Method of producing liquid hydrocarbon mixtures by hydroconversion of lignocellulose biomass

FIELD: chemistry.

SUBSTANCE: method of producing liquid hydrocarbon mixtures is carried out via hydroconversion of lignocellulose biomass in a solvent medium in the presence of a dispersed catalyst precursor. The method includes drying the biomass; grinding the biomass; preparing a paste from the ground biomass, solvent and dispersed catalyst precursor; hydroconversion of the prepared paste; separating the obtained products in a system of separators; the method is characterised by that the solvent used is an organic solvent having viscosity of 0.5-2.5 Pa·s at 60-90°C, which contains 2-5.5 wt % sulphur and 5-25 wt % polycyclic aromatic hydrocarbons and/or derivatives thereof, and grinding of the biomass and preparation of said paste is carried out via dispersion with mechanical activation of the biomass in a solvent medium containing a catalyst precursor, wherein the prepared paste is first heated in an inert atmosphere to temperature of 330-380°C and pressure of 0.2-0.5 MPa until removal of the basic amount of oxygen in the biomass in the form of CO, CO2 and H2O, followed by hydroconversion.

EFFECT: high output of liquid products of hydroconversion of the biomass, higher conversion of the biomass and simpler process.

10 cl, 10 tbl, 2 dwg, 7 ex

 

The present invention relates to technology for production of liquid hydrocarbon mixtures that are intended for further processing into fuels and chemical products from solid carbonaceous materials, namely, plant lignocellulosic biomass, including waste wood, algae and other vegetable materials, waste paper production, etc., using the process of hydroconversion in the environment of the hydrocarbon diluent (solvent) and the precursor of ultradispersed catalysts. In the last few years there has been an increased interest in obtaining liquid hydrocarbons from renewable feedstocks, which could partially replace or Supplement the fuel derived from petroleum. One of the possible sources of hydrocarbon production is the processing of lignocellulosic biomass. Lignocellulosic biomass or a cellulosic biomass consists of three major biopolymers: cellulose, hemicellulose and lignin. Depending on the nature of the biomass ratio of components may vary. The substance of the biomass has a high content of oxygen - up to 50%. In the process of production of fuels from biomass is necessary to reduce the oxygen content and increase the ratio N/S. There are different methods of conversion of biomass. Gasification biome�ssy obtained synthesis gas, which can be used for the production of liquid fuels technology Fischer-Tropsch. Other methods of liquefaction of biomass are high-speed pyrolysis or hydrothermal treatment in the presence or without a catalyst, but without the addition of hydrogen.

These methods allow you to remove only a portion of oxygen. The resulting liquid products are unstable, oxygen-rich and complex physico-chemical properties are very different from the distillate products of petroleum origin and require further processing. In addition, these purely thermal processes have, in fact, a very poor selectivity; reaction are accompanied by a significant formation of gas and solid particles of coke.

A more effective solution to the problem of recycling is to use a catalytic process of hydroconversion in the presence of hydrogen and a diluent (solvent).

The known method of hydroconversion suspension of chopped biomass in the petroleum refining products, comprising at least 80% of the fraction boiling above 343°C and containing 10-50% of aromatic hydrocarbons. The hydro conversion is carried out at 350-500°C and a pressure of 8.0 is 16.8 MPa in the presence of a suspension of particles of catalyst based on metal sulfide (application WO No. 2009/146225 A1, publ. 03.12.2009, IPC C10G 45/04; SS 3/02).

The disadvantage of the invention JW�makes the the heating of the slurry of the biomass to a temperature of hydroconversion is held in contact with hydrogen, resulting in a significant number (25 - 30% by weight of biomass) of ballast gases CO and CO2are mixed with hydrogen and dilute it, reducing its partial pressure. This leads to a reduction of the depth of conversion, the need to use high pressure when hydroconversion and greatly complicates and increases the cost of the cleaning process recycled hydrogen-containing gas.

In another invention of the solid biomass or liquid products (e.g., resin pyrolysis oils extracted from algae, etc.) is subjected to hydroconversion in the presence of a suspension of sulfides of metals. For the formation of metal sulfide precursor pre-sulfydryl in the presence sliderules agent in a separate apparatus in an atmosphere of hydrogen at T=250-350°C with obtaining a suspension of the catalyst in the liquid product. As a medium for suspension of the catalyst, pyrolysis tar, oils derived from biomass, light oil, etc. as precursors used water or oil-soluble compounds of the elements 6 and 8 groups of the periodic system of elements. As sliderui agents use hydrogen sulfide, organic sulfides, such as DMDS (dimethyldi�elfid), polysulfides, elemental sulfur, sodium sulfide, thiophene, and so on. The average particle size of the catalyst is preferably less than 20 microns (application U.S. No. 2009326285 A1, published on 31.12.2009, IPC SS 1/00). The disadvantage of the invention is the complexity of the process and the use of additional sliderules agent.

The closest analogue (prototype) of the present invention is a method of hydroconversion of biomass in the reactor in the presence of a dispersed catalyst (French patent No. 2974109 A1, published on 19.10.2012, IPC C10 IN 53/02; C10G 1/00; C10L 1/04). The distinguishing feature of the invention is thermal treatment of biomass at a temperature of from 200 to 300°C, preferably between 225°C and 275°C, in the absence of air. The thus treated biomass is ground to a preferred particle size less than 150 microns. For the process of hydroconversion powdered biomass is mixed with the solvent. As the solvent for hydroconversion use leftovers of refined oil, crude oil, heavy oil, asphalt deasphalting, products hydroconversion biomass, coal, industrial polymers, etc. the hydro conversion is carried out at a temperature of 300-450°C, total pressure 2-35 MPa, the flow rate of the raw material is 0.1-5 h-1, the ratio of hydrogen/feedstock from 0.1 to 2 nm3/kg, in the presence of dispersed catalysts on the basis of sulfi�s Mo, Fe, Ni, W, Co, V, Ru. The dispersed catalyst is prepared in a special autoclave from precursor - salts of metals (molybdenum, Nickel, etc.) with the addition of sliderules agent, for example DMDS. As catalysts may also be used a catalyst with grain sizes less than 1 mm. Products hydroconversion separated into gas, naphtha, kerosene, diesel oil fraction, a vacuum gas oil and heavy residue containing the catalyst particles. Part of the distillate products can be used for preparing a slurry of the biomass. According to one of embodiments of the invention, the recycled fraction is subjected hydrotreated. In addition, the patent provides for partial recirculation of the residue containing the catalyst particles. Output from the process a portion of the residue containing the solid catalyst, is used to obtain precursor by known methods of combustion, separation extractants and methods.

