Method of obtaining low-viscous white oils

FIELD: chemistry.

SUBSTANCE: invention relates to a method of obtaining low-viscous white oils, in which vacuum gasoil is subjected to hydrocracking with the volume ratio of hydrogen to a raw material of 800-1000 nm3/m3, volume rate of the raw material supply of 0.4-0.6 h-1, temperature of 340-360°C and partial pressure of hydrogen of 20-30 MPa on Ni/Mo catalyst, applied on a silica-alumina carrier, with the content of active components counted per the catalyst burnt at a temperature of 600°C, wt %: MoO3 - 35.0, NiO - 15.0, SiO2 - 7.0 or on Ni/W catalyst, applied on the silica-alumina carrier, with the content of active components counter per the catalyst burnt at a temperature of 600°C, wt %: WO3 - 25.0, NiO - 10.0, SiO2 - 5.0. The target fraction with the boiling out temperature from 280 to 340°C, the content of aromatic hydrocarbons above the required norm and the temperature of solidification not higher than minus 10°C is separated from the obtained stream, boiling out in the range of temperatures from 280 to 400°C. Hydration of the target fraction is carried out by its contact with hydrogen with the volume ratio of hydrogen to the raw material of 800-950 nm3/m3 on the catalyst at a temperature of 240-320°C, partial pressure of hydrogen of 6.0-8.0 MPa, volume rate of the raw material supply 0.25-0.5 h-1.

EFFECT: reduction of the technological process of obtaining white oils for the medical purpose.

4 cl, 1 tbl, 5 ex

 

The invention relates to the field of refining and petrochemistry, particularly to a method for producing white oils for use in medicine and veterinary medicine, for example as oil adjuvant in the manufacture of vaccines against foot and mouth disease, glanders and other diseases of large and small livestock.

Mineral white oils are highly refined transparent distillate fractions of hydrocarbons with a very low content of toxic polycyclic aromatic compounds, heavy metals, sulfur - and nitrogen-containing compounds or their complete absence. They have increased stability compared with most mineral, chemical and vegetable products and have exceptional chemical inertness.

There are two types of white oils: technical and medical. One of the most important technical indicators of white oils is the percentage distribution of hydrocarbons - aromatic (CA), naphthenic (CN), paraffin (CP). Special attention is paid to the content of aromatic hydrocarbons (SA) due to their high toxicity: technical white oil content of the SA should not exceed 7.0 percent; for medical white oil content of the SA should not exceed 0.5%, to certain types of oils used more stringent requirement on the content of CA, namely, to complete their OTS�accordance.

White oils are of great industrial importance, but the process of their manufacture is one of the most expensive in oil refining.

Current technology for the production of white oils include various combinations gidroliticheskikh processes, such as hydrocracking, Hydrotreating, hydrogoethite (hydrofinishing), hydrogenation, catalytic dewaxing, isodeparaffinization, isomerization. Hydrocracking is a process of refinement to improve the viscosity index and reduce the content of unsaturated hydrocarbons, including aromatic. Hydroforming, especially soft hydroforming, known as hydrofinishing or hydrogenation, can be used to stabilize the oil against oxidation by saturating the aromatics and olefins, the removal of sulfur and nitrogen and destruction of coloured substances. Catalytic dewaxing can be used to remove paraffin and improves appearance and low-temperature properties of lubricating oil.

The best option of these processes is selected according to many factors, mainly on the quality of raw materials, product requirements and the specific requirements of the process. In General, the cleaning stage to increase the viscosity index and UD�tion of sulfur and nitrogen from petroleum precede stages of hydroforming and dewaxing. In many cases, it is desirable that phase hydrofining followed the stages of cleaning and dewaxing to remove or hydrate unstable molecules that could be formed at other stages of the process. Dehydrogenization processes, such as solvent extraction, are also widely used for oil refining raw materials.

In GB 1310320 A, 21.03.1973 a method for producing white oils, which paravenously distillate lubricating oil is subjected to interaction with a catalyst comprising a Nickel/molybdenum, in the presence of hydrogen at a temperature of 371°C, followed an instant evaporation for removal of gaseous products, with the subsequent second area where the first liquid fraction is subjected to interaction at a temperature of 399°C with a catalyst comprising a platinum soda, silica-alumina-crystalline aluminosilicate extrudate, and further subjected to interaction at a temperature of 290°C with a catalyst containing platinum or aluminum oxide.

