RU2215020C1 - Heavy hydrocarbon feedstock processing method - Google Patents

Abstract

FIELD: petroleum processing and petrochemistry. SUBSTANCE: method involving double-step viscosity breaking comprises heating feedstock, affecting it by electromagnetic field prior to be fed into the first step, cracking in furnace and routing stream of feedstock and thermal destruction products to the second step in reaction section, cooling and separating stream of reaction products followed by fractioning of liquid products. According to invention, residual petroleum products preheated to 80-200 C, prior to be fed into the first viscosity breaking step, is exposed to constant magnetic field with magnetic induction 0.1-0.4 Tl at flow rate 0.003-0.05 m/s and constant temperature. EFFECT: increased homogeneity of oil system to raise extensiveness of processing heavy hydrocarbon feedstock, reduced coke formation in viscosity breaking process, and reduced power consumption in magnetic field generating device. 2 cl, 1 dwg, 4 tbl, 15 ex

Description

 The invention relates to the field of oil refining and can be used in the processing of oil residues.

A known method of processing residual petroleum feedstock by visbreaking, according to which the tar is subjected to cavitation treatment using a static cavitating mixer (the cavitating body is a ball, the degree of blocking of the flow is 80%) and mixed with aromatic or polar additives. The resulting mixture is subjected to visbreaking at 450 ^o C and 0.6 MPa (RF Patent 2021994, C 10 G 9/14).

The disadvantage of this method is the need for the addition of highly aromatic petroleum products or polar compounds (catalytic cracking gas oil, selective oil purification extract, acetone) and the involvement of distillate fractions in the visbreaking residue (above 180 ^° C).

There is also a method of producing liquid products from heavy oil residues by mixing raw materials with organic mineral additives using an electromagnetic vortex layer of ferromagnetic elements. The magnitude of the magnetic induction in the apparatus of the vortex layer is 0.08-0.3 T, the rotation frequency of the magnetic field is 1500-3000 rpm. The resulting suspension is cracked at 390-440 ^o C and a pressure of 0.2-5.0 MPa (RF Patent 2132354, C 10 G 9/00).

 The disadvantages of this method are the high energy consumption for creating an electromagnetic vortex layer in the mixers at both stages, as well as the contamination of the remainder of the products of visbreaking with metal as a result of abrasion of the ferromagnetic elements that create the vortex layer.

 Closest to the claimed method is a method of processing heavy hydrocarbons (Patent RF 2122011, C 10 G 9/14). According to this method, the raw material is subjected to two-stage visbreaking, after which it is fed to fractionation. Before feeding to the first stage, in order to reduce energy costs during the processing of heavy hydrocarbon feedstocks, it is exposed to an electric field with a strength of 0.5-1000.0 V / mm.

 The disadvantages of this method is a slight decrease in the temperature of the process and, consequently, energy consumption, low depth of conversion and output of distillate oil products and a complex device of the reactor creating an electric field.

 The problem solved by the claimed invention is to increase the homogeneity of the oil system to increase the depth of processing of residual petroleum products, produce marketable boiler fuels, reduce coke formation during visbreaking while reducing energy costs for the process and powering the device that creates an electromagnetic field.

The essence of the proposed method is the processing of heavy hydrocarbons by two-stage visbreaking. The method includes heating the feedstock, exposing it to an electromagnetic field before being fed to the first step, cracking in a furnace, and feeding the feed stream and thermal decomposition products to the second step to the reaction section. Then produce cooling and separation of the flow of reaction products and subsequent fractionation of the liquid product. The method is characterized in that the residual oil products preheated to 80-200 ^{° C.} are subjected to a constant magnetic field with a magnetic induction of 0.1-0.4 T at a flow rate of 0.003-0.05 m / s at constant temperature. Moreover, the lines of constant magnetic field intensity are directed perpendicular to the residual oil product flow vector. As a result of magnetic treatment, the dispersion state of a heavy hydrocarbon feed is converted, resulting in a decrease in the particle size of the dispersed phase of the oil system. As a result, the homogeneity of the oil system increases, which leads to an increase in the yield of light distillate fractions, and also reduces the association of polycondensed aromatic compounds (asphaltenes), that is, the formation of coke.

 The physicochemical characteristics of the heavy hydrocarbon feedstock are given in Table 1, and the changes in the dispersed state when exposed to a magnetic field are shown in Table 2. The tables show that when the residual oil product is heavier (from feed type 1 to type 6), the particle diameter of the dispersed phase has upward trend. An increase in the flow velocity in the absence of a magnetic field leads to a slight enlargement of particles. The influence of a constant magnetic field reduces the particle size of the dispersed phase, and with an increase in magnetic induction from 0.150 to 0.225 T, the influence of the field is more noticeable. An increase in the linear flow velocity also increases the effect of the magnetic field - a decrease in particle size reaches 27%.

