SU1253984A1 - Method of producing oil fractions - Google Patents

Description

1125398 4

The invention relates to methods for the recovery of petroleum fractions.

The purpose of the invention is to increase the production of crude oil by reducing the energy consumption for the following: s process in two-stage installations of oil refining and irrigation of the upper part of the oily and atmospheric column with gas condensate, supplying 1 st in 10 specific amounts.

The drawing shows the setup diagram and the direction of the material flow.

The scheme contains: raw line 1, tS of the topping {salt 2, stream 3 of the top product of the topping column, condenser / cooler 4, reflux tank 5, stream b of the gasoline fraction of the topping column, 20 stream of gas condensate to irrigate the top of the topping columns, stream 8 of the bottom product of the topping column, tube furnace 9, stream W of mountains - 25 jets, stream 11 of excess boiled oil, atmospheric column. 12, atmospheric column overhead stream 13, condenser / cooler 14, reflux tank 15-30 of the gasoline fraction of the atmospheric column, stream 16 of the gasoline fraction for stabilization, gas condensate stream 17 for the irrigation of the atmospheric column, stream 18 of the kerosene fraction, stream 19 with solar fractions, flow 20-gas fraction, flow 21 fuel oil.

Oil feedstock is fed via line I to the topping column 2. Top product 3 from the topping column, vapors of the gasoline fraction are fed to condenser / cooler 4, where it is fully condensed. The condensed product is then sent to a reflux tank. From the reflux tank 5, benz1, the new fraction is directed to stabilization. Li 7 and 7 are used to irrigate the upper part of the topping column 50 with gas condensate. The bottom product 8 of the topping column, the topping off oil and gas condensate mixture is fed to the tube furnace 9, where it is heated to 350 ° C and sent along the line 55 10 to the bottom of the topping column as a hot stream, 3 balance excess oil and gas 40

45

de then chi ko nt l g v n l l

so lo ta doo

.

S 0 5 0

0 5

0

five

The condensate mixture, through line 11, heated before, is sent to the evaporative part of the atmospheric column 12. The top product 13 is from the atmospheric column, vapor of the gasoline fraction is fed to the condenser / cooler 14, where it is fully condensed. The condensed product is then sent to. Refsox tank 15. From the reflux tank 15, the gasoline fraction I6 is sent to stabilize. The gas condensate stream is fed to the irrigation of the upper part of the atmospheric column 2. As side streams of the atmospheric column, kerosene 1B, salt 19 and gas oil 20 fractions are removed. fuel oil 21 is injected from the bottom of the atmospheric column.

The invention is illustrated by the following examples.

Example 1, Raw material I in the amount of 8000 thousand tons is sent to the evaporating unit on a part of the topping column. The topping column is working in the r.ozhimae with the minimum ratio and maximum selection of gasoline fractions. The process is conducted in the following mode:

Pressure at . benzinating

column, Sha0.43

The temperature of the input of raw materials, s200 Top temperature topping

columns, p156

The temperature of the bottom of the topping column, ° C. 240 Acute irrigation temperature, C20 Hot jets inlet temperature, C 350 Reflux ratio at the top of a gasoline column 0.5. Molecular mass of gasoline with a boiling point of 180 ° C 105 Molecular mass of condensate with a boiling point of 280 ° C. 132

The number of squondon

sowed gasoline parov, required for irrigation of the upper part of the extraction column (8000x0.12: 0.5), thousand tons.

The amount (G) of gas condensate for irrigating the upper part of the withdrawal column is 603 thousand tonnes.

The gas condensate in the amount of 603.4 thousand tons is sent as an irrigation to the upper part of the bottom column. On top of the topping 1 column, a gasoline fraction in the amount of 1032 thousand tons or 12% for raw materials is taken.

From the bottom of the topping of the column is removed the topped mixture in the amount of 757 thousand tons or 88% for raw materials ..:

Oil-gas condensate stripped mixture 11 with a temperature of 757 thousand tons is supplied to the evaporative part of the atmospheric column. The atmospheric column operates in the mode with the maximum selection of diesel fuel, when the gas supply of the left fractions in fuel oil boiling up to 360 ° C reaches the smallest value.