In the patent EA 000717 B1, 28.02.2000 a method for producing a basic lubricating oils, technical white oils, which includes stages: the interaction of the source hydrocarbon oils in the presence of hydrogen in a first reaction zone with a catalyst comprising at least one metal component�and VI groups and at least one component of non-noble metal of group VIII, deposited on a refractory oxide substrate; separating the effluent at elevated pressure gaseous fraction and a liquid fraction having a sulfur content less than 1,000 parts per million by weight (ppm) and nitrogen content less than 50 ppm; the interaction of the liquid fraction in the presence of hydrogen in a second reaction zone with at least a catalyst comprising a noble metal component deposited on an amorphous refractory oxide substrate; and definition of the main lubricating oil having a viscosity index of at least 80.

In the patent EA 001407 B1, 26.02.2001 a method for producing a technical or food white oil, the refining of lubricating oil, comprising contacting a base lubricating oil fraction and hydrogen under the reaction conditions of hydrofining in the reaction zone of a hydrofining catalyst comprising a platinum-palladium alloy and an oxide matrix of aluminum oxide, silicon dioxide or combinations thereof, where the molar ratio of platinum to palladium is from 2.5:1 to 1:2.5 and the base lubricating oil fraction has a boiling interval in the range of temperatures from 316 to 566°C and a viscosity index of at least 90.

However, the described methods do not allow to obtain a white oil with a content of aromatic hydrocarbons of not more than 0.5 wt.%.

The closest to savenamespace make white oils is a process for the production of white oils, described in US 2009/0166251 A1, 07.02.2009. The main stages of the process according to the first embodiment include: 1) two-stage Hydrotreating of hydrocarbons; 2) separation of ammonia and hydrogen sulfide from the hydrotreated product; 3) catalytic deparaffinization received hydrotreated product; (4) removal of residual quantities of ammonia, hydrogen sulfide and light ends from the dewaxing product; 5) the separation of the dewaxed product; 6) two-stage hydrogoethite dewaxed feedstock selective solvents.

The second variant of the method of producing white medical oils include: 1) Hydrotreating a hydrocarbon feedstock; (2) the hydrocracking product of the Hydrotreating; 3) the removal of ammonia and hydrogen sulfide from the products of hydrocracking; 4) catalytic dewaxing of the product of hydrocracking; 5) hydrogoethite products dewaxing; 6) fractionation of the product of the first stage of hydrogoethite obtaining: light fractions, the first of the chase medical white oils, base oils and technical white oils; 7) hydrogoethite first epaulet medical white oils.

The main disadvantages of these options make white oils is a multistage and a low yield of white oils for medical purposes.

The technical object of the present invention is to provide a method of obtaining white�x oils for medical purposes with a smaller number of stages and high output.

The technical result from implementation of the proposed invention is the reduction of technological process of production of white oils for medical purposes, including vaccine oil, ensuring the achievement of the kinematic viscosity at 40°C from 5 to 12.5 mm2/s, the aromatic hydrocarbon content of from 0.1 to 0.5 wt.%.

The technical result is achieved in that the method comprises hydrocracking of vacuum gas oil at a volume ratio of hydrogen to feedstock of 800-1000 nm3/m3, the volumetric feed rate of 0.4 to 0.6 h-1the temperature of 340-360°C and partial hydrogen pressure of 20-30 MPa for the Ni/Mo catalyst deposited on silica-alumina carrier, the content of active components on calcined at a temperature of 600°C the catalyst, wt.%: MoO3- 35,0, NiO - 15,0, SiO2- 7,0 or Ni/W catalyst deposited on silica-alumina carrier, the content of active components on calcined at a temperature of 600°C the catalyst, wt.%: WO3- 25,0, NiO And 10.0, SiO2- 5.0 receiving stream boiling in the temperature range from 280 to 400°C, the separation from the stream of the target fraction with a final boiling point of from 280 to 340°C, the aromatic hydrocarbon content is above the required rate and a pour point not higher than minus 10°C and subsequent hydrogenation of the target fraction �UTEM its contacting with hydrogen at a volume ratio of hydrogen to raw 800-950 nm 3/m3on the catalyst at a temperature of 240-320°C, partial pressure of hydrogen of 6.0-8.0 MPa, the volumetric feed rate of 0.25 to 0.5 h-1.