The disadvantages of the prototype are as follows:

- low temperature thermal pre-treatment of biomass. At the stated temperature (300°C) processes of decarbonylation (removal of carbonyl groups of substances biomass), decarboxylation (removal of carboxyl groups) and hydrodeoxygenation (removal of hydroxyl groups) occur in a small degree. In PR�maintained example as a result of thermal treatment of beech wood, the oxygen content in the sample decreased slightly from 41.5 to 38.1%. In the process of hydroconversion carried out at a higher temperature, the process further decarbonylation and decarboxylation will be the sources of large quantities of carbon oxides and water. As a result, in the gas phase will be supplied WITH and CO2that will reduce the partial pressure of hydrogen and create difficulties in the purification of recycled hydrogen-containing gas. As a result, decreases the depth of conversion and significantly complicates the technology of concentration of hydrogen;

- in this method, the dispersed catalyst is prepared in a special autoclave from precursor - salts of metals (molybdenum, Nickel, etc.) with the addition of sliderules agent, for example DMDS, which greatly complicates the process of hydroconversion;

- the disadvantage of this process is the low yield of liquid products is 24-32% and high output gas - 66,8-73.9% of the biomass substance.

Objects of the invention is to increase the yield of liquid products and to simplify the process, increase the depth conversion of biomass.

To solve the problem in the method of producing a liquid hydrocarbon mixtures through hydroconversion lignocellulosic biomass, comprising drying the biomass, its grinding, cooking pasta from the crushed biomass, solvent and precursor dispersed catalyst, hydroconversion paste separation of the products obtained in the system of separators, used as a solvent an organic solvent having in the temperature range 60-90°C a viscosity of from 0.5 to 2.5 PA·s, containing 2-5,5% wt. sulfur and 5-25 wt%. polycyclic aromatic hydrocarbons and/or their derivatives, and grinding of biomass and the specified cooking pasta is carried out by dispersing with mechanical activation of the biomass in a solvent containing the catalyst precursor. In this pre-heating is carried out cooked pasta in an inert atmosphere to a temperature of 330-380°C at a pressure of 0.2-0.5 MPa to remove the main quantity of oxygen biomass in the form of CO, CO2and H2O followed by hydro conversion.

The solvent containing the catalyst precursor can be obtained by mixing and dispersing with mechanical activation of an aqueous solution of catalyst precursor containing one or more water-soluble compounds of elements selected from Mo, Fe, Ni, W, Co, with an organic solvent to obtain an emulsion with a droplet size of from 0.1 to 3 μm. Dispersing with mechanical activation of the aqueous catalyst precursor with an organic solvent is preferably carried out in a rotary cavitation disperser.

The solvent containing the catalyst precursor, can also get predvaritelnyye in an organic solvent oil-soluble catalyst precursor, containing one or more compounds of elements selected from Mo, Fe, Ni, W, Co.

Dispersing with mechanical activation of the biomass in a solvent containing a precursor of the catalyst is carried in retrocessional disperser. Preferably it is carried out at 70-120°C.

The mass ratio of biomass to solvent and precursor of the catalyst in cooked pasta is(0,1-0,7):1:(0,005-0,1).

After this heating deoxygenating paste mix heated to 400-450°C with hydrogen at a ratio of hydrogen: pasta = (500-1500): 1 nl/l, and the hydro conversion is carried out at a pressure of 5 to 9 MPa, a temperature of 400-450°C, the dwell time of the feedstock in the reaction zone (contact time) of 0.33 - 2 hours, in the presence of the formed catalyst precursor is one or more sulphides of elements selected from Mo, Fe, Ni, W, Co, with a particle size of 10-1000 nm.

Preferably the ratio of hydrogen/paste is (800-1100):1 nl/L.

The main differences of the proposed solution from the prototype are as follows:

- synthesis of dispersed particles of the catalyst from the precursor is carried out in a separate block, in a special apparatus, and directly into the raw material mixture, in the process of heating to a temperature of hydroconversion and without IP-

use special sliderui agents;

- grinding of biomass is carried out by iediterranean in a solvent with a specific set of physico-chemical properties, with the use of mechanical activation processes, allowing to obtain highly dispersed active fragments of polymer molecules of lignin, cellulose and hemicellulose;

- for the purpose of increasing the partial pressure of hydrogen in the gas phase reactor hydroconversion, lower grades of ballast gases (CO and CO2in recirculating hydrogen-containing gas, simplification of purification technology of circulating hydrogen-containing gas are pre-dioxygenase heat treatment (heating) paste at 330-380°C, preferably 340-360°C.

A diagram of the process shown in Fig.1.

According to one of the embodiments of the invention the aqueous solution of catalyst precursor (2) containing one or more salts of elements selected from Mo, Fe, Ni, W, Co, mixed and dispersed with mechanical activation using a device (14) at a temperature of 60-90°C, preferably 75-85°C, in an organic solvent (1).

