SU1247392A1 - Method of producing petroleum fractions - Google Patents

Description

The invention relates to methods for producing petroleum fractions.

The aim of the invention is to improve the performance of the method for the crude oil and increase the yield of gasoline fractions due to the additional supply of gas condensate to the topping column.

According to the invention, a part of the gas condensate calculated by the first formula shown is preheated and served as additional hot strings in the lower part of the topping column, and a part calculated by the second formula given is served as additional irrigation in the upper part of the topping column.

The drawing is a schematic diagram for implementing the invention.

The scheme includes the raw line 1j to the topping column 2, the overhead stream of the topping column 3, condenser / cooler 4, reflux tank 5, irrigation line 6, overflow-gasoline fraction 7, bottom toppings 8 bottom stream, tubular furnace 9, stream the main hot jet 10j is a stream of excess waste from stripped oil 11, a stream of gas condensate 12, a stream of heated gas condensate 13, an evaporator 14, an additional stream of hot stream 15, and an additional irrigation stream 16.

Raw materials (raw oil) are fed via line 1 to the topping column 2, the top product of the topping column 3 — the gasoline fraction with the end of boiling — is not superior; it is fed to the condenser / cooler 4, where it is fully condensed. The condensed product is then sent to a reflux tank 5, from which a portion of the condensed product is sent along line 6 as reflux to the top of the topping. and the excess gasoline fraction 7 is sent to stabilize. The bottom product 8 of the topping column - stripped oil - is fed to a tube furnace 9, where it is heated to and sent along the line as a hot stream 10 to an evaporative one. part of the topping column 2, and the balance of the stripped oil 11 is recycled to the atmospheric column. Gas condensate 12 served in the convection part of the pipe

12473922

furnace 9, where it is heated to 250 ° C and sent to the evaporator 14. The top product of the evaporator (vapor phase gas condensate 13) is fed to the bottom 5 of the topping column as an additional hot stream 15,

0

five

0

thirty

The bottom product of the evaporator (gas condensate reflux 12) is fed as an additional reflux 16 of the concentration part of the topping column.

An example of the method.

Raw material t in the amount of 8,000 thousand tons is sent to the evaporative part of the topping column. The stream of hot jet 10 of stripped oil is fed to the bottom of the stripping column. The main hot stream of the initial stripped oil is fed to the evaporative part of the topping column.

The amount of vapor of the gas condensate is determined, which is supplied as an additional hot stream 25 of the topping column.

G 2680

ABOUT

730,744.

 388.3 thousand tons

870,770

At a boiling point of 250 ° C, the yield of gas condensate along the NTK curve is 71% by weight.

The amount of gas condensate reflux is determined, which is fed as an additional reflux to the concentration part of the topping column,

,, 388.3 (100-71) .с „,

GOP 15 8.6 thousand, t.

The required amount of gas condensate per process is. 546.9 thousand tons per year.

The process is conducted in the following mode; pressure in the topping column 4 MPa; raw material inlet temperature 220 ° С; temperature of the top of the topping column, temperature of sharp irrigation of the top of the topping column

60 С; additional irrigation stream temperature of 240 ° C; temperature in the evaporative part of the topping column; temperature of the bottom of the topping column: 240 ° С; temperature of the main hot jet of the sleeving column 360 ° CJ the temperature of the additional hot jet the reflux number in the upper part of

3

gasoline column 2.9; steam number in the lower part of the atmospheric to ponny 0,236; the consumption of the main hot water in the country is 33.5%; the consumption of additional irrigation for raw materials 1.98%; The relative fraction of the pro-phase in the hot jet flows was 43.2%.

A gasoline fraction in the amount of 1,530 thousand tons or 17.9% of raw materials is collected on top of the topping column, which is 95.7% of the potential output; From the bottom of the topping column, the recovered oil in the amount of 7016.9 thousand tons or 82.1% for raw materials; The depth of selection of light oil products from their potential in the raw material is 4,402 thousand tons or 95.9% at a two-stage distillation of an oil and gas condensate mixture.