For carrying out the process of hydrogenation catalyst used: nyelinyeinaya catalyst modified with tungsten deposited on a silica-alumina carrier with a mass fraction of components on calcined at 650°C the catalyst, wt.%: MoO3- 15,2, NiO - 4,5, WO3- 2.4 GHz; sulfatirovnie platinum catalyst deposited on alumina with a platinum content on calcined at 850°C, the catalyst is 0.15 wt.% or palladium catalyst deposited on alumina with palladium on calcined at a temperature of 600°C, the catalyst was 1.0 wt%.

The obtained target product is a white oil with a kinematic viscosity at 40°C from 5 to 12.5 mm2and the aromatic hydrocarbon content of from 0.1 to 0.5 wt.%. White oil analyze the content of aromatic hydrocarbons using gas chromatography or gas chromatography together with mass spectrometry.

The invention is further illustrated by examples, not limiting its scope.

Example 1

Vacuum gas oil having the characteristics presented in table 1, the vertical�contribute to the hydrocracking.

The hydrocracking is carried out at a temperature of 350°C, the partial hydrogen pressure of 25 MPa, volume ratio of hydrogen to raw 1000 nm3/m3and the volumetric feed rate of 0.5 h-1. Hydrocracking of vacuum gas oil is carried out on a Ni/Mo catalyst deposited on silica-alumina carrier, the content of active components on calcined at a temperature of 600°C the catalyst, wt.%: MoO3- 35,0, NiO - 15,0, SiO2- 7,0. From the resulting hydrocracking stream with a final boiling point 280-400°C allocate the target fraction with a final boiling point 280-340°C and an aromatic content of 3.7 wt.%.

The target fraction is subjected to hydrogenation at nigelmasonwm the catalyst, modified with tungsten deposited on a silica-alumina carrier with a mass fraction of components on calcined at 650°C the catalyst, wt.%: MoO3- 15,2, NiO - 4,5, WO3- 2.4 GHz.

The hydrogenation is carried out at a temperature of 320°C, the partial hydrogen pressure of 8.0 MPa, the volumetric feed rate of 0.25 h-1, the ratio of hydrogen to raw 900 nm3/m3. The resulting white oil had an aromatics content of 0.5 wt.% and kinematic viscosity at 40°C 5.0 mm2/S.

Example 2

Vacuum gasoil from ha�acteristically, presented in table 1, is subjected to hydrocracking under the conditions described in Example 1 in a volume ratio of hydrogen to feedstock 800 nm3/m3, the volumetric feed rate of 0.4 h-1, a temperature of 340°C and a partial hydrogen pressure of 30 MPa. From the resulting hydrocracking stream with a final boiling point 280-400°C allocate the target fraction with a final boiling point 280-340°C and an aromatic content of 4.4 wt.% and carried out the hydrogenation of the target fraction.

Hydrogenation of the target fraction is carried out at a temperature of 260°C, the partial hydrogen pressure of 7.0 MPa, volumetric feed rate of 0.25 h-1, the ratio of hydrogen to raw 900 nm3/m3. As the hydrogenation catalyst used sulfatirovnie platinum catalyst deposited on alumina, the platinum content on calcined at 850°C, the catalyst is 0.15 wt.%. The resulting white oil had an aromatics content of 0,1 wt.% and kinematic viscosity at 40°C 7.5 mm2/S.

Example 3

Vacuum gas oil with the characteristics presented in table 1, is subjected to hydrocracking under the conditions described in Example 1. From the resulting hydrocracking stream with a final boiling point 280-400°C allocate target fraction with the rate�the boiling temperature 280-340°C and an aromatic content of 4.4 wt.% and carried out the hydrogenation of the target fraction.

Hydrogenation of the target fraction is carried out at a temperature of 260°C, the partial hydrogen pressure of 7.0 MPa, volumetric feed rate of 0.5 h-1, the ratio of hydrogen to raw 900 nm3/m3. As the hydrogenation catalyst used sulfatirovnie platinum catalyst deposited on alumina, the platinum content on calcined at 850°C, the catalyst is 0.15 wt.%. The resulting white oil had an aromatics content of 0.3 wt.% and kinematic viscosity at 40°C 7.5 mm2/S.