In another embodiment of the invention as a precursor using oil-soluble compounds of elements selected from Mo, Fe, Ni, W, Co, which is dissolved in a solvent with the use of the device 14. The mass ratio of solvent and precursor of the catalyst is 1:(0,005-0,1), preferably of 1:(0,01-0,05). As the liquid medium for the preparation of a dispersion of the precursor used�comfort organic solvents, contains 2-5,5% sulfur, 5 to 25% of polycyclic aromatic hydrocarbons (PAHs) or alkyl derivatives of PAHs.

The presence of sulfur-containing compounds in the composition of the solvent provides the during of dispersed catalysts by heating the paste to a temperature of hydroconversion. Polycyclic aromatics in the temperature range 350-400°C in the presence of sulfide dispersed catalysts hereroense education gidroproizvodnam, which in turn hydrogen donors in relation to the fragments of polymer molecules of the biomass. For maximum catalytic activity synthesized from a precursor of a highly dispersed catalyst, the viscosity of the solvent in the temperature range 60-90°C should be from 0.5 to 2.5 PA·s.

To the resulting dispersion containing the precursor of the catalyst, add biomass (3). The mass ratio of biomass to solvent and precursor of the catalyst is(0,1-0,7):1:(0,005-0,1), preferably(0,4-0,55):1:(0,01-0,05). Biomass is subjected to mechanical activation and dispersing in a solvent containing a catalyst precursor, in the device (15) at a temperature of 60-90°C, preferably 75-85°C. the mechanical Activation of the substance of the biomass is carried out without access of air. For this process, suitable dispersing agents, disintegrators and other equipment, allowing to obtain paste diametre solid particles less than 30 microns, but preferred a rotary cavitation disperser.

The particle size of the biomass after mechanical activation is less than 30 μm, including the content of fraction with a diameter of 7 μm is not less than 40%.

As a result of mechanical activation of polymer molecules of the components of biomass formation of active radicals having high reactivity. In the homogenization process, the precursor is partially sorbed by the biomass substance, forming a surface complex compounds, which further increases its reactivity.

To remove the main quantity of oxygen from the biomass substances cooked pasta (4) heated to a temperature of 330-380°C, preferably up to 340-360°C with receiving stream (5), in a tubular furnace (16). This temperature provides the best conditions for removal of oxygen from a substance of the biomass. The resulting gas (7) containing CO, CO2, methane, ethane, water vapor is separated from the liquid product in the separator (17) at a pressure of 0.2-0.5 MPa. Next, a liquid product (6) with a temperature of 330-380°C is mixed with preheated hydrogen (8). It can add the recirculating gas, also containing hydrogen (13). Further, the gas-liquid mixture under a pressure of 5 to 9 MPa, preferably 6-8 MPa serves in the oven (18), where it is heated to 400-450°C (stream 9) and then sent to the reactor hydroconversion (19). In the process of heating seriousnes source precursor is subjected to a thermochemical conversion and sulfidized with the formation of particles of catalysts - sulphides of metals with a particle size of from 10 to 1000 nm. The hydro conversion is carried out at a temperature of 400-450°C, a pressure of 5 to 9 MPa, a space velocity of 0.5-3 h-1(which corresponds to a contact time of 0.33-2 hours), the ratio of hydrogen gas/raw meal (500-1500) nl/l of raw pasta. The optimal values of the parameters of hydroconversion are determined by the properties of biomass, solvent and catalyst used.

Products hydroconversion (10) enter the separation unit products (20). The separation of the products is carried out according to the usual separation of the products of hydroconversion of crude oil. As a result of separation of the liquid product (hydrogenate) and a gas containing hydrogen (13). Hydrogenate is subjected to atmospheric and vacuum distillation of obtaining petrol, diesel, gas oil distillate fractions and a residue of a vacuum distillation with a boiling point above 500°C. In the vacuum residue is present ultradispersed catalyst. To reduce the consumption of catalyst per part of residue vacuum distillation (11) return to the process of hydroconversion for mixing with the biomass in the device 15. Another portion of the residue (12) is used for the extraction and regeneration of the precursor in the unit catalyst regeneration (21). The regenerated catalyst precursor (PKK

returns to the site of dispersing the precursor in the solvent in devices� D1.

The technical result of the invention are as follows:

- increase the yield of liquid products of hydroconversion biomass as a result of using the method of mechanical activation in a solvent, the use of solvent with an optimal set of physico-chemical properties, the interaction of the precursor with the surface of the particles of biomass in the process of cooking pasta, first removing the main quantity of oxygen from a substance of biomass;

- increasing the depth conversion of biomass;

- simplifying the process by eliminating the process of preparing the dispersed sulfide catalyst in a hydrogen atmosphere with the addition of special sliderui agents.

Example 1

The biomass is dried at 110°C pine sawdust particle size of 0.3 mm and a residual moisture content of 5.1 wt%. As a solvent the residue of vacuum distillation of crude tar. The compositions of biomass and solvent shown in table 1. To 100 g heated to 80°C vacuum residue is added 10 g of an aqueous solution of the precursor containing 0,155 g of ammonium paramolybdate rate of 0.05% molybdenum organic mass of pasta. The mass ratio of the solvent and the aqueous solution of the precursor of the catalyst is 1:0,1. The mixture is dispersed by mechanical activation at 80°C for 40 min using a rotary cavitation disperser. In grill�Lenno emulsion droplet sizes are in the range of 0.1-3 microns.

The resulting emulsion was mixed with 70 g of woody biomass. The mixture is dispersed using a rotor-cavitation disperser at 120°C for 40 minutes. The mass ratio of biomass to solvent and an aqueous solution of precursor of the catalyst is 0.7:1:0,1. Fig.2. given the dispersed composition of the biomass particles in the paste before and after dispersion.

