Method for processing of high-temperature pyrolysis condensate fraction homogeneous pyrolysis of saturated hydrocarbons composition c3- c5
The invention relates to integrated processing of high-temperature pyrolysis condensate fraction homogeneous pyrolysis of saturated hydrocarbons With3-C5. The pyrolysis condensate fraction is subjected to fractionation with the selection of the first fraction with so Kip. to 80-83oWith the second fraction so Kip. from 84 to 164oWith and VAT residue with so Kip. over 165oC. the First fraction is predominantly benzene with a basic substance content of about 90%, the second fraction is oxidized by potassium permanganate at a ratio by weight of 1:3.6 and 4.0 when heated for 3-4 h in aqueous solution at the boiling temperature of the reaction mass to obtain benzoic acid with the release of 63-68% of theory. VAT residue is subjected to chlorination molecular chlorine at a temperature of 80-140oIn the presence of a catalyst FeCl3for 1.5-2.0 hours from the receipt of mastic with a chlorine content of 50-77%. Originally chlorination lead in carbon tetrachloride 0.5 h at 80oWith, then distilled it and continue to gloriavale for 2 h at 140oC. Technical result - utilization of by-products of high-temperature pyrolysis to produce salable products. 2 C.p. f-crystals, 3 tables. The invention apply the average composition from C3H8to C5H12in the production of acetylene and ethylene.With all the differences of technological processes pyrolysis of hydrocarbons at a temperature of 1,600-2,000oC and above [S. P. Gorislava and other Pyrolysis of hydrocarbons. Ed. "Naukova Dumka", 1977, S. 197, 292] [Ang. Patent 924591, 1963] to target products are always accompanied by the formation of a significant amount of pyrolysis condensate fraction. In the production of acetylene and ethylene pyrolysis condensate fraction, the so-called "stable aromatica', cannot find qualified, is in the dump or in the best case, it is used as a component of boiler fuel.Target qualified recycling pyrolysis condensate fraction as waste production, not only can significantly improve the economic, but also to improve the environmental performance of production. Unskilled such wastes have a certain toxicity (and even cancerogenity) [Harmful substances in industry. A DSS. so 1, ed. "Chemistry", L.-D., 1976, S. 77, 140 and others], is not conducive to environmental protection and production safety.Known technical solutions for processing of pyrolysis condensate fraction associated with fractional distillation, selective extraction and fractional talk of the hydrocarbons. Ed. "Naukova Dumka", 1977, S. 197, 292]. However rational this solution is not. The selection of one component does not solve the problem in General, and the selection of each of the 15 components of the mixture products of the pyrolysis condensate fraction is only a theoretical value. For practice it is extremely difficult and very expensive solution.In particular, this is illustrated in the method of separating a mixture of aromatic hydrocarbons [Ed. St. USSR 422164, With 10 G 25/00. Bull. 12, publ. 30.03.74].More acceptable technical solution is the way co-processing of pyrolysis condensate fraction and spent sulphuric acid [Ed. St. USSR 1772133 A1, 10 G 17/06. Bull. 40, publ. 30.10.92]. Disposal of waste is carried out by sulphurization of 85% H2SO4aromatic products of pyrolysis condensate fraction at a mass ratio of 1:1-2 when heated to boiling, followed by distillation of the unreacted benzene with the release of 2-35% while gaining sulfatase (about 60-70%), which is of interest for use in the production of concrete.However, this method of processing of pyrolysis condensate fraction partially solves the problem of waste production for a number of reasons.For large volume production is. In addition, processing is subjected to the pyrolysis condensate fraction, containing in its composition 52-53% benzene and 0.6-0.7 per cent higher aromatic hydrocarbons, and the rest falls on the alkyl benzenes. Such a composition of the pyrolysis condensate fraction is formed at low loads hydrocarbon feedstock in the production of ethylene and