SU1227652A1 - Method of processing heavy vacuum gas oil - Google Patents

Description

The invention relates to methods for the purification of heavy petroleum feedstocks, mainly heavy vacuum gas oils, and can be used in the refining industry.

The aim of the invention is to increase the yield of the target product.

The drawing shows the scheme of the proposed method.

From the remainder of the oil boiling above 350 ° C (fuel oil), two vacuum gas oil fractions are obtained: t, kip, 350-500 ° C and residual (fraction above 500 s, preferably 500-550 ° C),

These fractions are fed through lines 1 and 2 respectively to mixers Zi4, where they are mixed with circulating hydrogen-containing gas supplied through line 5, the resulting mixture is heated in raw heat exchangers 6 and furnaces 8 and 9, heated in furnace 8 to 370-400 ° C a mixture of the fraction with t, kip, 350 500 C is fed under the pressure of 4-7 Sch to the reactor 10 with a fixed bed of an alumino-cobalt or alum-nickel-molybdenum catalyst. The reaction is carried out with a bulk feed rate of 1-5 hours. To reduce the heating of products due to the energy available during the reaction, cold purified hydrogen-containing gas through line 5 is supplied to the reaction zone Gndrogenizat coming out of the reactor 10 , is separated at the same temperature into vapor and liquid phases in a high-temperature high-pressure separator 11. The residual fraction is heated in a furnace 9 to 390-420 ° C and sent with a bulk velocity of 0.5-1.5 hours to one of the parallel-connected reactors 12 or 13 to remove metals. The catalyst in these reactors is spent catalyst from reactor 10,

Reactors 12 and 13 are switched on alternately: first, the heated stream passes through reactor 12, and reactor 1 is shut off to unload the spent catalyst from it and replace it with the catalyst discharged earlier and the main reactor 10, then shut off the reactor 12 to unload and turn on the reactor 13, Usually, in the reactor 10, the service life of the catalyst is 2–4 times longer than in reactors 12 and 13, since in the light component there are very few metals.

27652i

irreversibly deactivating catalysts. But yoskolka loading volume of this catalyst is also almost 3-4 times. More than in reactors 12

5 and 13 (due to the corresponding difference in quantities of 1 and 2 fractions), the amount of catalyst treated in reactor 10 is enough to load reactors 12 and 13, using

10 of this spent catalyst in demetallization reactors 12 and 13 allows, without prejudice to the depth of metal recovery, to save an appropriate amount of fresh catalyst.

After the metals are removed from the feedstock, the stream is mixed with cold hydrogen-containing gases supplied through line 5 to lower the temperature and

20 is directed to the second stage in the main reactor 14 purification of the residual fraction with a bulk velocity of 0.51, 5 h

- (

Hydrogenate exiting

0

five

0

five

the reactor 14 is separated at the temperature of the reactor in a high-temperature high-pressure separator 15. The vapor phases 16 and 17 from the high-temperature high-pressure separators 11 and 15 are mixed, cooled, and 0 is directed through a condenser / cooler 18 to a low-temperature separator 19 under high pressure, where at 35-50 ° C, a hydrogen-containing gas is separated through line 20. The latter is cleaned from hydrogen sulphide r on purification unit 21 and returned to line 22 via feed line 22 by feeding fresh hydrogen into the reaction zone and mixing it with feed pump components.

The liquid phases along lines 24 and 25 of the high-temperature high-pressure separators 11 and 15 are throttled through the valves 26 and 27 to a pressure of 0.1-0.3 MPa and fed to the high-temperature low-pressure separator 28. Due to the sharp decrease in pressure in this separator, residues of light gases dissolved in streams 24 and 25, as well as light side fractions boiling up to 350 ° C, formed as a result of cracking side reactions, separate from the liquid phase. . The liquid phase from the separator 28, which is practically free of fractions up to 350 ° C (the heavy component of hydrogenate), is withdrawn through line 29, cooled in heat exchangers 30 and refrigerator 31. and removed from