10 Moisture content, %
Table 1
Physico-chemical properties of woody biomass and tar
№ p/pIndicatorTarWoody biomass
1Density, kg/m3at 15°C1011903
2.Fractional composition. Boil over in % at temperature:
initial boiling point388-
5502-
519-
20545-
30565-
40577-
3Element composition, %
Carbon83,951*
Hydrogen10,16,4*
Oxygenod42,55*
Nitrogen0,380,05*
Sulfur5,50-
4.Microsocopy residue %17,1 -
5.The ash content at 550°C0,17-
6Dynamic viscosity at 60°C, PA·s2,49-
7Pour point, °C56-
8Group hydrocarbon composition, %
Paraffin-naphthene31.8 mm-
Resin17,6-
Asphaltene5,1-
Aromatic, including:Over 45.5-
polycyclic aromatics and their derivatives25-
9-5,1
* on dry weight

Next, the paste was charged into a heated autoclave equipped with a stirrer, a volume of 1 L. Autoclave was sealed and include blowing with nitrogen at a rate of 2 nl/min under a pressure of 0.2 MPa. The autoclave was heated to 380°C for 1 hour and maintained at this temperature for 30 min under constant duct of nitrogen. Coming out of the autoclave, the gas is cooled in the refrigerator up to 25°C. the Condensed water and gas separated in the separator. Gas analyzed on a chromatograph. As a result of heat treatment of the paste formed 52.6 g of gas, including to 27.7 g of water vapor, including 9.8 g - from the precursor catalyst, 15.2 g CO2, WITH 5.2 g, 4.5 g of hydrocarbons C1-C4. The release of gas on a dry biomass (excluding hygroscopic moisture of the wood and water of the catalyst precursor) was 59.1%. The degree of removal of oxygen from a substance biomass was 96%. Further supplied to the autoclave nitrogen is replaced with hydrogen, heated to 450°C, which constantly serves at a speed of 13.1 nl/min under a pressure of 9 MPa. The autoclave is heated to a temperature of hydroconversion - 450°C and maintained at this temperature for 20 min. contact Time - 0.33 per hour.

The ratio of hydrogen/paste is 1497 nl/l of feedstock. Wijedasa� from the reactor gas-vapor mixture is cooled in a system of separators for the removal of liquid products. Then the autoclave was cooled to room temperature. Stop the flow of hydrogen and unload the autoclave. The residue in the autoclave together with collected in separators distillate fractions. Hydrogenate is subjected to atmospheric and vacuum distillation into fractions of n-K-180°C", "180-350°C, 350-500°C and analyzed. In the residue after distillation determine the size of the particles formed from the precursor catalyst - MoS2. According to electron microscopy the average diameter of catalyst particles ranging from 10 to 1000 nm.

In table.2 and 3 shows the compositions and the product yield of hydroconversion. As the table shows, the yield of liquid organic products from biomass amounted to 38.7%, which is higher than in the known patents. For example, in the prior art, the yield of liquid products was from 23,7% to 32%.

Table 3
The composition and properties of the hydrogenation
Composition of raw materialsBiomass + tarTar
Density at 20°C, kg/m3910933
Iodine number, g/100 g34,8 48,8
Elemental composition, %:
C85,93Of 86.9
H12,111,1
N0,210,2
S0,981,6
O0,780,2

Example 2

To prepare the raw material mixture used 20 g of pre-dried at 110°C pine sawdust with particle size up to 0.3 mm and a residual moisture content of 5.1%. As a solvent the residue of atmospheric distillation of crude oil. The compositions of biomass and solvent are given in table 4.

To 200 g heated to 70°C fuel oil is added 1 g of an aqueous solution of the precursor containing 0.2 g of ammonium paramolybdate rate of 0.05% molybdenum paste. The mass ratio of the solvent and the aqueous solution of the precursor of the catalyst is 1:0,005. The mixture was dispersed at 70°C for 40 min using a rotary cavitation disperser.

In the prepared emulsion droplet sizes are in the range of 0.5-3 μm. The received e�ulsio mixed with 70 g of woody biomass. The mixture is dispersed using a rotor-cavitation disperser at 70°C for 40 minutes. The mass ratio of biomass to solvent and an aqueous solution of precursor of the catalyst is 0.1:1:0,005.

414tr>
Table 4.
Physico-chemical properties of woody biomass and heating oil
№ p/pIndicatorOilWoody biomass
1Density, kg/m3at 15°C0,937903
2.Fractional composition. Boil over in % at temperature:
initial boiling point330-
5348-
10363-
30-
50444-
80502-
3Element composition, %
Carbon85,451*
Hydrogen11,476,4*
Oxygen0,8842,55*
Nitrogen0,150,05*
Sulfur2,1-
4.Microsocopy residue %3,5-
5.The ash content at 550°C0,07-
6Dynamic viscosity at 60°C, PA·s0,52-
7Pour point, °C47-
8Group hydrocarbon composition, %
Paraffin-naphthene53,1-
Resin8,9-
Asphaltenes3,8-
Aromatic, including:34,2-
polycyclic aromatics and their derivatives5-
9Moisture content, %-5,1
* - �and dry weight

Next, the paste was charged into a heated autoclave equipped with a stirrer, a volume of 1 L. Autoclave was sealed and include blowing with nitrogen at a rate of 2 nl/min under a pressure of 0.5 MPa. Next, the autoclave was heated to 330°C for 1 hour and maintained at this temperature for 1 hour at a constant current of nitrogen. Coming out of the autoclave, the gas is cooled in the refrigerator up to 25°C. the Condensed water and gas separated in the separator. Gas analyzed on a chromatograph. As a result of heat treatment of the paste formed 11,84 g gas, including 5.8 g of water vapor, including 0.8 g - of the catalyst precursor, 4,21 g CO2, 0.89 g CO, 0,94 g of hydrocarbons C1-C4. The release of gas on a dry biomass (excluding hygroscopic moisture of the wood and water of the catalyst precursor) 52.8%. The degree of removal of oxygen from a substance biomass was 88%. Further supplied to the autoclave nitrogen is replaced with hydrogen, heated to 450°C, which is constantly fed with a speed of 0.98 nl/min under a pressure of 5 MPa. The autoclave is heated to a temperature of hydroconversion - 400°C and maintained at this temperature for 2 hours. The contact time is 2 hours.