Example 4

Vacuum gas oil is subjected to hydrocracking at a temperature of 350°C, the partial hydrogen pressure of 25 MPa, volume ratio of hydrogen to raw 1000 nm3/m3and the volumetric feed rate of 0.5 h-1. Hydrocracking of vacuum gas oil is carried out on Ni/W catalyst deposited on silica-alumina carrier, the content of active components on calcined at a temperature of 600°C the catalyst, wt.%: WO3- 25,0, NiO and 10.0. SiO2To 5.0.

From the resulting hydrocracking stream with a final boiling point 280-400°C allocate the target fraction with a final boiling point 280-340°C and an aromatic content of 3.5 wt.%. Hydrogenation of the target fraction is carried out at a temperature of 240°C, partial pressure vodorod,0 MPa, the volumetric feed rate of 0.25 h-1, the ratio of hydrogen to raw 900 nm3/m3. As catalytic hydrogenation using palladium deposited on alumina, palladium on calcined at 850°C the catalyst was 1.0 wt.%. The resulting white oil had an aromatics content of 0.2 wt.% and kinematic viscosity at 40°C 10,0 mm2/S.

Example 5

Crude oil, which is used as a gas oil having the characteristics indicated in Table 1, is subjected to hydrocracking under the conditions described in example 1. Then the stream from stage hydrocracking with a final boiling point 280-400°C fractionary with separation of the target fraction with the boiling temperature 320-340°C, containing aromatic hydrocarbons of 2.8 wt.%. The target fraction is hydrogenated at a temperature of 240°C, the partial hydrogen pressure of 7.0 MPa, volumetric feed rate of 0.5 h-1, the ratio of hydrogen to raw 900 nm3/m3. As catalytic hydrogenation using palladium deposited on alumina, palladium on calcined at 850°C the catalyst was 1.0 wt.%. The resulting white oil had an aromatics content of 0,1 wt.% and kinematic viscosity at 40°C 12.5 mm2 /S.

1. A method of producing low-viscosity white oils comprising hydrocracking of vacuum gas oil at a volume ratio of hydrogen to feedstock of 800-1000 nm3/m3, the volumetric feed rate of 0.4 to 0.6 h-1the temperature of 340-360°C and partial hydrogen pressure of 20-30 MPa for the Ni/Mo catalyst deposited on silica-alumina carrier, the content of active components on calcined at a temperature of 600°C the catalyst, wt.%: MoO3- 35,0, NiO - 15,0, SiO2- 7,0 or Ni/W catalyst deposited on silica-alumina carrier, the content of active components on calcined at a temperature of 600°C the catalyst, wt.%: WO3- 25,0, NiO And 10.0, SiO2- 5.0 receiving stream boiling in the temperature range from 280 to 400°C, the separation from the stream of the target fraction with a final boiling point of from 280 to 340°C, the aromatic hydrocarbon content is above the required rate and a pour point not higher than minus 10°C and subsequent hydrogenation of the target fraction by contacting with hydrogen at a volume ratio of hydrogen to raw 800-950 nm3/m3on the catalyst at a temperature of 240-320°C, partial pressure of hydrogen of 6.0-8.0 MPa, the volumetric feed rate of 0.25 to 0.5 h-1.

2. A method according to claim 1, characterized in that the hydrogenation lead to nigelmasonwm the catalyst, a modified wolf�am, deposited on a silica-alumina carrier with a mass fraction of components on calcined at 650°C the catalyst, wt.%: MoO3- 15,2, NiO - 4,5, WO3- 2.4 GHz.

3. A method according to claim 1, characterized in that the hydrogenation lead to sulfatirovnie platinum catalyst deposited on alumina, the platinum content on calcined at 850°C, the catalyst is 0.15 wt%.

4. A method according to claim 1, characterized in that the hydrogenation lead to a palladium catalyst deposited on alumina with palladium on calcined at a temperature of 600°C catalyst - 1.0 wt.%.