acetylene. Under optimal operating modes of the homogeneous pyrolysis of benzene content in the pyrolysis condensate fraction in 2-3 times less, and higher aromatic hydrocarbons of about 20%. While the hallmarks of the way the joint waste disposal must be different.Technical solutions associated with the processing of other pyrocondensation or hydrocarbons, do not set a goal and tasks similar to those stated. So, as an oxidizer for treatment of various fractions widely used oxygen O2and the air, for example, [Ed. St. USSR 1382404 A3, 10 G 27/06. Bull. 10, publ. 15.03.88], hydrogen peroxide H2O2[Ed. St. USSR 1540998 A1, 10 G 17/06. Bull. 10, publ. 15.09.90], Gidropress tert-butyl, but they are all dedicated to the purification of hydrocarbons from impurities.The proposed method for the processing of pyrolysis condensate fraction solves the problem of disposal of waste by expanding areas of using the product about the Dien 1-2, benzene 15-20, toluene 35-40, ethylbenzene 15-20, styrene 8-15, phenylacetylene 1-3, higher aromatic hydrocarbons 12-18.The task of the invention is to obtain benzene, benzoic acid and mastic from a complex mixture of products, which is the pyrolysis condensate fraction of the high-temperature pyrolysis of hydrocarbons.The technical result is achieved in that the pyrolysis condensate fraction is initially subjected to fractional distillation at atmospheric pressure under reflux into three fractions: the first fraction with so Kip. to 80-83oWith the second fraction with so Kip. from 84 to 165oAnd the third and so Kip. more than 165oC - VAT residue. Chemical and chromatographic analysis shows that the first faction in the number of 14-19% by weight of pyrolysis condensate fraction is predominantly benzene content of the basic substance is not less than 90%. This benzene can be used as a solvent, additives to motor fuel, etc.,The second fraction with so Kip. from 84 to 165oWith oxidized by potassium permanganate KMPO4when the ratio (wt.) 1:3,6-4,0 when heated for 3-4 h in aqueous solution at the boiling temperature of the reaction mass to obtain benzoic acid with the release of 63-68% of theory. Benzoic acid is used in p is x products.Physico-chemical basis of the oxidation process specified fraction of the pyrolysis condensate fraction is based on the use of simple and affordable method of oxidation of homologues of benzene, containing marginal and multiple bond in the side chain. Regardless of the length of the chain oxidation to carbonposition relative to the aromatic nucleus. Used aqueous solutions of oxidizing agent KMPO4commonly used for the oxidation of toluene. The consumption of the oxidizing agent when it is close to the stoichiometry based on each component of the second distillate fraction (after distillation of benzene). Gross-equation process includes oxidation of each component (its equation), for example, ethylbenzenewith subsequent neutralization of hydrochloric acid With6H5The Cooke+Hcl-->6H5COOH+KCl Should be borne in mind that the decomposition of the oxidizer Mno2and Kalemie salt can be used for its intended purpose, the latter, for example, as potash.The third faction with so Kip. more than 165oC - VAT residue is subjected to chlorination molecular chlorine at a temperature of 80-140oWith the presence catalectic is a waxy substance from dark brown to black, so pl. from 92 to 106oWith depending on the depth of chlorination. Mastic close in performance and industrial purpose product - mastic halowax (Galowax 1001,USA) [Industrial organochlorine products. A DSS. Ed. by L. A. Osina. Ed. "Chemistry", M., 1978, S. 530-532] . It can be used for impregnation of fabrics and wood to make a fire in the building business, in the production of building materials and rubber products.Physico-chemical basis of the chlorination process specified fraction of the pyrolysis condensate fraction is based on the ability of organic compounds to enter into substitution reactions under the action of chlorine in the presence of a radical or ionic activators process. So, by chlorination of peat or lignite wax in solution, at a temperature of 10-12oC for 2 h are chlorinated wax with a