SU1162852A1 - Method of crude oil refining - Google Patents

Abstract

METHOD OF REFINING OIL by separating the original gas into liquid and vapor phases, followed by distillation of these phases in an atmospheric column while supplying the vapor phase and water vapor to the stripping section of the atmospheric column and distillation. the residue obtained in a vacuum column, characterized in that, in order to reduce the energy consumption per process, the vapor phase is directed to the middle of the distant section of the atmospheric column.

Description

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The invention relates to the refining industry and can be used in the primary distillation of petroleum.

There is a method of processing oil by distillation using an atmospheric column with an evaporator, followed by distillation of the remainder of the atmospheric column (fuel oil) in a vacuum column. In this method, the oil heated in the heat exchangers is introduced into the evaporator and separated into the vapor and liquid phases. The liquid phase is heated in an oven and fed to the feeding zones of the atmospheric column. The low-temperature vapor phase is also directed there. Water vapor is injected into the bottom of the stripping section for evaporation from the light fuel oil (diesel) fractions. The fuel oil is heated in an oven and sent to a vacuum column for separation.

However, this does not use the vapor phase evaporation capacity, where gas components and light boiling gasoline fractions are concentrated.

The closest to the invention is a method of refining oil in atmospheric yolon with an evaporator and c-subsequent distillation of the atmoch: ferric column residue in a vacuum column, through which oil heated in heat exchangers is introduced into an evaporator, where it is separated into vapor and liquid phases. The liquid phase is heated in an oven and sent to the feed zone of the atmospheric column, and the low-temperature vapor phase is fed under the bottom plate by distilling the section along with water vapor 2}

The disadvantage of this method is the increased energy consumption, since the introduction of a low-temperature vapor phase from the evaporator under the bottom plate by distilling the section of the atmospheric column lowers the temperature of the bottom column. This, in turn, leads to an increase in heat consumption in the furnace when the remainder of the atmospheric column is heated before it is directed to the vacuum column.

The aim of the invention is to reduce energy costs.

The goal is achieved by the fact that according to the method of oil refining by separating the initial gas into liquid and vapor phases, followed by distillation of these phases in an atmospheric column while feeding

vapor phase and water vapor to the stripping section of the atmospheric column and distilling the residue obtained in a vacuum column; the vapor phase is directed to the middle of the stripping section of the atmospheric column.

The drawing is a schematic diagram of the method.

Oil is heated in heat exchangers 1 and sent to evaporator 2. The liquid phase is withdrawn from the evaporator via line 3, heated in the furnace 4 and introduced into the feeding zone of the atmospheric column 5. The vapor phase is fed from the evaporator through line 6 between the plates, in the middle of the stripper sections of the atmospheric column, into the bottom of which water line is introduced via line 7. The remainder of the atmospheric column is withdrawn via line 8, heated in an oven 9 and sent for separation to a vacuum column 10.

Example. Characteristics of the original oil are given in table. one.

In order to compare the energy consumption during the distillation of oil, the calculations on the computer for the typical operating conditions of the columns were carried out using the known and proposed methods. In both cases, the temperature in the evaporating unit is 374 ° C in the feed zone of the atmospheric column. The pressure in the atmospheric column is 0.3 MPa, the flow rate of water vapor in the distillation section 1, O may.% For oil.

During distillation, gasoline fractions up to 130 ° C, kerosene 130-230 ° C, light diesel 230280 ° C and heavy diesel 280 360 ° C are obtained.

The various operating conditions of the atmospheric column and, in particular, the change in the connection scheme of the evaporator with a distillation column mainly reflects the quality of the heavy diesel fraction. In this connection, the selection of the remaining products is fixed, and the output of the heavy diesel fraction is selected in this way.

to have its constant group composition. In the above calculations, in the heavy diesel fraction, I control the content of the components boiling up to (96% according to the ITK), which causes its boiling point to 360 C.

Calculations for the known and proposed methods show that the output of the heavy diesel fraction is set3

quality, and therefore, fuel oil are almost the same. Under acceptable separation conditions, the residual of the atmospheric column is 51% by weight of oil with a content of light fractions (components boiling up to) 5.6% by weight.

It follows from the calculations that the temperature of the remainder of the atmospheric column during the distillation of oil by the proposed method is

in a known manner 334 s.

. The elevated temperature of the bottom of the column determines the increased supply of heat with a residue, which according to the proposed method is

48320 kJ per 100 kg of oil, and by a known method 46960 kJ per 100 kg of oil.

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Thus, the heat consumption in the furnace is reduced by the same amount by heating the residue to the same tempura {) temperature before entering it into the vacuum column.

In tab. Table 2 shows the composition of the heavy diesel fraction and azuta, obtained in the calculation by the known and proposed methods.

10 From table. 2 that during the operation of the column, 0.84% by weight of gasoline and kerosene fractions (components boiling up to 280 ° C) remain in the fuel oil by the known method in fuel oil, of which 0.66%

15 gasoline (up to 180 ° C) and 0.23% gas components. At. According to the proposed method, gasoline components in fuel oil are practically absent, and the fraction of fractions up to 280 ° C is 0.13%.

Table 1

Continuation of table 1

Claims (1)

METHOD FOR OIL REFINING by separating the feedstock into liquid and vapor phases, followed by distillation of these phases in an atmospheric column by supplying a vapor phase and water vapor to the distillation section of the atmospheric column and distillation. the obtained residue in a vacuum column, characterized in that, in order to reduce energy consumption for the process, the vapor phase is sent to the middle of the distillation section of the atmospheric column. SU „..1162852>