The ratio of hydrogen/paste is 505 nl/l of feedstock. Effluent from the reactor gas-vapor mixture is cooled in a system of separators for the removal of liquid products. Then the autoclave was cooled to room temperature. Exce�asaut the supply of hydrogen and unload the autoclave. The residue in the autoclave together with collected in separators distillate fractions. Hydrogenate is subjected to atmospheric and vacuum distillation into fractions of n-K-170°C", "170-350°C, 350-500°C and analyze. In the residue after distillation determine the size of the particles formed from the precursor catalyst - MoS2. According to electron microscopy, the diameters of the catalyst particles ranging from 10 to 1000 nm. In table.5 and 6 shows the compositions and the product yield of hydroconversion. As the table shows, the yield of liquid organic products from biomass amounted to 35.3%, which is higher than in the known methods. For example, in the prior art, the yield of liquid products was 23.7-32%.

Table 6
The composition and properties of the hydrogenation
Composition of raw materialsBiomass + fuel oilOil
Density at 20°C, kg/m3910906
Iodine number, g/100 g35,9The 38.2
Elemental composition, %:
C86,5386,57
N11,8411,8
N0,10,1
S1,071,21
On0,460,32

Example 3

Raw material as in example 1. The compositions of biomass and solvent shown in table 1.

To 120 g heated to 80°C sludge is added 1.5 g of oil-soluble precursor is molybdenum naphthenate containing 0.09 g of molybdenum rate of 0.05% molybdenum organic mass of pasta. The mass ratio of solvent and precursor of the catalyst is 1:0,0125. The mixture was stirred at 80°C for 20 min using a rotary cavitation disperser.

The resulting solution of the precursor in the sludge is mixed with 60 g of woody biomass. The mixture is dispersed using a rotor-cavitation disperser at 90°C for 40 minutes. The mass ratio of biomass to solvent and precursor of the catalyst is 0.5:1:0,0125.

Next, the paste was charged into a heated autoclave equipped with a stirrer, a volume of 1 L. Autoclave was sealed and include blowing with nitrogen with�orotu 2 nl/min under a pressure of 0.2 MPa. Next, the autoclave was heated to 370°C for 1 hour and maintained at this temperature for 30 min under constant nitrogen flow. Coming out of the autoclave, the gas is cooled in the refrigerator up to 25°C. the Condensed water and gas separated in the separator. Gas analyzed on a chromatograph. As a result of heat treatment of the paste is formed 35,37 g gas, including 14.5 g of water vapor, 12.9 g CO2, 4,32 g CO, 3,65 g of hydrocarbons C1-C4. Gas yield from biomass amounted to 58.9 per cent. The degree of removal of oxygen from a substance of biomass amounted to 94.3%.

Further supplied to the autoclave nitrogen is replaced with hydrogen, heated to 430°C, which always serves with a rate of 3 nl/min under a pressure of 7 MPa. The autoclave is heated to a temperature of hydroconversion - 430°C and maintained at this temperature for 90 min contact Time 1.5 hours.

The ratio of hydrogen/paste is 950 nl/l of feedstock. Effluent from the reactor gas-vapor mixture is cooled in a system of separators for the removal of liquid products. Then the autoclave was cooled to room temperature. Stop the flow of hydrogen and unload the autoclave. The residue in the autoclave together with collected in separators distillate fractions. Hydrogenate is subjected to atmospheric and vacuum distillation into fractions of n-K-170°C", "170-350°C, 350-500°C and analyze. In the residue after distillation determine the size of particles formed from precursor rolled�lit - MoS2. According to electron microscopy, the diameters of the catalyst particles comprise from 10 to 500 nm.

In table.7 and 8 shows the compositions and the product yield of hydroconversion. As the table shows, the yield of liquid organic products from biomass amounted to 38.7%, which is higher than in the known methods. For example, in the prior art, the yield of liquid products was from 23,7% to 32%.

Table 8
The composition and properties of the hydrogenation
The composition and properties of the hydrogenationBiomass + tarTar
Density at 20°C, kg/m3910933
Iodine number, g/100 g34,848,8
Elemental composition, %:
85,93Of 86.9
N12,111,1
N0,21 0,2
S0,981,6
On0,780,2

Examples 4-7

Raw material as in example 1. The compositions of biomass and solvent shown in table 1. Conditions of the experience is identical to that given in experiment 1. In examples 4, 5 and 6 as precursors used 10 g of aqueous solutions containing ferrous sulfate, Nickel sulfate and cobalt sulfate at a rate of 0.1% of the active component (metal) organic mass of pasta. In example 7 as precursor used 10 g of an aqueous solution of ammonium tungstate rate of 0.05% of tungsten in organic mass of paste.

Mixing of components, heat treatment and hydro conversion of the paste was performed analogously as described in example 1.

In table.9 and 10 shows the compositions and the product yield of hydroconversion. As the table shows, the yield of liquid organic products from biomass amounted to 33.8-38.7 per cent, higher than in the known methods. For example, in the prior art, the yield of liquid products was from 23,7% to 32%.