In the known method, the yield of gasoline fractions in the topping column is 1320 thousand tons or 15% at a depth of selection of their potential of 93.5%. The yield of light petroleum products is 4,224 thousand tonnes or 48% with a depth of extraction from a potential of 93.5.

With an increase in the supply of gas condensate as an additional hot stream and additional irrigation in more quantities than according to the above formulas (700 thousand tons versus 546.9 thousand tons), all the final results of the operation of the installation deteriorate. R

The process in the topping column

lead in trace mode: pressure in the topping column 5 MPa; raw material inlet temperature 220 C; tempera

tour of the top of the topping column 128 С; the temperature of the acute irrigation of the top of the topping column is 60 ° C;

T a b l

The quality indicators of the fractionation according to the well-known

and proposed methods

Crude oil

870

2.7

ten

20

thirty

35

Q

additional irrigation stream temperature of 240 ° C; temperature of the bottom of the topping column 240 С; temperature of the main hot jet of the topping column; temperature of the additional hot jet of 250 ° C .; reflux number in the upper part of the topping column: 3.5; steam number at the bottom of the topping column 0,320.

From the top of the topping column, a gasoline fraction is taken at the end of boiling point of 126 ° C in the amount of 1050 thousand tons, or 12% for SFE, which fS is 64.5% of the selection from the potential of gasoline fractions boiling away to 180 ° C (total 1627 thousand tons).

Thus, increasing the supply of gas condensate as a hot stream and additional reflux of the topping column more than the above formulas reduces the boiling end of the selected gasoline fractions and their output from the total potential of gasoline, increases the pressure and loading light gasoline fractions of the atmospheric column, which reduces the depth of selection of target fractions from their potential to 93-94%.

Reducing the supply of gas condensate as a hot stream and additional reflux to the topping column reduces the capacity of the plant for oil feedstock, and hence the yield of gasoline fractions.

In tab. Figures 1 and 2 present the quality indicators of the fractionation according to the prototype method and according to the proposed and material balances of these methods are given.

25

and c a 1

I

0.146

0.236

0.352

0.432

Gas condensate 770

Continuation of table

cm

P)

S

h y n n

Editor M.Kelemes

Compiled by N. Vsesv tsk

Tehred I. Gajdosh Corrector L. Pilipenko;

Order 4079/25 Circulation 482 - Subscription

VNYIPI USSR State Committee

for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5

Production and printing company, Uzhgorod, st. Project, 4

Claims (1)

METHOD FOR PRODUCING OIL · FRACTIONS from crude oil c. topping column, including the removal of gasoline fraction vapors from the top of the topping column, condensation and supply of a part of the condensed vapors to irrigate the top of the topping column, and the balance excess of gasoline fraction to processing, removal of the topped oil from the bottom of the topping column, heating and supply of a portion of the heated as a hot jet of a topping column, and a balance of excess topped oil for processing into an atmospheric column, which distinguishes so that in order to increase the productivity of the method for petroleum feed and the output of the gasoline fraction, gas condensate is additionally supplied to the topping column, where G ^ is the amount of vapor phase of the gas condensate supplied as an additional hot stream, t; G _{2 fe.} - the amount of hot stream of the main stream of stripped oil, t, - the density of gasoline, kg / m ³ ; - the density of the vapor phase of the gas condensate, kg / m ³ ; - oil density, kg / m ³ ; gas condensate density, kg / m ³ ; preheated and served as an additional hot stream in the lower part of the topping column- §. us and the chart calculated by the formula / Rad ’ V 4PF. / Ζ Rvd \ „ 1 -—- XI, η io pia Central Committee With _About r-Cg.s. part of which, calculated according to RZB _. T20 1 P w. - amount of a hot stream of the main stream of stripped oil, t; - the density of gasoline, kg / m ³ , - the density of the vapor phase of the gas condensate, kg / m ³ , - the density of oil, (raw materials) j kg / m ³ , - the density of the gas condensate, kg / m ³ , χί, η - mass fraction of the vapor phase of the gas condensate, served as additional irrigation in the upper part of the topping column. ^{g "e G} nc p ^g cf pro p ^th 'CPU io 1 10