SU1249061A1 - Method of producing fuel fractions from gas condensate - Google Patents

Description

one

This invention relates to gas condensate fuel fraction methods.

The aim of the invention is to improve the quality of fuel fractions due to the additional refluxing of the upper part of the distillation column with gas condensate of a naphthenic-aromatic base, supplied in a certain amount.

The drawing shows the principle; 1l- on the scheme of the installation for obtaining fuel fractions from gas condensate.

The scheme contains the raw material line 1., Distillation column 2, overhead product stream 3 of the distillation column, condenser / cooler 4, reflux tank 5, irrigation line 6, excess gasoline fraction 7, gas condensate flow 8 of naphtenoaromatic base for irrigation in the upper part of the distillation column, bottom product stream 9 of the distillation column; a tube furnace 10; a hot jet line II; an excess diesel flow 1 2.

The raw material, gas condensate, flows through line 1 to the distillation column 2 "The top product 3 of the distillation column, a pair of gasoline fraction, is fed to the condenser-cooler 45 where it is fully condensed. The condensed product is then sent to re (} shuksuyu capacity 5, from the latter part of the condensed product is sent along line 6 as irrigation to the upper part of the atmospheric column, and the excess gasoline fraction 7 is sent to the consumer. Atmospheric columns: gas condensate from the aftenoaromatic ospo / van. The bottom product 9 of the distillation column, part of the diesel fraction is fed for heating to the tube furnace 10, where its complete evaporation takes place. odayut through line 11 as reflux hot bottom of distillation column 2 and bug ansovy excess diesel fraction 12 is fed to the consumer.

The composition and characteristics of the gas condensate are shown in Table 1.

90612

Example, Gas condensate (tabl.), In the amount of 50 thousand, t is fed through raw line 1 to the evaporative part of the distillation column 2, which operates in mode C with the maximum extraction of gasoline fractions.

The process is carried out in the following mode: pressure in the distillation column 0.11 MPa; input temperature of the raw material is 160 С; temperature of the top of the distillation column 140 C 5 temperature of the bottom of the distillation column 200 C; temperature acute oroshe15 NIN 60 C; the temperature is hot

jet 320 C; reflux number in: the upper part of the distillation column

,eight;

steam number in the distant one

parts of distillation column O, 616;

the experimental density of the benzene and diesel fractions, as well as the gaseous condensate of the naphthenoaromatic base, are respectively 730 5 830, 770 kg / m

The amount of gas condensate of a naphteno-aromatic base according to the formula given is (730,)

g. ,, 830 thousand tons (1 - 770

From the upper part of the distillation column, gasoline fraction vapors with a boiling point of 180 ° C are taken, which are condensed and cooled in the temperature range 140-60 ° C, Ha; 5O) napytenoaromatic condensate

The bases in the amount of 16.6 thousand tons d, additionally served: and the freezing of the upper part of the distillation code was compounded, and the balance surplus was condensed, x vapors 7 sent to the consumer and the weight.

Upper and lower products meet the requirements of GOST for gasoline A-72 and GOST for DI - brand 3 fuel, their output

is respectively 50% each.

Example 2 (known method) The process is carried out as described in Hoivry in Example 1. but without the additional refluxing of the top of the column with naphtheno-aromatic gas condensate: - base. The output of diesel fuel is 36% by weight of the raw material. Diesel fuel soot3

GOST for diesel fuel brand 3,

The gasoline yield is 64 wt. by weight of the raw material, however, the quality of gasoline does not correspond to GOST, Example 3. The process is carried out on raw materials, as in Example 1, but the amount of gas condensate of the naphthenic aromatic base is 21 thousand tons or 36 May. 7. by weight of raw materials

The process is carried out in the following mode: the pressure in the distillation column is 0.13 MPa; temperature of input of raw materials temperature of the top of the distillation column 128 C; bottom temperature of the distillation column; acute irrigation temperature 60 ° C; hot stream temperature 320 ° C; reflux number in the upper part of the distillation column -2,2 steam number in the distant part of the distillation column 0,620,

The yield of gasoline fractions is 41% by weight.

The yield of diesel fractions is 59% by weight of the raw material,

An increase in the consumption of gas condensate of the naphteno-aromatic base as an additional irrigation of the upper part of the distillation

60

102

157

300

The content of hydrocarbons, wt.%:

paraffin 70; naphthenic 13; aromatic 17.

compared to the example, leads to an irrational distribution of hydrocarbons of various bases in the gasoline and diesel fractions, which in turn leads to an increase in the normalized potential of the operating properties of these fractions

reduces the reserves of the normalized potential of raw materials and increases the cost of reproduction and processing of raw materials.

Example 4. The process is carried out on raw materials and according to the mode of example 1, but the amount of gas condensate of a naphthenic-aromatic base for additional irrigation of the upper part of the distillation column is less than in example 1.

The quality of gasoline does not correspond to GOST, since the octane number of gasoline is 68-70 against the required value of 72,

The material balance of the process according to the proposed and known methods, as well as information on the quality of the products obtained are given in Table 2,

Table 3 presents data on the quality of the gasoline and diesel fractions obtained by the proposed method.

Table 1

350 781

-36

1H

The output of the condensate, wt.%

Density, kg / m

Fractional composition with NC

ten%

50%

90% 96%

QC

Volume yield,%

Kinematic viscosity at 20 ° С, m7 s 10

Pour point, ° С

Acidity, mg KOH / 100 ml

Flashes

Sulfur content, wt.%

Octane number

The number of more than 35 over 0.5 over 1 15 over 160

more than 180 98

50

870

172

202

232

260

302

98

No more than 250

No more than 340

98

2.31.8-3.2 -38 -35

more than 3,0 2,10 Not more than 5

more than 0.15 0.02Ne more than 0.2 less than 72

56Not less than 45

Editor P.Kossey

Compiled by V. Kostyuchenko Tehred V. Kadar

Order 4202/27

Circulation 482. Subscription VNIIPI USSR State Committee

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

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

Corrector; L. Pilipenko

Claims (1)

The METHOD FOR PRODUCING FUEL FRACTIONS FROM A GAS CONDENSATE in a distillation column, including the removal of gasoline fraction vapors from the upper part of the distillation column, condensation and supply of a part of the condensed vapors for irrigation of the upper part of the distillation column, and the excess of gasoline fraction to the consumer, and the output that, in order to improve the quality of fuel fractions, gas condensate of naphthenoaromatic base is additionally supplied to the top of the distillation column the quantity determined by the formula where G _kha is the amount of gas condensate of the naphthenoaromatic base supplied for additional irrigation, kg / h; G _op - the amount of condensed vapor of the gasoline fraction supplied to the irrigation of the upper part of the distillation column, kg / h; „90 - the density of the naphthenoaromatic gas condensate supplied for irrigation. whom is the foundation; Dr - the density of the diesel fraction; P is the density of the gasoline fraction. SU „, 1249061