The catalyst precursor
Table 10
The composition and properties of the hydrogenation
Ferrous sulfate (II)Nickel sulfateCobalt sulphateThe ammonium tungstate
Density at 20°C, kg/m3985938949952
Iodine number, g/100 g65,946,451,540,1
Elemental composition, %:
C86,686,0285,7285,81
H10,5811,73Of 11.3411,94
N0,250,180,240,11
S1,190,881,070,83
O1,381,191,631,31

1. A method of producing a liquid hydrocarbon mixtures through hydroconversion lignocellulosic biomass in a solvent in the presence of a precursor of particulate catalyst comprising drying the biomass, its grinding, cooking pasta from the crushed biomass, solvent and precursor dispersed catalyst, the hydro conversion cooked pasta, separation of the products obtained in the system of separators, characterized in that is used as a solvent an organic solvent having in the temperature range 60-90°C a viscosity of from 0.5 to 2.5 PA·s, containing 2-5,5% wt. sulfur and 5-25 wt%. polycyclic aromatic hydrocarbons and/or their derivatives, and grinding of biomass and the specified cooking pasta is carried out by dispersing with mechanical activation of the biomass in a solvent containing a catalyst precursor, wherein the pre-carry out hot cooked pasta in an inert atmosphere to a temperature of 330-380°C at a pressure of 0.2-0.5 MPa to remove the main quantity of oxygen biomass in the form of CO, CO2and H2O followed by hydro conversion.

2. A method according to claim 1, characterized in that the solvent containing the catalyst precursor,�ucaut by mixing and dispersing with mechanical activation of an aqueous solution of catalyst precursor, containing one or more water-soluble compounds of elements selected from Mo, Fe, Ni, W, Co, with an organic solvent to obtain an emulsion with a droplet size of from 0.1 to 3 microns.

3. A method according to claim 2, characterized in that the dispersing with mechanical activation of the aqueous catalyst precursor with an organic solvent is carried out in a rotary cavitation disperser.

4. A method according to claim 1, characterized in that the solvent containing the catalyst precursor, pre-dissolved in an organic
the solvent of the oil-soluble catalyst precursor containing one or more compounds of elements selected from Mo, Fe, Ni, W, Co.

5. A method according to claim 1, characterized in that the dispersing with mechanical activation of the biomass with a solvent containing a precursor of the catalyst is carried in a rotary cavitation disperser.

6. Method according to one of claims. 1-5, characterized in that the dispersing with mechanical activation of the biomass in a solvent containing a precursor of a catalyst, carried out at 70-120°C.

7. Method according to one of claims. 1-5, characterized in that the mass ratio of biomass to solvent and precursor of the catalyst in cooked pasta is(0,1-0,7):1:(0,005-0,1).

8. A method according to claim 6, characterized in that the mass ratio of biomass to solvent and precursor of the catalyst in �prigotovlennoi pasta is(0,1-0,7):1:(0,005-0,1).

9. A method according to claim 1, characterized in that after the specified heating deoxygenating paste mix heated to 400-450°C with hydrogen at a ratio of hydrogen: pasta = (500-1500):1 nl/l, and the hydro conversion is carried out at a pressure of 5 to 9 MPa, a temperature of 400-450°C, the dwell time of the feedstock in the reaction zone of 0.33-2 hours, in the presence of the formed catalyst precursor is one or more sulphides of elements selected from Mo, Fe, Ni, W, Co, with a particle size of 10-1000 nm.

10. A method according to claim 9, characterized in that the ratio of hydrogen/paste is (800-1100):1 nl/L.



 

Same patents:

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: invention relates to method of obtaining basic lubricating oil, including bringing hydropurified raw material and hydrogen-containing gas in contact with catalyst of deparaffinisation under conditions efficient for catalytic deparaffinisation, where combined total content of sulphur in liquid and gaseous formed, supplied to the stage of bringing into contact, constitutes more than 1000 wt ppm with respect to hydropurified raw material. Catalyst of deparaffinisation includes, at least, one zeolite with monosized pores, formed by ten-member rings, at least, one metal of group VIII and, at least, one fire-proof binding agent based on metal oxide with low surface area, and in which catalyst of deparaffinisation has ratio of area of surface of micropores to total surface area equal to 25% or more, where total surface area equals external area of zeolite surface plus area of surface of fire-proof binding agent based on metal oxide.

EFFECT: increased output of deparaffinised lubricating oil.

17 cl, 14 dwg, 7 tbl, 20 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing olefin monomers for producing a polymer. The method is characterised by that it includes the following steps: feeding into a catalyst bed (7) biological oil containing more than 50% tall oil fatty acids and up to 25% tall oil resin acids, as well as hydrogen gas; and catalytic deoxygenation of the oil with hydrogen in the catalyst bed (7); cooling the stream coming out of the catalyst bed (7) and separation thereof into liquid phase (10) containing hydrocarbons and a gaseous phase; and steam cracking (4) of the liquid (13) containing hydrocarbons to form a product containing polymerised olefins.

EFFECT: method provides an industrially applied process, which can be used to convert wood-based raw material to olefin monomers used to produce biological raw material-based polymers.

15 cl, 1 tbl, 6 ex, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: method used for obtaining middle distillates based on the mixture of paraffin hydrocarbons obtained by Fischer-Tropsch synthesis involves the following subsequent stages: a) separation at least of light gas fraction C4-, which has final boiling temperature of less than 20°C, from the flow leaving the Fischer-Tropsch synthesis plant in order to obtain only heavy liquid fraction C5+, which has initial boiling temperature of 20 to 40°C; b) hydrogenation of non-saturated compounds of olefinic type at least of some part of heavy fraction C5+ in presence of hydrogen and hydrogenation catalyst at the temperature of 100 to 180°C, at total pressure of 0.5 to 6 MPa with volumetric hourly velocity of 1 to 10 h-1 and at supply of hydrogen, which corresponds to volumetric "hydrogen/hydrocarbons" ratio of 5 to 80 nl/l/h; c) hydroisomerisation/hydrocracking of the whole hydrogenated liquid fuel of stage b), without implementation of the pre-separation stage in presence of hydrogen and catalyst of hydroisomerisation/hydrocracking; d) distillation of the flow subject to hydrocracking/hydroisomerisation, which has been obtained at stage (c) in order to obtain at least fractions of kerosene and gas oil, and residual fraction. Obtained gas oil has the flow point below 0°C, cetane number exceeds 60, kerosene has setting point of not more than -35°C, and height of smokeless flame exceeds 25 mm.