chlorine content of 3,6-6,92% [Ed. St. USSR 1004451, With 10 G 73/00. Bull. 10, publ. 15.03.83]. The above halowax is a product of electrophilic aromatic substitution under the action of chlorine on naphthalene in the presence of metal chlorides Fl3or ll3where n=3-4.The third faction with so Kip. more than 165o(Higher aromatic hydrocarbons in the amount of 12-20% from pyrocondensation accounts for about 50% of the composition. The reactivity of such compounds above naphthalene. The transformation is more heat and does not require heating at the initial stage. For heat removal is necessary VAT residue to gloriavale in carbon tetrachloride CCl4with the subsequent regeneration of the solvent.Formed at the initial stage of chlorination and end (without solvent) of hydrogen chloride is readily absorbed by water in the form of hydrochloric acid used for neutralization at the stage of selection of benzoic acid in the oxidation of the second fraction of the pyrolysis condensate fraction.It should be borne in mind that prolonged exposure to chlorine at temperatures140oWith these higher aromatic hydrocarbons does not contribute to the process of substitution. More competitive are the processes of degradation and elimination, sharply decreases the chlorine content in the final product (due to the removal of Hcl) and decreases sharply so square (break C-C bonds).The invention is illustrated by the following examples.Processing of pyrolysis condensate fraction carried out as follows. The addition of pyrolysis condensate fraction is subjected to distillation at atmospheric pressure fractional distillation installation under reflux for three frda oxidation (examples 1-6); the third faction is the VAT residue is used as the feedstock for the process of chlorination (examples 7-15).Example 1. In Trekhgorny reactor equipped with reflux condenser and stirrer, load 10 g of a second fraction of the pyrolysis condensate fraction, 740 ml of water and 38 g of finely pulverized potassium permanganate (ratio of mass fractions of pyrolysis condensate fraction : KMPO4it is 1:3,8). Boil the mixture for 4 hours After the reaction colorless solution is cooled, the precipitated manganese dioxide MnO2filtered off and washed twice with hot water (10-15 ml). The filtrates are combined, evaporated and acidified with concentrated hydrochloric acid until acid reaction to Congo. This precipitated benzoic acid. It is filtered off, washed with ice water and dried.Received 8,31 g of benzoic acid With6H5COOH with so PL 121-122o(Sample mixing temperature depression is not).Output 66,45% of theoretically possible quantity 12,50 g, which follows from the calculated value of the molar fractions of the components of the mixture of the second fraction of the pyrolysis condensate fraction (0,0582 toluene; 0,0246 ethylbenzene; 0,0167 styrene; 0,0028 phenylacetylene).Examples 2-6. The oxidation of the second fraction of the pyrolysis condensate fraction carried out analogously to example 1, wherein less time is a great value, but less time (example 5). It should be borne in mind that the completeness of the reaction by oxidizing (bleaching) is observed only in example 6. In example 5, the completeness of the reaction MnO2occurs at a ratio of 1: 3,6, as in example 3 - with a ratio of 1:4,0. When colored solutions of the reaction mixture becomes colorless by the addition of small amounts of ethyl alcohol. The results of the experiments are summarized in table 1. They show that the best conditions for oxidation are the conditions of example 1, with variations in composition corresponds to the ratio of the second fraction : KMPO41:3,6-4,0.Example 7. In a three-neck reactor equipped with a reflux condenser with absorption of gases, a stirrer and a bubbler, a load of 50 g of the third fraction of the pyrolysis condensate fraction (VAT residue), 50 ml of carbon tetrachloride CCl4and 0.5 g of ferric chloride FeCl3. Under vigorous stirring served chlorine Cl2from a cylinder with a flow rate of 0.6-0.7 g/min for 30 minutes after the specified time the reflux condenser is changed downward, at a temperature of 80oWith distilled carbon tetrachloride (48-50 