The process is conducted in the following mode:

Pressure in the atmospheric column, MPa0,13

 Temperature BJCO- yes raw material, s360

Top temperature of the atmospheric column, C150 Bottom temperature i of the atmospheric column, C 340 The temperature of the lateral reflux kerosene, salt and gas-oil reflux is -190, equals respectively 234 C and 302 Acute irrigation temperature, C 20 The average reflux ratio in the gasoline ,

 kerosene, salt, 1.78 hours and gas oil 1.52 atmospheric sections, I, 25

-

-

15

2539844

Noah column and 0.5

Steam number in the distant part of the column; 0; 224 5 Molecular mass of gasoline with boiling point 180112 Molecular mass of condensate with end

to boil 280132

The amount of condensed gasoline vapor required to irrigate the upper part of the atmospheric column (8000-0.061.78) 854.4

. The quantity (G) of gas condensate for irrigating the upper part of the atmospheric column is 1007 thousand tons.

A gas condensate in the amount of 1007 thousand tons is directed as an irrigation to the upper part of the atmospheric column.

A total of gas condensate for irrigation of the stripped and atmospheric columns requires 1,610.4 thousand tons, which is 20.1% of the actual capacity of the installation and corresponds to the maximum possible loads of distillation columns.

Example 2. The process is carried out similarly to Example 1, but the amount of gas condensate for refluxing the topping column is 900. In this case, the operation mode of the topping column is as follows:

20

 25

thirty

35

40

Topping column pressure, Mila

Inlet temperature of the raw material, ° С Top temperature of the topping, ° C

The temperature of the bottom of the topping column, ° C

Acute irrigation temperature, C Hot jet entry temperature, ° C Reflux c. upper part: STI bobbing column

0.45

200

132

240

20

350

1.0

The yield of the gasoline fraction is 9% by weight of the raw material. The end of the boiling gasoline fraction

woo c.

An increase in the amount of gas condensate to irrigate the top of the atmospheric column as compared to the spreading one in Example 1 is impossible, since in this case the load by cf exceeds the permissible value and the fractional quality is determined.

Example 3. Irrigation with gas condensate from the top of the topping column in a quantity smaller than Example 15 leads to a deterioration in the quality of the gasoline fraction.

Analysis of the results of the process in examples 1-3 shows that the amount of gas condensate for irrigation in example I is optimal.

Example 4 (known)

The process is carried out in the following mode:

Topping column:

Pressure in the topping column, MPa Raw material inlet temperature, ° С

Top temperature of topping column, with

The temperature of the bottom of the topping column, C

Acute irrigation temperature, C Hot jet entry temperature, C

0.43,200

154

240

60

350

Reflux at the top of the topping column

Atmospheric column:

0

five

0

five

0

Pressure in the atmospheric column, MPa Inlet temperature of the feedstock, ° С Temperature of the top of the atmospheric column, s

The lateral reflux temperature of the kerosene, salt and gas-oil reflux is, respectively, C The temperature of the sharp irrigation, ° C The average reflux in the gasoline, kerosene, salt and gas oil sections of the atmospheric column is respectively The vapor number in the distant part of the column Comparison material balances of the process of obtaining petroleum fractions of example 1 and the known method j are given in table. 1.

A comparison of the economic efficiency of the known and proposed methods for carrying out the process is given in Table 2.

0.15

350

150

340

190

235

and 300

60

1.78, 1.41; 1.58-, and 0.34

0.226.

 Famous 8000

For example 1 9610

, (8000 (1610

3848

5458

oil) gas condensate)

48.1,960 12 1.3 1.17 1572.2

56.8 1032 12 11, 1.14 1737.5

Editor M.Nedoluzhenko

Compiled by V. Kostyuchenko

Tehred I., Popovich Proofreader A.Obruchar

Order 4686/28 Circulation 482Subscription

VNSHPI USSR State Committee

for inventions and discoveries 113035, Moscow, Zh-35, Auska, Ha6.j, d. 4/5

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

Claims (1)

METHOD FOR PRODUCING OIL FRACTIONS from petroleum feedstock using a two-stage processing scheme, including the removal of gasoline fraction vapors from the top of the topping - 4-Zavaya columns, condensation and withdrawal of condensed vapors of the gasoline fraction for processing, removal of vapors of the gasoline fraction from the upper part of the atmospheric column, condensation and withdrawal of condensed vapors of the gasoline fraction for processing, characterized in that, in order to increase the productivity of crude oil and reduce energy consumption to conduct the process, for irrigation of the upper part of the topping and atmospheric columns serves gas condensate in an amount determined by the formula where G _K h ' - total amount of gas condensate supplied for irrigation, t / h; the number of condensed vapors of the gasoline fraction required for irrigation of the upper part of the distillation column, t / h; molecular weight of the gasoline fraction; molecular weight of gas condensate. to>