EFFECT: improvement of gas oil properties.

14 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a catalyst for realising a method of hydrogenating olefins and oxygen-containing compounds in synthetic liquid hydrocarbons obtained via a Fischer-Tropsch method, containing a porous support made from γ-aluminium oxide on which a catalytically active palladium component is deposited, characterised by that pores in the support have effective radius of 4.0-10.0 nm, wherein content of foreign-metal impurities in the support is not more than 1500 ppm, and content of palladium in the catalyst is equal to 0.2-2.5 wt %. The invention also relates to a hydrogenation method using said catalyst.

EFFECT: invention enables to obtain saturated hydrocarbons from liquid Fischer-Tropsch synthesis products, which are a complex mixture of paraffin hydrocarbons with 5-32 carbon atoms, with ratio of normal paraffin hydrocarbons to isoparaffin hydrocarbons ranging from 1:1 to 7:1, containing up to 50% olefins and up to 5% oxygen-containing compounds.

2 cl, 1 tbl, 7 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing middle distillates from paraffin material obtained via Fischer-Tropsch synthesis, involving, before the hydrocracking/hydroisomerisation step, a step for hydrofining and purifying and/or removing impurities by passing through at least one multifunctional protective layer, where the protective layer contains at least one catalyst saturated with an active hydrogenating-dehydrogenating phase and having the following characteristics: volume of macropores with average diametre of 50 nm determined from mercury is higher than 0.1 cm3/g, the complete volume is greater than 0.6 cm3/g. The method also relates to apparatus for realising the disclosed method.

EFFECT: efficient method of obtaining middle distillates from paraffin material.

16 cl, 5 ex, 2 tbl, 5 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for desulphuration of two streams containing hydrocarbon material involving the following steps: (a) reaction of a first hydrocarbon material-containing stream (1), containing hydrocarbon components which boil above 343°C, and hydrogen (28), with a desulphuration catalyst in a desulphuration zone (3) used in desulphuration conditions to produce an outgoing stream (4) from the desulphuration zone; (b) feeding the outgoing stream from the desulphuration zone into vapour-liquid separator (5) which provides a vaporous stream (17) and a first liquid hydrocarbon-containing stream (6); (c) feeding the vaporous stream (17) and a second hydrocarbon-containing stream (18) into a hydrocracking zone (21) to produce an outgoing stream from the hydrocracking zone. (d) feeding the outgoing stream from the hydrocracking zone and the hydrocarbon-containing stream (16) of a repeated cycle into a hydrogenation zone (22) to produce an outgoing stream (23) from the hydrogenation zone; (e) fractionation of the outgoing stream (23) from the hydrogenation zone to produce an ultralow-sulphur hydrocarbon-containing stream (38); and (f) fractionation of the first liquid hydrocarbon-containing stream (6) extracted from step (b) to obtain a hydrocarbon-containing stream (16) of the repeated cycle, and a second liquid hydrocarbon-containing stream (17) containing hydrocarbon components and having low sulphur concentration.

EFFECT: obtaining ultralow-sulphur hydrocarbon products.

7 cl, 1 ex, 3 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to converting and/or processing distillation residues. Invention relates to a method of processing hydrocarbon material, involving a sequence of a first hydroconversion process which is realised upstream in at least one reactor, involving a reaction or reactions inside the said reactors and which activate at least one solid phase, at least one liquid phase and at least one gaseous phase, and a second reforming process realised downstream, conversion with water vapour, which includes at least one reactor, where the said process which is carried up stream is carried out in suspension and/or boiling bed and the said process which is realised upstream involves a first step for at least partial conversion of gaseous phase hydrocarbons, which are heavier than methane, to methane, where the step is called a pre-reforming step, and the reforming reaction(s) inside the said reactors downstream enable to obtain a hydrogen reagent required for chemical reactions in the first process.

EFFECT: self-sustenance of the hydroconversion process with hydrogen, high conversion of hydrocarbons.

3 ex, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a benzene hydrogenation and ring opening method and isomerisation of C5-C6 paraffins of starting paraffin material, which contains normal paraffins C5-C6 and at least 1 wt % benzene, involving: (a) feeding starting material, without tapping or condensing hydrogen, into a drier for removing water and obtaining dried starting material containing not less than 0.5 wt % water; (b) combination of dried starting material with a hydrogen-rich gas stream with formation of a mixed load; (c) feeding the mixed load at temperature ranging from 38 to 232°C into the hydrogenation zone, and bringing the said mixed load into contact with a hydrogenation catalyst under hydrogenation conditions in order to saturate benzene and form a stream of products, removed from the hydrogenation zone, with temperature ranging from 149 to 288°C and containing less than 1.5 wt % benzene; hydrogenation conditions include excess pressure from 1400 kPa to 4800 kPa, hourly space velocity for feeding the load from 1 to 40 h-1 and ratio of contained hydrogen to hydrocarbons ranging from 0.1 to 2; (d) regulation of temperature of the stream of product removed from the hydrogenation zone in the interval from 104 to 204°C through at least heat exchange of the product removed from the hydrogenation zone with the mixed load; (e) feeding at least part of the product removed from the hydrogenation zone into the isomerisation zone and bringing the stream of the said load into contact with an isomerisation catalyst under isomerisation and ring opening conditions at excess pressure ranging from 1380 to 4830 kPa; and (f) extraction of the isomerisation product obtained in the isomerisation zone. The invention also relates to a device for realising the proposed method.