ml, which is used in subsequent examples at the initial stage chlorination). After removal of CCl<'s the promotional mass is blown with nitrogen to remove residual hydrogen chloride (absorbed by water in the flask Drexel).Received of 92.5 g (gain 85% of the initial mass) mastic with so pl. 104-106oWith a total chlorine content of 72%.Mastic is a waxy substance in black with a faint odor of organochlorine products. Does not burn or support combustion, such as wood after impregnation (tested method of fire pipes according to GOST 16363-81). Mastic soluble in acetone, carbon tetrachloride, benzene at low heat; almost insoluble in benzene and hexane; insoluble in water.Examples 8-15. Chlorination of the cubic residue is carried out analogously to example 7, with a higher temperature (example 8), a large contact time of the reactants, there is a degradation product with the active secretion of hydrogen chloride (example 12), lower temperature (example 11) and less contact time (examples 14, 15). The results of the experiment are shown in table 2. They show that the mastic is most similar in its properties to "halowax", based on the melting temperature and the content of total chlorine obtained in examples 9, 10, 13, and example 7, which defines features of the invention under the conditions of chlorination. The optimum temperature 12020oWith more than who headed the remainder of in carbon tetrachloride at 80oC for 0.5 h followed by regeneration of the solvent.Comparative data for the processing of high-temperature pyrolysis condensate fraction homogeneous pyrolysis of saturated hydrocarbons, declared and known way, most closely related to the goals and objectives listed in table 3. When a certain difference in the composition of the starting mixtures of aromatic hydrocarbons in both cases used the pyrolysis condensate fraction the same production as the target product emit benzene using a distillation process. However, the procedure, time and place of the distillation process in the system of measures on waste management is different. A variety of other target products and, accordingly, techniques, and processes for their production. Outlined displayed in restrictive and distinctive part of the claims.
Claims1. Method for processing of high-temperature pyrolysis condensate fraction homogeneous pyrolysis of saturated hydrocarbons With3-C5to target products using the process of distillation, characterized in that the pyrolysis condensate fraction is subjected to fractional distillation under reflux at atmospheric pressure and Ganaton potassium to benzoic acid, and VAT residue with so Kip. more than 165oWith subjected to chlorination molecular chlorine at a temperature of 80-140oWith getting mastic.2. The method of processing of pyrolysis condensate fraction under item 1, characterized in that the fraction with so Kip. from 84 to 165oWith subjected to oxidation with potassium permanganate KMnO4when the ratio of the fraction:KMPO41:3,6-4,0 mass for 3-4 h in aqueous solution at the boiling temperature of the reaction mass.3. The method of processing of pyrolysis condensate fraction on the PP.1 and 2, characterized in that the VAT residue of pyrolysis condensate fraction with so Kip. more than 165oWith subjected to chlorination in the presence of a catalyst FeCl3in the amount of 1% by weight of the cubic residue at a temperature (12020)oC for 1.5-2 hours until the chlorine content of the mastic 50-77%, and for heat removal initially glorious VAT residue in carbon tetrachloride at 80oC for 0.5 h followed by regeneration of the solvent.
FIELD: crude oil treatment.
SUBSTANCE: to remove hydrogen sulfide and mercaptans, 3-30% solution of urotropin in technical-grade formalin or in formalin/aqueous ammonia is added to crude material in amounts corresponding to 0.8-3.5 mole formaldehyde and 0.009-0.3 mole urotropin per 1 mole hydrogen sulfide and mercaptan sulfur. Reaction is carried out at 15 to 70°C. Method is applicable for oil and gas production and petroleum processing industries.
EFFECT: reduced consumption of reagents at high degree of purification of raw material.
5 cl, 3 tbl
FIELD: crude oil treatment.
