SU1687596A1 - For warm-up of the chambers of the inhibited carbonization, steaming and cooling of the coke - Google Patents

Abstract

The invention relates to a method for heating chambers of delayed coking, steaming and cooling of coke and reduces the loss of petroleum products and reduces operating and energy costs. Hydrocarbon vapors are fed to the coking chamber to warm it, after coking of the crude oil, steam is supplied to the chamber to steal the coke and water to cool the coke. The products of heating the chamber, steaming and cooling the coke are removed from the chamber respectively. The products of steaming and cooling of coke are mixed with coking vapors having a temperature of 420 - 470 ° C, in a 1: 1 volume ratio. The resulting mixture is cooled with water together with the heating products of the chamber and the hydrocarbons are separated. Hydrocarbons with a boiling point higher than 200 ° C, QLF by sludge. Hydrocarbons with a boiling point below 200 ° C are recovered by evaporation. 2 hp f-ly, 1 ill. (L

Description

The invention relates to delayed coking of oil residues, in particular, to a method for heating chambers of delayed coking, steaming and cooling of coke, and can be used in the petroleum refining industry.

The purpose of the invention is to reduce the loss of petroleum products and reduce operating and energy costs.

The drawing shows an installation diagram for implementing the method.

The plant contains coke chambers 1 and 2, a distillation column 3, a furnace 4 for heating the raw material, a boiler 5, a condenser 6 mixing with a settling tank, through-valves 7 and 8, a mixer 9, a distillation column 10, a gasoline collection 11 and a gate valve 12-20 .

When the chamber is heated after pressing it with water vapor, valves 12 and 13 are opened, thereby directing the flow of hot coking vapors from the working chamber through chamber 1 to the boiler 5. The dehydrated product from the boiler 5 is sent to the raw material coil.

In the boiler 5, to separate the water from the product, the temperature is maintained at more than 130 ° C due to heat recovery of the heavy gas oil process, which

ABOUT

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J

ate

CD

SE

serves as a coolant. The heating operation of chamber 1 is carried out until reaching 1687596-1.

gasoline (fr. below 200 ° C) in the condenser Y.

Neither the wall temperature of the chamber is about 250 ° C, then the flow of condensation products from the bottom of chamber 1 is transferred to distillation column 3 and then the heating of chamber 1 is carried out in the usual way.

After filling the chamber with 2 coke to the level of 18-19 m, the feed stream from the furnace 4 is directed to the newly prepared chamber 1 heated to 370 ° C. To do this, close the valves 13 from the bottom of the chamber 1, open the valve 7 and gradually with the help of a 4-way valve The flow of raw material from the furnace coil is directed to the chamber 1. The valve 8 is closed. For steaming the coke into the filled chamber 2, water vapor is supplied for 1.5-5 hours by opening the valve 20. The vapors obtained by steaming from chamber 2 enter the column 3. After the steaming of the coke is completed, the column 3 is up to 5 hours long. the vapor flow from chamber 2 is directed to the mixing condenser 6, for which purpose the valve 15 is closed and the valve 17 is opened and the steaming of the coke continues with steam supply to the mixing condenser 6 for 3-5 hours.

The process of cooling the coke with water is a continuation of the steaming of the coke. To do this, close the valve 20 of the steam supply line to the chamber 2, open the valve of the water supply line to the chamber 2. The valve 17 is left open in the mixing condenser 6.; The coke in the chamber 2 is cooled to a vapor temperature at the outlet of chamber 2 to 100 ° C Then the chamber 2 is prepared for the coke unloading operation.

Immediately after the vapor has been transferred from the cooled chamber 2 to the mixing condenser 6, the valve 18 is opened in order to supply the hot gases from the working chamber 1 and maintain the thermal conditions in the displacement condenser 6. On line vapors from chambers to

the mixing condenser 6 is mounted mixed for intensive mixing 9, where vapors of intensive mixing of some of the coking vapors from the working and enter the mixing condenser 6. Water is supplied to the top plate to condense the wires in the mixing condenser 6.

