscosity at 100 ° С, cSt 25-30 3 Ash content,% 0.05-0.07 5 The sulfur content,% of the mass. 1.1-1.2

The proposed method is as follows (diagram). Dehydrated bituminous oil from the oil dehydration unit with the pump N-1 is fed to the light oil distillation unit to the K-1 column, the obtained light oil products are removed after cooling in the X-1 refrigerator. The remainder of atmospheric distillation from the bottom of the K-1 column by pump N-2 or dehydrated bituminous oil (when the content of light oil products in bituminous oil is 0-5% by mass atmospheric distillation is not carried out) by pump N-1 is fed to the T-1 heat exchanger block and further to the mixer C-1, where it is mixed with a solvent and sent to an extractor K-2. The solvent is fed into the extractor in two streams. Pure solvent is fed to the bottom of the extractor, and a mixture of raw materials and solvent is removed from the mixer.

The obtained deasphalting solution is removed from the top of the K-2 extractor, heated in a T-4 steam heater and sent to the C-2 deasphalting separator, where the main amount of solvent is separated and the deasphalting is sent to the K-4 solvent stripping column. After stripping off the solvent in the K-4 column, the deasphalting agent is discharged from the bottom of the K-4 column. The asphalt solution from the bottom of the K-2 column is heated in a T-3 steam heater and sent to the K-3 column for stripping the solvent. After stripping off the solvent, the asphalt is removed from the bottom of the K-3 column.

For the regeneration of the solvent, columns K-3, 4, a refrigerator X-2, a tank E-1, pumps H-3, 4 are used. The deasphalting process is carried out in one step.

The resulting products: light petroleum products and deasphalting can be removed from the installation with a mixture (low-sulfur liquid fuel) and separately as components of low-sulfur liquid fuel.

The proposed method allows the processing of bituminous oils with a minimum set of processes and obtain demanded oil products - low-sulfur liquid fuels.

During the processing of heavier or, conversely, lighter oils compared to Yaregskaya oil, the quality of the obtained asphalt and light oil products is controlled by selections in such a way as to obtain the maximum yield of low-sulfur liquid fuel with sulfur content up to 1% of the mass.

Literature

1. GOST R 51858-2002, Oil, General specifications.

2. Akhmetov S.A. et al. Technology and equipment for oil and gas refining processes. Nedra, 2006

3. Smidovich E.V. Oil and Gas Processing Technology, Part 2, Moscow: Chemistry, 1980

4. Sukhanov V.P. Catalytic processes in oil refining. M .: Chemistry, 1979

5. Oil refinery reference. Edited by G.A. Lastovkin, E.D. Radchenko and M.G. Rudin. - L .: Chemistry, 1986. 34-35 p.

6. Application for invention, 2006147241/04, 04/20/2005, date of publication of the application: July 10, 2008. Improving heavy oil and bitumen refining.

Claims (1)

A method for processing bituminous oils, including dehydration processes, atmospheric distillation of light oil products, deasphalting, characterized in that, during processing, dehydrated bituminous oil is separated in the process of atmospheric distillation into light oil products and the residue of atmospheric distillation, which is sent to the deasphalting stage with a solvent at a temperature of 120-130 ° C, pressure 4.0-4.5 MPa and volumetric multiplicity solvent: raw materials (1.5-2): 1, processes of atmospheric distillation of light oil products and deasphalting of the remainder of the atmosphere Sulfur distillation is carried out with such screenings that after mixing the obtained light oil products and deasphalting agent, the sulfur content in the mixture does not exceed 1% by mass, and a mixture is obtained that meets the regulatory requirements for low-sulfur liquid fuel.

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