 The results of visbreaking of heavy hydrocarbon feedstocks are presented in table 3, and the quality of the resulting boiler fuel is shown in table 4. It can be seen from the tables that a decrease in the process temperature by 10 degrees during visbreaking of residual oil products (feed type 1 and 6) allows, as in the prototype, to obtain commercial boiler fuel in almost the same amount. At the same time, visbreaking by the proposed method allows to maintain a rather high yield of light distillate fractions (about 27 and 31 wt.%, Respectively, for types of raw materials 1 and 6).

 An increase in the linear flow velocity and magnetic field induction increases the effect of a constant magnetic field. Thus, an increase in magnetic induction from 0.15 to 0.225 T causes a decrease in coke formation during visbreaking of heavy hydrocarbon feedstocks (feedstock type 6) by about 20% and an increase in the yield of light distillate fractions. At the same time, an increase in the flow velocity from 0.003 to 0.0011 m / s during visbreaking of the residual oil product (type 4) can reduce the coke yield by almost a third, and increase the yield of light distillate fractions by 3 wt.

 The inventive method allows the process of processing heavy hydrocarbon raw materials with greater efficiency, namely: to lower the temperature of visbreaking, to obtain a greater number of light distillate fractions, to obtain marketable boiler fuel brands M-40 and M-100, to reduce coke formation, i.e., coking of equipment, and, thus, increase the mileage of the installation between stops to clean the equipment from coke.

 The electromagnetic effect on heavy hydrocarbon feeds is carried out at low energy consumption using a simple magnetizer device (for example, Tebenikhin E.F. Reagentless methods of water treatment in power plants. - M .: Energy, 1977, S.80-98; RF Patent 2167824, C 02 F 1/48). This magnetizer is simpler and less energy intensive than a device that creates an electric field in the prototype (RF Patent 2122011, C 10 G 9/14).

The drawing shows a diagram of the processing of heavy hydrocarbons according to the proposed method. The proposed method is as follows. Heavy hydrocarbon feedstocks (feedstock I) are heated to 80-200 ^{° C.} and pumped through pump 1 through magnetizer 2 (apparatus producing a constant magnetic field). After exposure to a magnetic field, the heavy hydrocarbon feed is sent to furnace 3 to the first stage of visbreaking, where it is heated to a temperature of 420-460 ^o C and partially decomposes. Then the stream of unconverted heavy hydrocarbon feed and reaction products enters the second stage 4, where it undergoes thermal transformations for a certain time.

The products of reaction II, after leaving the reactor, are cooled in the refrigerator 5, and then fed to the receiver 6, where the separation into gaseous III and liquid phase IV takes place. Visbreaking gases are analyzed to determine their density and component composition using standard techniques. The liquid visbreaking product is separated into gasoline and diesel fractions and a residue> 300 ^o C. Their analysis is carried out according to standard methods. The dispersed state of the initial heavy hydrocarbon feedstock is determined by the method described in the article (Pivovarova N.A., Tumanyan B.P., Beregovaya N.M. Features of determining the particle size of the dispersed tar phase. - M .: Science and technology of hydrocarbons, 4, 2001, p. 168-169).

 Example 1

Heavy hydrocarbon feedstocks (feedstock type 1), characterized by the parameters given in Table 1, were heated to 180 ^{° C.} and subjected to a magnetic field at a linear flow velocity of 0.008 m / s and a magnetic induction of 0.225 T, after which they were sent at a pressure of 0.2 MPa in the heating section of the reaction furnace, where the temperature rises to 440 ^o With and there is a partial decomposition of raw materials.

Then the stream was fed into the reactor to the second stage of visbreaking, where a constant temperature of 440 ^° C was maintained. Gas was released from the reaction products, gasoline fraction nk-195 ^° C, light diesel fraction 195-300 ^° C and the residue. The yield of light distillate fractions was 28.9 wt.%. The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for low ash sulfurous fuel from high-paraffin oil.

 Example 2

The heavy hydrocarbon feed from Example 1 was subjected to a magnetic field under the conditions of Example 1 and visbreaking at a temperature of 430 ^° C. The yield of light distillate fractions was 26.9 wt.%.

 The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for low ash sulfurous fuel from high-paraffin oil.

 Example 3

 The heavy hydrocarbon feed (feed type 2) was subjected to magnetic field and visbreaking under the same conditions as in Example 1. The yield of light distillate fractions was 30.1 wt.%. The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 4

 The heavy hydrocarbon feed (feed type 3) was subjected to magnetic field and visbreaking under the same conditions as in Example 1. The yield of light distillate fractions was 36.9 wt.%. The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 5

 The heavy hydrocarbon feed (feed type 4) was subjected to magnetic field and visbreaking under the same conditions as in Example 1. The yield of light distillate fractions was 30.3 wt.%. The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 6

 Heavy hydrocarbon feedstocks (feedstock type 4) were exposed to a magnetic field with a linear flow velocity of 0.003 m / s and a magnetic induction of 0.225 T. The yield of light distillate fractions of the products was 33.2 wt.%. The quality of the residue obtained corresponded to the requirements for M-40 brand fuel oil.