SUBSTANCE: invention relates to removal of hydrogen sulfide and mercaptans from petroleum and gas condensate. Process is conducted through oxidation of impurities with air oxygen dissolved in petroleum under pressure up to 2.5 MPa at 20 to 70°C in presence of solution of ammonium salts of cobalt sulfophthalocyanines in 20-30% aqueous ammonia solution. Reagents are used in following amounts calculated per 1 mole hydrogen sulfide: 0.1-1.6 mole NH4OH, 0.05-0.1 g phthalocyanine catalyst, and 0.05-0.1 m3 air. More specifically, ammonium salts of cobalt sulfo-, disulfo-, tetrasulfo-, dichlorodisulfo-, and dichlorodioxydisulfophthalocyanine are used. Part of exhausted ammonia catalyst solution is separated from cleaned raw material and returned into process.
EFFECT: minimized consumption of reagents and power, and enabled carrying out the process directly under oil-field conditions.
10 cl, 1 dwg, 2 tbl, 3 ex
FIELD: organic chemistry.
SUBSTANCE: invention refers to enhanced method of propane and/or butanes flow separation from original hydrocarbons containing alkylmercaptan impurities by means of fractional distillation resulted in liquid phase and separated flow from column head at pressure providing that separated flow from column head containing propane and/or butanes has temperature within 50 to 100°C, including (i) addition to specified origin hydrocarbons an amount of oxygen sufficient for mercaptan oxidation, (ii) fractional distillation of produced mixture containing at least one catalyst layer oxidising mercaptans to sulphur compounds with higher boiling temperatures and (iii) separation of sulphur compounds with higher boiling temperatures as portion of distillation liquid phase.
EFFECT: improved method of propane and/or butanes flow separation from of original hydrocarbons by means of fractional distillation resulted in liquid phase and separated flow.
8 cl, 2 tbl, 1 dwg, 1 ex
FIELD: organic chemistry.
SUBSTANCE: invention refers to hydrocarbon raw materials decontamination from sulphur compounds and can be applied in oil-processing industry. Described hydrocarbon raw materials decontamination from sulphur and sulphur compounds includes oxidation at contact of hydrocarbon raw materials with process reagent, mixture separation resulted from this contact with decontaminated hydrocarbon raw materials, before oxidation hydrocarbon raw materials are treated with, negative electromagnetic field and after oxidation with oxygen as process reagent hydrocarbon raw materials flow goes heavily stirred water containing reagent in proportions to hydrocarbon raw materials within 1:50. Then mixture flow is dispersed and soothed before separation and additional selection of released gas and sediment. Technological effect is simplification of hydrocarbon raw materials decontamination process.
EFFECT: simplification of hydrocarbon raw materials decontamination from sulphur and sulphur compounds.
5 cl, 1 dwg, 1 ex
FIELD: technological processes; chemistry.
SUBSTANCE: method involves reaction of raw material containing organic component with a catalyst composition. Processing method is selected out of alkylation, acylation, hydrotreatment, demetallisation, catalytic deparaffinisation, Fischer-Tropsch process and cracking. Catalyst composition includes mainly mesoporous silicon dioxide structure containing at least 97 vol.% of pores with size in the interval from ca. 15 Å to ca. 300 Å, and at least ca. 0.01 cm3/g of micropores. Mesoporous structure features at least one catalytically and/or chemically active heteroatom in amount of at least ca. 0.02 mass %, selected out of a group including Al, Ti, V, Cr, Zn, Fe, Sn, Mo, Ga, Ni, Co, In, Zr, Mn, Cu, Mg, Pd, Ru, Pt, W and their combinations. The catalyst composition radiograph has one 0.3° to ca. 3.5° peak at 2θ.
EFFECT: highly efficient method of organic compound processing in the presence of catalyst composition without zeolite.
20 cl, 31 ex, 17 tbl, 22 dwg
FIELD: chemistry; technological processes.
