Method of oil residue processing into distillate fractions

FIELD: oil-and-gas production.

SUBSTANCE: invention related to oil-and-gas production, particularly to crude oil refinery with low temperature initiated cracking, and can be use for distilled motor fuel production increase. The method includes of oil residue processing into distillate fraction by adding catalyst followed by thermal-cracking, as a catalyst use ashes micro sphere magnetic fractions d from heat and power plants in a quantity 2.0-20.0% wt, containing 40.0-95.0% wt, iron oxide (III), with micro sphere diametres 0.01-0.60 mm, tempered at 600-800°C, process itself to be executed at temperature 400-500°C.

EFFECT: increase in distilled fractions total outcome up to 58,0% wt with the temperature up to 350°C, outcome of gasoline fractions up to 18,0% wt (with the temperature up to 200°C).

1 cl, 1 tbl, 7 ex

 

The invention relates to the field of oil processing, namely, processing of heavy petroleum residues in the process initiated by low temperature cracking, and can be used to obtain a distillate diesel fuels.

Currently, in the context of global trends - increasing oil consumption and reduce the amount of proven reserves of light oil, the further development of the petrochemical industry aimed at increasing the depth of oil processing and oil residues. Thus, at the moment in the world there are researches and new technologies of deep processing of heavy hydrocarbon feedstocks.

At the moment, described many ways of deep processing of non - traditional raw material heavy oil and oil residues, etc. (Nadirov NICHOLAS heavy oil and natural bitumen. In 5 volumes, volume 3. - Almaty: "Gylym". 2001).

A method of obtaining distillate fractions of petroleum residues by mixing them with the crushed catalyst - waste enrichment of molybdenum, or cobalt, or Nickel, or tungsten ores and subsequent thermal cracking units resulting mixture (RF patent 2182923, 2002).

The disadvantages of the method are the need for preliminary preparation of the catalyst (grinding) and subsequent homogenization of the catalyst with the raw materials and ivaska of this method to the territorial location of plants enrichment above ores (as the delivery of these catalysts over long distances and is not able to regenerate reduce the profitability of this method).

The known method of pyrolysis oil residue in the presence of hematite (Sharipov VI, Beregovoe N.G., Baryshnikov S.V., Kuznetsov B.N. Chemistry for sustainable development. - 1997, No. 5. - Page 287-291). The disadvantages of the method are the necessity of using water vapor, preliminary mechanical activation of the catalyst and duration of 4-5 hours.

Closest to the proposed method is a method of thermal processing of the heavy oil in the presence of micaceous iron catalyst (teliashev EG, Gurkin OP, Vezirov P.P., Larionov S.L., Imashev U.B. / Chemistry of solid fuels. in 1991, No. 5. - P.57-62).

The disadvantages of the method are the necessity of using in the process of water vapor and a low yield of gasoline fraction that does not exceed 5%.

The objective of the invention is to simplify the process of heavy oil residue and increasing the yield of distillate fractions by using as a catalyst the magnetic fractions of microspheres evils combined heat and power plants (CHP).

This object is achieved by carrying out thermolysis of heavy oil residues in the presence of a magnetic fractions of microspheres (diameter of the microspheres is from 0.01 to 0.60 mm) angry CHP, calcined at 600-800 is With in 2 hours containing up to 40,0-95,0 wt.% iron oxide (III), taken in an amount of 2.0-20.0 wt.%, at temperatures of 400-500°C for 100-120 minutes.

The technical result of the invention is the increase in the total output of distillate fractions up to 58,0 wt.% at temperatures up to 350°C, output gasoline fractions to 18.0 wt.% at temperatures up to 200°C.

Example 1

In used as raw material oil. In a fuel injected 2.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 800°C for 2 hours. The process is carried out in an autoclave periodic operation at 400°C for 120 minutes. Process indicators shown in the table.

Example 2

In used as raw material oil. In a fuel injected 2.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 800°C for 2 hours. The process is carried out in an autoclave periodic operation at a temperature of 450°C for 120 minutes. Process indicators shown in the table.

Example 3

In used as raw material oil. In the fuel oil is injected 10.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 800°C for 2 hours. The process is carried out in an autoclave periodic operation at a temperature of 450°C for 120 minutes. Process indicators shown in the table.

Example 4

In used as raw material oil. In the fuel oil is injected 20.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 800°C for 2 h the owls. The process is carried out in an autoclave periodic operation at a temperature of 450°C for 120 minutes. Process indicators shown in the table.

Example 5

In used as raw material oil. In a fuel injected 2.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 800°C for 2 hours. The process is carried out in an autoclave periodic operation at 500°C for 120 minutes. Process indicators shown in the table.

Example 6

In used as raw material oil. In a fuel injected 5.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 600°C for 2 hours. The process is carried out in an autoclave periodic operation at a temperature of 450°C for 120 minutes. Process indicators shown in the table.

Example 7

In used as raw material oil. In the fuel oil is injected 15.0 wt.% magnetic fractions of microspheres angry CHP, calcined at 600°C for 2 hours. The process is carried out in an autoclave periodic operation at a temperature of 450°C for 100 minutes. Process indicators shown in the table.