 3

Tai11pk11 as a finished product. The flapo ({laTv is withdrawn through line 32, cooled n with an equalizer ator 33 to 33-SO C and fed to a low-temperature separator FOR low pressure, where the pressure is close to the pressure in separator 28 (0.08-0.25 Sha.) An unstable light fraction of hydrogenate from separator 19 is supplied through line 35 to throttle valve 36. Hydrocarbon gases are separated from low pressure separator 34 through line 37 ° C and sent to hydrogen sulfide purification unit 38. t along line 39, heated in heat exchangers 40 to 280-350 ° C and sent to a stabilization column 41, where side light fractions are separated: gasoline line (42 ° C) at the line 42, 43 from the top of the column through the condenser and 43 separator 44 from the diesel line (160-350 ° C) through the line 45. At the bottom of the column 41, line 46 serves water vapor to deepen the selection of fractions up to 350 C.

A stabilized fraction is withdrawn from the bottom of the column via line 47 (above 350 ° C hydrogenation, which after cooling in heat exchangers 48 is mixed with the heavy hydrogenation component discharged through line 29, and this mixture is removed via line 49 as a finished target product — hydrotreated older vacuum gas oil

Example. From the fuel oil of West Siberian oil, two fractions of upgraded vacuum gas oil — light (350-500 C) with a sulfur content of 1.6 wt.%, Resins 6.6 wt.% And vanadium 1 mg / kg in an amount of 223 tons are obtained by deep vacuum distillation. / h and residual (500-540 C) with a sulfur content of 2, O may.%, 13% resins and vanadium

1.8 mg / kg in the amount of 38 t / h. The first one is mixed at a pressure of 6 MPa with hydrogen and hydrogen-containing gas, which is cold from hydrogen sulfide, in an amount of 475 (23.8 tons / h), the mixture is heated to 37 (J C and sent to the reactor | In the case of alum-nickel-molybdenum KaTajn-3aT () poM on a C1-skate basis in the amount of 81 tons, where the main reaction of hydrogenolysis of sulfur- and az1g (: 11 retaining compounds takes place. The products of this reaction (hydrogenate

light fractions) at temperature renapaTopf pygokogo pressure at 402 ° C and 4.7 MPa are divided

ten

five

2 /

0 5

o 5

0

five

0

 on the azoparuoru (101145 t / h) and liquid, kyu (153973 t / h) phases. To lower the temperature in the reactor, cold gas (GHA in the amount of 7.9 t / h) is fed to the intermediate section of the reactor. The residual fraction (500-540 C) is mixed at a pressure of 6.1 IPa with cold and purified GHS in the amount of 4.1 t / h (415 nm / m), the mixture is heated to 400 ° C and sent to a preliminary demetallization reactor, where hydrogenolysis reactions of the heaviest heteroorganic (mainly organometallic) compounds proceed to the processing of TaHtfOM in the light fraction reactor. ) compounds. The resulting metals in amounts 2-3 mg / kg of the heavy component in the form of oxides (sulfides) are deposited in the pores of the catalyst. The products of this reaction stage after mixing with cold WASH in the amount of 1335 kg / h with a temperature of 391 ° C enter the main reactor of the heavy fraction, where they are hydrogenated sulfur and nitrogen-containing organic compounds. The products of this purification stage (residual fraction hydrogenation product) are separated in a high-temperature high-pressure separator at 4-10 ° C and a pressure of 4.7 MPa into gas-vapor (14371 kg / h) and liquid .

The gas vapor phases of the hydrogenates of the light and residual fractions are mixed, this mixture in an amount of 1 15608 kg / h is cooled to 35 ° C and separated in a separator at a pressure of 4.5 MPa.