SUBSTANCE: method of hydrocarbon oil desulfurisation involves hydrocarbon oil contact with hydrodesulfurisation catalyst in hydrodesulfurisation reaction zone (3) to reduce sulfur content to a relatively low level, and contact of obtained hydrocarbon flow from hydrodesulfurisation zone with an oxidiser (8) to transform residual sulfur-containing compounds with low grade of concentration into compounds oxidised for sulfur. Obtained hydrocarbon oil flow with compounds oxidised for sulfur is separated by contact to adsorbent material (18, 30) adsorbing compounds oxidised for sulfur, after decomposition of any residual oxidiser. With obtaining of hydrocarbon oil flow featuring low concentrations of compounds oxidised for sulfur. Exhausted adsorbent (18, 30) is recovered and returned to service as adsorbent.
EFFECT: obtaining products with ultra low sulfur concentration.
SUBSTANCE: method includes contacting of oil distillate with oxygen-containing gas under oxidation conditions at temperature from 110°C to 175°C in presence of heterogeneous catalyst, containing metal of VIII group on base carrier, for oxidation of any sulfur- and/or nitrogen-containing compounds into oxidised sulfur- and/or nitrogen-containing compounds. Shift of composition of sulfur- containing compounds is performed towards heavier compounds, which results in desulfurisation approximately on 90%, and after further stage of isolation - to content of sulfur at level lower 5 fraction, nitrogen - less than 10 fraction by weight.
EFFECT: ecologically safe components for mixing in obtaining transport fuels for oil-processing plants.
11 cl, 3 ex, 1 dwg, 5 tbl
SUBSTANCE: method of selective fuel oxygenation based on distillate raw material includes contacting of said raw material with oxygen-containing gas in oxidation zone in conditions of oxidation in presence of oxidation catalyst, representing cobalt, in amount from approximately 0.1 wt % to approximately 50 wt % in account for total catalyst weight, and base carrier in form of magnesium oxide or calcium oxide, and isolation of outlet distillate flow, containing introduced oxygen and method of selective oxygenation of distillate flow, which lies in contacting of said raw material with oxygen-containing gas in oxidation zone in conditions of oxidation in presence of oxidation catalyst, which contains cobalt in amount from 4 to 12 wt % and magnesium oxide.
EFFECT: improvement of cetane number and characteristics of gases coming off distillate raw material.
6 cl, 3 ex, 3 dwg, 2 tbl
SUBSTANCE: invention refers to method of refining oil, gas condensate and oil fractions from mercaptans by means of catalyst alkali-free liquid phase oxidising de-mercaptanisation at temperature 20-50°C using as catalyst a homogenous liquid composition containing 15-20 wt % of copper chloride or bromide (II), 30-50 wt % of alcohol C1-C3 or mixture of the said alcohols, 15-45 wt % of solvating organic additive from row of alkylsulphoxides and alkylamides of linear or cyclic structure, water to 100% - the rest.
EFFECT: increased efficiency of refining.
5 ex, 2 tbl
FIELD: oil and gas production.
SUBSTANCE: here is disclosed method of removal organic sulphur and nitrogen containing compounds from light ends of crude oil consisting in mixing hydroperoxide with light end of crude oil, in producing mixture, in heating it by means of treatment with sound energy, and in centrifugation of said light end of crude oil.
EFFECT: removal of sulphur containing compounds, nitrogen containing compounds and other undesirable components from oil and fuel on base of oil.
9 cl, 3 tbl, 2 dwg
FIELD: petroleum processing.
SUBSTANCE: invention relates to process of treating hydrocarbon stock, in particular to reducing nitrogen level in liquid hydrocarbon stock. Process is characterized by that (a) liquid hydrocarbon stock containing alkylation agent and organonitrogen compounds is brought into contact with acid catalyst at elevated temperature in a first reaction zone to form liquid hydrocarbon stock with reduced content of alkylation agent and organonitrogen compounds having elevated boiling temperatures; and (b) liquid hydrocarbon stock with reduced content of alkylation agent and containing organonitrogen compounds with elevated boiling temperatures is fractioned to remove said organonitrogen compounds.