The condensed product above the temperature of 200 C flows into the boiler 5, from where it is dehydrated, the product is pumped out into the raw material coil of the furnace, unfused vapors

chamber with vapor of the cooled reactor for the purpose of dissolving high-boiling hydrocarbons and resinous products with hot coking vapors. When the reactor is heated, the heating products are sent to the mixing condenser 6, where they come into contact with water and drain into the settling zone of the condensate

0 5

0

five

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.

Example 1 (known method). The tar of Surgut oil with a density of rh - 0.970 and coking ability of 10.8 wt.% Is heated in a furnace to 500 ° C and sent to the coke ovens. After the chambers are filled with coke, the coke is cooled with water vapor. Oil products released from the chambers, mixed with water vapor, are sent to an absorption column, where hydrocarbons are trapped in heavy coking gas — a solvent of high-boiling fractions by feeding it to the top of the column.

The liberated gases with low-boiling hydrocarbons from the absorber through the air-cooled condenser enter the tank, the liquid part from the tank is pumped out to the park, and the gases are sent for combustion.

When the chambers are heated, the heating products, which are preliminarily mixed with a solvent having a temperature of 200 ° C, are sent to a tank, from where condensed oil products are pumped out as a component of boiler fuel, and uncondensed hydrocarbons are sent to a distillation column.

Material balance of the installation, May.%:

Raw material

Tar 100

Received:

Gaz12,8

Fr NK-18011,9

26.0 21.8

Fr 450 C773

Coke19.2

Loss of petroleum products 1.0%.

PRI me R 2 (the proposed method). This feedstock is subjected to coking under the same conditions, but using a mixing condenser 6 and a mixer 9, preFr. 180-350 s fr. 350-450 ° C

about.

appointed for intensive mixing of coking vapors from working

chamber with vapor of the cooled reactor for the purpose of dissolving high-boiling hydrocarbons and resinous products with hot coking vapors. When the reactor is heated, the heating products are sent to the mixing condenser 6, where they come into contact with water and flow into the settling zone of the mixing condenser 6, from where they go to the booster and from the boiler 5 to the raw material furnace.

When steaming and cooling the coke in the chamber with steam and water, the hydrocarbon fractions in the vapor form come from the chamber to the mixer 9, where they are mixed with the solvent. As a solvent, pairs of hot hydrocarbon fractions from the operating reactor are used, they are fed with a temperature of 420-470 ° C in line in front of mixer 9 for vigorous stirring.

After the mixer 9, the resulting mixture is sent to the mixing condenser 6

The material balance of the installation, wt.%: Raw materials:

Tar 100

Received

Gaz12,8

Fr NK-180 ° C12,0

Fr 180-350 ° C27.9

Fr 350-450 ° C20.1

Fr 450 ° C 7.5 Coke19.5

Loss of oil products 0,2%. Operating conditions in the capacitor cm Sheni:

Pressure, MPa

Top temperature, C Temperature of the bottom, ° C Temperature of the product, its output from the boiler, ° C

The vapor temperature at the inlet to the mixing condenser, ° C. The ratio of solvent and vapor in front of the mixer

Up to 0.6 60-110 100-130

200-250

120-450

eleven

ten

20

25

thirty

35

40

From the presented primer pidno,

4th the proposed method allows

5 times to reduce the loss of petroleum products or installation.

In addition, the proposed scheme is more simple to manufacture and operate and is less energy-consuming, since it contains fewer pumps and other equipment and, accordingly, less metal box.

Claims (3)

1. The method of heating the delayed coking chambers, steaming and cooling the coke, including the supply of hydrocarbon vapors to the chamber to warm the water vapor for steaming the coke and water to protect the coke, respectively, withdrawing the heating products of the chamber, steaming and cooling the coke, mixing the products of the chopark and cooling the coke with the dissolving agent and the subsequent separation of hydrocarbons from this mixture, characterized in that, in order to reduce the loss of petroleum products and reduce operating and energy costs, the coking steam with a temperature of 420 is used as the dissolving agent - 470 ° C, mixing takes place in a 1: 1 volume ratio and, before the release of hydrocarbons, the mixture is cooled with water together with the heating products of the chamber. 2. A method according to claim 1, wherein the reaction is carried out by separating hydrocarbons with an initial boiling point above 200 ° C by sludge. 3. A method according to claim, characterized in that hydrocarbons are separated with a boiling point of less than 200 ° C by evaporation.