SU1273379A1 - Method of condensing vapours of vacuum column in process of petroleum refining - Google Patents

Abstract

The invention relates to the field of condensation of a mixture of vapor discharged from the top of the vacuum columns of an oil distillation process. In order to increase the degree of condensation and reduce environmental pollution, the vapor mixture is hydrocompressed. Then cooled and condensed in surface condensers. Next, the vapors are cooled and condensed. The condensed cooled oil is returned to the condensation of the vapor mixture. It is also used in hydrocompression of the initial vapor mixture. Hydrocompressing is carried out to atmospheric pressure. Non-condensed vapors are ejected to produce vapor and liquid phases. The amount of condensed water vapor is 1.5 wt.%, Condensed (oil fumes of petroleum products-} 0.8% by weight. 1 sludge, table 2).

Description

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The invention relates to methods for condensing a mixture of vapors containing petroleum products and water vapor captured from the top of vacuum columns of primary distillation units for petroleum, and can be used in the refining and petrochemical industries. The aim of the invention is to increase the degree of condensation and reduce environmental pollution.

The drawing shows a schematic diagram of the method.

The mixture of vapors from the top of the vacuum column with the temperature of 70-240 ° C in the amount of 1-20 wt.% For fuel oil via line 1 is fed to the receiving chamber of the hydrocompressor 2, where part of the oil cooled to 20 ° C is sent as a working agent.

The partially condensed vapor-liquid mixture with a temperature of 70120 s along line 4 is directed to a combined apparatus 5, operating under a pressure of 700-900 mm Hg. to zone 6 of surface oil condensers, and then to zone 7 of surface water condensers, where it is cooled and partially condensed. Uncondensed vapors from zone 7 are directed to zone 8 of the barometric condenser, where they are cooled and condensed by mixing with petroleum product having a temperature of 20-30 0. Uncondensed vapors from zone 8 along line 9 with a temperature of 30-40 ° C at a pressure of 700-900 mm Hg . served on steam ejectors 10, where they are ejected with water vapor with a temperature of 350,360 s. The product condensed in zones 6 and 7 of the heat removal from the bottom of the combined apparatus 5 is fed to the barometric well of the combined apparatus 5, where the condensed water vapor separates from it. The oil from apparatus 5 is sent to an intermediate tank 11 for separating the product from water. From the tank 11, the oil product is fed by the pump 12 to the refrigerator 13, where it is cooled to 2030 s and then sent via line 14 to the apparatus 5. The balance of the oil in an amount of 0.1 to 19.6 wt.% Is pumped out to the oil as a finished product. park on line 15. Supplied oil product in the amount of 5-30 wt.%

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the fuel oil is divided into two streams in the ratio of 3: 1 and directed respectively to the inlet of the hydraulic compressor 2 via line 3 and to the barometric condenser 8 via line 16. The oil withdrawn from the condensation zone through line 17 is sent to the zone 7 of surface water condensers from where it flows into the barometric well of the combined apparatus 5. The vapor – gas mixture from the steam ejector 10 is fed through line 18 to tank 19, where it is divided into vapor and liquid phases, which are sent, for example,

15 topping column 22 along lines 20 and 21 using steam 23 and liquid 24 ejectors, as steam irrigation and feed additive, respectively.

20 Example. Processing in a vacuum column is subjected to oil obtained from petroleum. The example is verified by calculation. Technological parameters and main indicators of the process of condensation of a mixture of vapors discharged from the top of a vacuum column, according to the proposed and known methods, are given in Table 1,

The operating parameters of hydrocompressor and ejectors are given in Table 2.

From the comparative data given in Table 1, it can be seen that the proposed method, in comparison with the consumption of the petroleum product for cooling and condensation of the vapor mixture in the combined apparatus with the same mixture, allows increasing the degree of condensation of the vapor mixture and reducing the consumption of water vapor for ejection uncondensed vapors.

Claims (1)

Invention Formula Method for condensing a vapor mixture of a vacuum column of an oil distillation process by cooling and condensing it in surface condensers, further cooling and condensation of vapors, collecting and separating condensation products, followed by cooling the condensed product, feeding it in two streams to condense the vapor mixture and ejecting uncondensed vapors with water vapor , different from the fact that, in order to increase the degree of condensation and reduce environmental pollution, the feedstock 312733794 It is preliminarily cooled, and the hydrocompression-condensed vapors of water obtained by ejection and condensation of hydrocompre- Table 1 The temperature of the exhaust vapor from the top of the vacuum column, C The pressure of the exhaust vapor from the top of the vacuum column, mm Hg The amount of exhaust vapor, wt.% (For fuel oil) Pressure in the combined apparatus, mm.rt.st. The temperature of non-condensed vapors discharged from the top of the barometric condenser, C Temperature of the petroleum product supplied to the combined apparatus, C The amount of oil supplied to the hydraulic compressor 2, t / h The amount of oil supplied to the barometric condenser, t / h The number of vapors condensed in the combined apparatus, wt.% (For fuel oil) water vapor of oil product vapors Amount of vapors leaving the barometric condenser, wt.% (For fuel oil) The amount of oil withdrawn from the combined apparatus as a marketable product, wt.% (For fuel oil) Fractional composition of the refrigerant: boiling point boiling point 225 225 45 45 12.5 12.5 52 760 45 40 29 21 70 100 thirty 1.35 9.7 1, h5 9.7 160 380 Process parameters and indicators Steam consumption on a steam ejector, May.% (For fuel oil) The temperature of the gas-vapor mixture, flow-. in the tank 19, C The pressure in the tank 19, MPa The number of vapors after the steam ejector, wt.% (for fuel oil) Hydro parametersPressure parameters 2 Oil Operator Agent Working agent pressure at the entrance, MPa Working agent temperature WITH Pressure at the outlet, MPa Mix temperature at the outlet 85 de, ° C The ratio of the areas of cross-sections of the mixing chamber and the working nozzle Injection Coefficient Water Acid Oil Steam Vapor 0.7 0.7 200 50 0.6 0.6 250 50 1.2 0.92 0.1 Continued table. I Method of lag- T Izvestny 1.5 10.9 340 0.11 1.712.35 Table 2. Ejector;, 10 23 24