 

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11 cl, 1 dwg, 4 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: invention is related to a combined method of conversion of oil-derived hydrocarbon fractions into high-quality hydrocarbon mixtures as fuel, which includes catalytic cracking of hydrocarbon fraction in catalyst fluidised bed with catalyst containing ERS-10 zeolite, where the specified catalyst contains at least two components, where the specified components represent: (a) a component containing one or more catalytic cracking catalysts in fluidised, and (b) a component containing ERS-10 zeolite for obtaining Light Cycle Gas Oil (LCGO), hydrotreatment of light cycle gas oil, interaction of hydrotreated light cycle gas oil obtained at the previous stage of hydrotreatment in presence of hydrogen with catalytic system. The invention also touches the method of catalytic cracking and a stage of catalytic cracking in fluidised bed.

EFFECT: production of high-quality hydrocarbons, conversion increase.

21 cl, 3 tbl, 1 ex

FIELD: machine building.

SUBSTANCE: invention relates to the hydroconversion method for raw hydrocarbons in the mix with the circulating part of the hydroconversion vacuum residue by a high-aromatic modifier, dispersion of a catalyst precursor and hydrogen-containing gas which is supplied in the amount of maximum 800 nm3 per 1 m3 of raw material in terms of hydrogen and of minimum the value of chemical hydrogen demand. The above is carried out in a reactor with an internal circular baffle plate which adjoins the reactor top in a pressure tight way and forms axial and circular cavities, and with separation space at the top of the circular cavity. Hydroconversion gas is removed from the separation space, liquid hydroconversion product is removed from the top of the axial cavity, circulating reaction mass is removed from the bottom of the reactor's circular cavity, cooled and delivered for mixing with heated raw liquid-vapour mixture, the temperature of the liquid hydroconversion product is kept close to the upper limit of the hydroconversion temperature range, the temperature of the heated raw mixture and the temperature of the circulating reaction mass are kept close to the lower limit of the hydroconversion temperature range. Hydroconversion products are separated and rectified to isolate light fractions, heavy gas oil and vacuum residue, part of the latter is recirculated, and the balance part is recovered to produce regenerated catalyst precursor.

EFFECT: reduction of power inputs and metal consumption of equipment along with the provision for high yield of light fractions.

1 dwg, 1 ex

FIELD: engines and pumps.

SUBSTANCE: invention relates to production of fuel for jet engines from kerosene stock. Proposed method comprises hydrofining of kerosene stock with freezing point interval of 163-302°C (325-575°F) over hydrofining catalyst under conditions of hydrofining. This allows getting hydrofined kerosene stock. Besides, it includes dewaxing of, in fact, all hydrofined kerosene stock over catalyst including 1-D molecular sieve with ten rings under conditions of dewaxing to get water-dewaxed kerosene stock. Also, it includes fractionating of water-dewaxed kerosene stock to get fuel for jet engines.

EFFECT: higher yield, better properties.

10 cl, 1 dwg, 2 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: initial hydrocarbon raw material is initially separated and first part of initial raw material is introduced into first zone of dehydration reaction, which functions without oxidation re-heating, and obtained as a result output flow is introduced into second zone of dehydration reaction, which functions without oxidation re-heating. Obtained as a result output flow from second zone of dehydration reaction, together with second part of initial raw material is introduced into third zone of dehydration reaction, which functions with oxidation re-heating.

EFFECT: increased method productivity.

10 cl, 1 dwg

FIELD: by-product-coking industry.

SUBSTANCE: claimed method includes hydrofining of by-product-coke resin with subsequent hydrodealkylation. In hydrofining step hydrogen donators such as naphthalene, anthracene, and phenanthrene hydro- or alkyl-derivatives, containing in coal-far resin, are obtained. Dealkylation is carried out using the said hydrogen donators. Quantitative content of hydrogen donators is equal the same of benzene, naphthalene, alkyl-derivatives, and other hydrodealkylated compounds (15-30 wt.% as calculated to raw material). Hydrofining is carried out under hydrogen pressure of 2-5 MPa, at 280-4000C, feed space velocity of 0.5-2 h-1, in hydrogen/feed ratio of 500-1000 l/kg in flowing system.

EFFECT: finished product of improved quality.

4 cl, 2 tbl, 2 ex

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