Separated in the amount of 4 1426 kg / h, VASH is directed to the removal of hydrogen sulfide from an aqueous solution of MEA at 35 ° C and a pressure of 4.5 Sh, then returned again to mixing with the raw material. The liquid phases of the hydrogenates of the light and residual fractions are also mixed, this mixture in the amount of 182 tons / h is throttled to a pressure of 0.2 MPa and separated in a high-temperature separator at 397 ° C. The liquid phase from this separator (the heavy component of the hydrogenate) is cooled in heat exchangers and removed from the installation, and the vapor phase in an amount of 18.3 tons / h is cooled to 50 ° C and fed to a low-temperature low-pressure separator, which is also fed to a throttled unstable light fraction of hydrogenate in the amount of

7A t / h from a low pressure high temperature separator. In this separator, at a temperature of 50 ° C, 2.2 t / h of hydrocarbon gases are separated, which are sent to hydrogen sulfide for purification and removed from the installation.

The liquid phase in the amount of 90 t / h is heated in heat exchangers up to 350 ° C and fed to the stabilization column, to the bottom of which 1800 kg / h of water vapor are fed to stripper the light fractions.

From the top of the column, 39.9 t / h of the n. (160 ° C) at 133 ° C. This fraction is cooled to 50 ° C and returned in the amount of 39 tons per hour to the column as cold reflux, the remaining amount (1.9 tons per hour is sent to the hydrogen sulfide purification and removed from the installation.

From the 10th tray, the liquid phase is withdrawn and sent to a stripping column to obtain a fraction of 160-350 ° C. B, 300 kg / h of steam are fed to the bottom of the stripping column. The residue from the flue column of the fraction 160-350 C in the amount of 23 t / h with a temperature of 200 ° C is cooled to 50 ° C and removed from the installation.

The remainder of the main column t.

a fraction above 350 ° C in an amount of 65.4 t / h with a temperature is passed through heat exchangers at 100 ° C, mixed with a heavy component and the mixture in an amount of 229.4 t / h is removed from the installation as a finished product with sulfur content O, 18 May

Below are these mlteril.

installation balance. Enter

to G / h May. %

Raw material

Frakda 350-500 С Fraction 500-540 С VSG (hydrogen gas)

but-

264032 101.2

229448 87.9 22970 8.8

1904

0.7

22070.9

25221.0

39961.5

9850.4

264032101.2

Thus, the proposed method, as compared with the known processing of vacuum-added gas-free gas, allows to increase the selectivity of hydrogenolysis reactions of hetero-organic compounds and bring their conversion depth to 90-92% (against 80-85%) and increase the yield of the chain product — hydrotreated vacuum gas oil up to 88% of the feedstock.

Y

V. Compiler E. Gorlov. L. Veselovska Editor. Tehred M. Khodanych. Corrector M. Maximipgi.

Order 2796 Circulation 482 Subscription

VNIIPI USSR State Committee

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

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

P

Claims (2)

METHOD FOR PROCESSING A HEAVY VACUUM GAS OIL by displacing raw materials with a pre-purified hydrogen-containing gas, catalytic hydrogenation of the mixture to obtain hydrogenizate, its high-temperature separation at a temperature and hydrogenation pressure to obtain vapor-gas and liquid phases, low-temperature separation in a high-pressure vapor-gas phase pressure followed by its stabilization from light side fractions, characterized in that, in order to increase the efficiency of cession, vacuum gas oil previously fractionated with m. bales. 350-τ500 ^υ 0 and the residual, which are directed to separate hydrogenation, the hydrogenation products are separated, the combined gas and liquid phases are combined, the resulting vapor-gas phase is cooled, separated into a hydrogen-containing gas and an unstable light hydrogenated fraction, and the liquid phase is throttled to produce a vapor phase and the heavy component of the hydrogenate, the vapor phase is condensed, mixed with the unstable light fraction of the hydrogenate throttled to the same pressure and then sent to the or, bottoms stabilization residue is mixed with the heavy component of hydrogenation to obtain the target product. 2. The method of pop. 1, characterized in that the hydrogenation of the residual fraction is carried out in the form of a stage using the first stage of the processed catalyst for hydrogenation of the fraction of vacuum gas oil with _t , bale. 350-500 ° C.