EFFECT: enabled production of liquid hydrocarbon stock with reduced content of alkylation agent and reduced nitrogen level.
14 cl, 3 dwg
FIELD: oil-and-gas production.
SUBSTANCE: invention related to a method of calcium content decrease in fluid hydrocarbon medium, which includes contacting of mentioned above fluid hydrocarbon medium with a sequestrant, represented with a carboxylic acid for calcium containing separating complex formation, b. contacting of mentioned above fluid hydrocarbon medium with water medium for emulsion formation, in which after the mentioned above emulsion separation, at least part of the mentioned separated calcium containing complex stays in the water medium, and contacting the mentioned water medium with water soluble or water dispersing polymer, with I formula for the calcium disposals inhibition on surfaces, contacting with the mentioned above water medium, where the polymer has: (I) formula, where E - is a repeating fragment, which remains after non-saturated ethylene type compound polymerization, R1 is a hydrogen atom or the lowest (C1-C6)- alkyl or carbonyl, Q - is O or NH, R2 - is the lowest (C1-C6)-alkyl, hydroxy - substituted the lowest (C1-C6)-alkyl, the lowest (C1-C6)-alkyl sulfonic acid -(Et-O)-n, -(iPr-O)-n or -(Pr-O-)n, where n - is a variable from around 1 up to 100, and R3 - is a hydrogen atom or XZ, where X - is anion radical, selected form a group, consisting from SO3, PO3 or COO, Z - is hydrogen atom or atoms or any other water soluble cationic fragment, which serves is a balance in X anion radical valence; F - when presented, is a repeating fragment with a II: formula, where X and Z are the sane as in I formula, R4 - is a hydrogen atom or (C1-C6) the lowest alkyl, R5 - is hydroxy - substituted alkyl or alkylene, which has from 1 to 6 atoms, and XZ can or can not to be presented, c and d - are positive whole numbers, e is not-negative number, and j is equal to 0 or 1.
EFFECT: calcium disposal decrease on a surfaces contacting with water phase water in oil separated emulsion.
21 cl, 7 ex, 7 tbl
SUBSTANCE: invention relates to a method of producing base oil with low content of sulphur, ecologically clean aromatic filler materials and caoutchouc and rubber plasticisers, involving selective purification of petroleum oil fractions with a selective solvent, separation of the first step extract and raffinate solutions, wherein the first step extract solution is cooled with subsequent separation a first step pseudo-raffinate solution in the settling tank, and after solvent regeneration, the first step raffinate solution is dewaxed and oxidised with subsequent extraction of the oxidised dewaxed oil to obtain second step raffinate and extract solutions; after solvent regeneration and subsequent adsorption or hydrofining, group II base oil with low sulphur content is obtained from the second step raffinate solution, wherein the second step extract solution is mixed with the first step pseudo-raffinate solution to obtain, after solvent regeneration, ecologically clean aromatic filler and a caoutchouc and rubber plasticiser with less than 2.9% content of polyaromatic hydrocarbons (PAH).
EFFECT: obtaining base oil with negligible sulphur content.
3 cl, 3 tbl, 3 dwg
FIELD: oil and gas production.
SUBSTANCE: invention relates to stabilisation of gas-saturated oil. Proposed method comprises two-stage separation at 20-80°C with separation of gas at 1st separation stage at 0.11-0.16 MPa. It comprises also separation of degassed oil at 2nd separation stage at 0.01-0.06 MPa to obtain separated oil and gas. Separated gas is sucked off by degassing device, for example, ejector operated on associated gas from oil field separation stage. Here, extracted gas is mixed with 1st separation stage gas. Produced gas mix is cut in stable condensate and dry gas. Then, stable condensate is mixed with separated oil to feed stabilised oil and dry gas to consuming equipment.
EFFECT: higher yield of separator oil.
3 ex, 1 tbl