Thus, the new method allows to increase the output of distillate fractions up to 58,0 wt.% and to simplify the processing of heavy residue of oil.

Table
Note the market process initiated by low temperature cracking
No.ConditionsExamples
1234567
1.Oil98,0%98,0%90,0%80,0%98,0%98,0%90,0%
2.Microspheres angry CHP:
- calcined at a temperature of 600°C-----5,0%15,0%
- calcined at a temperature of 800°C2,0%2,0%10,0%20,0%2,0%- -
3.Process conditions:
temperature, °C400450450450500450450
- the heating rate, °C/min20202020202020
- duration, min120120120120120120100
4.The weight loss of the sample, wt.%:
- at temperatures up to 100°C0,0%0,0%1,0%2,5%3,0%0,0% 1,0%
- at temperatures up to 200°C0,0%0,0%6,5%14,5%18,0%1,5%7,5%
- at temperatures up to 300°C9,0%10,0%18,5%36,0%42,5%9,0%22,5%
- at temperatures up to 350°C22,0%24,0%31,5%49,5%58,0%19,5%35,0%

A method of processing oil residues in distillate fractions by integrating catalyst with subsequent thermocracking, characterized in that the catalyst used in the magnetic fractions of microspheres evils combined heat and power plants in the amount of 2.0 to 20.0 wt.%, containing 40,0-95,0 wt.% iron oxide (III), with the diameter of the microspheres is from 0.01 to 0.60 mm, and calcined at 600 To 800°C, the process is carried out at a temperature of 400-500°C.



 

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41 cl, 16 ex, 2 tbl

FIELD: physics.

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22 cl, 27 ex, 4 tbl, 12 dwg

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20 cl, 24 ex, 5 tbl

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16 cl, 3 tbl, 12 ex

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2 cl, 1 tbl

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15 cl, 1 ex, 1 tbl, 1 dwg

FIELD: industrial organic synthesis catalysts.

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EFFECT: increased selectivity of catalyst.

12 cl, 3 tbl, 12 ex

FIELD: carbon materials.

SUBSTANCE: invention relates to porous carbon materials and, more specifically, to carbon catalyst supports and sorbents. Preparation of catalyst support is accomplished by mixing carbon material with gaseous hydrocarbons at 750-1200°C until mass of carbon material increases by 2-2.5 times, after which resulting compacted material is oxidized, said initial carbon material being preliminarily demetallized carbon nanofibers.

EFFECT: increased sorption capacity of material.

1 tbl, 6 ex

FIELD: carbon materials.

SUBSTANCE: invention relates to porous carbon materials and, more specifically, to carbon catalyst supports and sorbents. Preparation of catalyst support is accomplished by treating carbon black with hydrocarbon gas at heating and stirring until mass of carbon material increases by 2-2.5 times, after which resulting compacted material is oxidized, said hydrocarbon gas being gas originated from liquid hydrocarbon electrocracking and said treatment being carried out at 400-650°C.

EFFECT: simplified technology.

1 tbl, 6 ex

FIELD: petroleum processing catalysts.

SUBSTANCE: catalyst containing platinum, rhenium, antimony, and chlorine on alumina are prepared by impregnation of carrier with aqueous solution of compounds of indicated elements, antimony being deposited as first or second component. Once antimony or platinum-antimony combination, or rhenium-antimony combination deposited, catalyst is dried at 130°C and then calcined in air flow at 500°C. Reduction of catalyst is performed at 300-600°C and pressure 0.1-4.0 MPa for 4 to 49 h. After deposition of antimony or two elements (platinum-antimony or rhenium-antimony) and drying-calcination procedures, second and third or only third element are deposited followed by drying and calcination. Final reduction of catalyst is accomplished in pilot plant reactor within circulating hydrogen medium at pressure 0.3-4.0 MPa and temperature up to 600°C for a period of time 12 to 48 h.

EFFECT: enhanced aromatization and isomerization activities of catalyst and also its stability.

2 cl, 1 tbl, 8 ex

FIELD: exhaust gas afterburning means.

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EFFECT: increased catalyst activity and imparted sufficient resistance to aggressive sulfur-containing components.

27 cl, 2 dwg, 7 tbl, 6 ex

FIELD: chemistry.

SUBSTANCE: invention refers to the field of organic synthesis, namely to the preparation of butyraldehyde from synthesis gas and propylene by the method of oxo process (called also propylene hydroformylation process), particularly to the cobalt regeneration of cobalt sludge. The described method involves the regeneration of the cobalt from cobalt-containing sludge forming in oxo process with usage of cobalt dicarbonyl as catalyst by the way of sludge treatment by the high-boiling organic acid with stirring at elevated temperatures, preferably 190-220°C at the ratio acid: sludge equal 10-20 during no less than 4 hrs.

EFFECT: simplifying of the technology of cobalt sludge regeneration and implementation of the regeneration stage directly on the hydroformylation plant.

3 cl, 3 tbl, 1 ex

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