 Example 7

 Heavy hydrocarbon feedstocks (feedstock type 4) were exposed to a magnetic field at a linear flow velocity of 0.011 m / s and magnetic induction of 0.225 T. Visbreaking was carried out under the same conditions as in example 1. The yield of light distillate fractions was 30.6 wt.%. The quality of the residue obtained corresponded to the requirements for M-40 brand fuel oil.

 Example 8

 The heavy hydrocarbon feed (feed type 5) was subjected to magnetic field and visbreaking under the same conditions as in Example 1. The yield of light distillate fractions was 31.2 wt.%. The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 9

 The heavy hydrocarbon feed (feed type 6) was subjected to magnetic field and visbreaking under the same conditions as in Example 1. The yield of light distillate fractions was 29.0 wt.%. The quality of the residue obtained corresponded to the requirements of the M-40 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 10

 Heavy hydrocarbon feedstocks (feedstock type 6) were exposed to a magnetic field at a linear flow velocity of 0.011 m / s and a magnetic induction of 0.150 T. Visbreaking was carried out under the same conditions as in example 1. The yield of light distillate fractions was 33.3 wt.%. The quality of the residue obtained corresponded to the requirements of the M-100 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 11

 Heavy hydrocarbon feedstocks (feedstock type 6) were exposed to a magnetic field at a linear flow velocity of 0.011 m / s and magnetic induction of 0.225 T. Visbreaking was carried out under the same conditions as in example 1. The yield of light distillate fractions was 36.0 wt.%. The quality of the residue obtained corresponded to the requirements of the M-100 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 12

Heavy hydrocarbon feedstocks (feedstock type 6) were subjected to a magnetic field at a linear flow velocity of 0.008 m / s and magnetic induction of 0.225 T. Visbreaking was carried out at a temperature of 430 ^o C. The yield of light distillate fractions was 31.1 wt.%. The quality of the residue obtained corresponded to the requirements of the M-100 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 13 (comparative).

 Heavy hydrocarbon feedstocks (feedstock type 4) were subjected to visbreaking under the same conditions as in Example 1. No magnetic field was applied. The yield of light distillate fractions was 23.3 wt.%. The quality of the residue obtained corresponded to the requirements of the M-100 brand according to GOST 10585-75 for sulfur ash fuel from high-paraffin oil.

 Example 14 (prototype).

The heavy hydrocarbon feed (heavy hydrocarbon feed) was subjected to a two-stage visbreaking according to the known method at 435 ^{° C.} , after which it was fed to fractionation. Before being fed to the first stage, the raw materials were subjected to an electric field with a strength of 0.5 V / mm. The residue yield was 86.0 wt.%. The kinematic viscosity at 80 ^o C was 84.2 cSt. Thus, the viscosity of the resulting residue corresponded to the requirements for boiler fuel brand M-100.

 Example 15 (prototype).

The heavy hydrocarbon feed (heavy hydrocarbon feed) was subjected to a two-stage visbreaking according to the known method at 445 ^{° C.} , after which it was fed to fractionation. Before being fed to the first stage, the raw material was exposed to an electric field of 1000.0 V / mm. The residue yield was 84.5 wt.%.

The kinematic viscosity at 80 ^o C was 85.0 cSt. That is, the resulting viscosity residue corresponded to the requirements for M-100 brand fuel oil.

Based on the data presented, it can be concluded that the proposed method for processing heavy hydrocarbon feeds allows to obtain up to 37 wt.% Light distillate fractions at 440 ^{° C.} with low coke formation. Moreover, when the process temperature is reduced by 10 ^o C and, accordingly, the energy consumption for heating the raw material is reduced, the yield of light distillate fractions is 26 -31 wt.%. The quality of the obtained visbreaking residue exceeds in its indicators (including ash content) the values required for GOST 10585 for boiler fuel grade M-40 (examples 1-2) and M-100 (examples 3-12), and therefore no distillate fractions are required to dilute the residue. In addition, the device for magnetic processing has a simpler design and does not require significant energy consumption for power.

Claims (2)

1. A method of processing heavy hydrocarbon feedstocks by two-stage visbreaking, including heating the feedstock, exposing it to an electromagnetic field before being fed to the first step, cracking in a furnace and feeding a feed of raw materials and thermal decomposition products to the second step into the reaction section, cooling and separating the reaction product stream followed by fractionation of the liquid product, characterized in that the residual oil pre-heated to 80-200 ^o With before submitting to the first stage of visbreaking is subjected a constant magnetic field with a magnetic induction of 0.1-0.4 T at a flow rate of 0.003-0.05 m / s at a constant temperature.  2. The method according to p. 1, characterized in that the line of constant magnetic field is directed perpendicular to the vector of the flow of raw materials.

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