EFFECT: use of the proposed invention provides for economisation by reducing the number of units of the equipment used and equipment expenses, and also reduces amount of hydrogen required for carrying the process.

9 cl, 1 tbl, 1 dwg

FIELD: fuels, chemical technology.

SUBSTANCE: invention relates to the content of benzene in commercial gasoline. Invention claims a method for decreasing the content of benzene in gasoline fractions by hydrogenation and isomerization in the presence of catalysts at increased temperatures and pressure of raw consisting of HK-85C fraction of the stable reforming fraction containing paraffins, naphthtenes and aromatic hydrocarbons with a directly distilled fraction wherein a directly distilled fraction represents HK-70C fraction and with recycle of flow isolated from products of isomerization of a hydrogenated fraction, regulation of temperature in the isomerization block of hydrogenation by measurement of amount of recycle taken in the amount 10-30% as measured for the parent raw.

EFFECT: improved decreasing method.

6 cl, 7 tbl, 11 ex

FIELD: machine building.

SUBSTANCE: proposed device comprises elongated vessel accommodating the tray. Said tray comprises multiple long cap extending above the tray upper surface. Said caps have bores in cover or side bore. Note here that first cap has topmost bore at great height abode the tray top surface compared with topmost bore of second cap.

EFFECT: controlled profile of fluid flow at increase in fluid flow.

13 cl, 5 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to catalysis. The invention relates to a zeolite Y with a modified faujasite structure, the intracrystalline structure of which contains at least one micropore system, at least one system of fine mesopores with average diametre of 2-5 nm and at least one system of large mesopores with average diametre of 10-50 nm. The invention also relates to particles which contain such zeolites, as well as use thereof in oil refinement, particularly as a hydrocracking catalyst.

EFFECT: high activity.

17 cl, 10 dwg, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to field of catalysis. Described is catalyst for recycling heavy oil fractions, in which active component, selected from nickel, or cobalt, or molybdenum, or tungsten compounds, or any their combination, is applied on inorganic porous carrier, consisting of aluminium oxide, dioxides of silicon, titanium or zirconium, alumosilicates or iron silicates, or any their combination, characterised by the fact that said catalyst contains macrospores, which form regular spatial macropore structure, and portion of macropores with size more than 50 nm constitutes not less than 30% in total specific volume of said catalyst pores.

EFFECT: increase of catalyst activity.

4 cl, 3 dwg, 1 tbl, 7 ex

FIELD: oil and gas industry.

SUBSTANCE: hydrofining method to obtain hydrocarbon compositions includes hydrofining of mixture that contains component (A) - gas oil in quantity from 20 up to 95 wt %; component (A1) - benzene in quantity from 1 up to 40 wt %; component (B) of biologic origin containing fatty acid esters, probably including freed fatty acids; quantity of biologic component is from 4 up to 60 wt %. Moreover all percent ratios are referred to total weight of all components. Hydrocarbon composition (C) has been also claimed; this composition can be used as propellant and/or fuel; it is obtained by hydrofining method; it has cetane number more than 50, density of 820-845 kg/m3, content of polyaromatic compositions less than 1 by wt % in regard to total weight of hydrocarbon compound and total content of polyaromatic compositions less than 20 be wt % in regard to total weight of the composition.

EFFECT: obtaining hydrocarbon composition with improved low-temperature properties.

39 cl, 4 tbl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: invention describes method of fine desulfurisation of oxygen-containing compounds, hydrocarbon material and sulphur-containing organic compounds by sulphur trapping from bulk containing ferric or zinc oxides in quantity of 20% by weight, zinc ferrite; at that the above method is implemented in presence of hydrogen at temperature within range of 200°C - 400°C.

EFFECT: increasing process efficiency.

10 cl, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: invention is referred to refining method of heavy vacuum residue and vacuum gas oil when raw material of vacuum residue is subjected to refining of heavy crude oil at first. The method includes vacuum segregation of output flow of the above refining in order to receive flow of heavy vacuum gasoil (HVGO), at that HVGO flow consists of content which more than 90% by mass boils within temperature range of 449-566°C and its part is recycled then back to the stage of heavy oil refining; light vacuum gasoil (LVGO) which content boils more than 90-100% by mass at temperature less than 538°C; medium vacuum gas oil (MVGO) that boils within the range between LVGO and HVGO; and the product in the form of vacuum residue, treatment of vacuum gasoil (VGO) when at least a part of the above LVGO and/or MVGO are subject to hydrofining.

EFFECT: higher selectivity for output of diesel fuel.

3 cl, 1 dwg, 3 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method for hydroconversion of heavy oil selected from crude oil, heavy crude oil, asphalt from tar sands, distillation residues, distillation heavy fractions, deasphalted distillation residues, plant oils, oils obtained from coal and oil shale, oils obtained by thermal decomposition of wastes, polymers, biomass, involving feeding heavy oil into a hydroconversion zone, said hydroconversion being carried out in one or more fluidised-bed reactors in which hydrogen is fed, in the presence of a suitable heterogeneous supported hydrogenation catalyst which is made of a support and an active phase which consists of a mixture of sulphides, one of which is obtained from a group VIB metal and at least one more is obtained from a group VIII metal, and a suitable hydrogenation catalyst which is a Mo or W sulphide-based catalyst, which is nanodispersed in said heavy oil, and feeding a stream from the hydroconversion zone into a separation zone in which the separated liquid fraction containing the nanodispersed catalyst is recycled into the fluidised-bed reactor(s).

EFFECT: high degree of hydrodenitrogenation and hydrodesulphurisation, high output of the diesel fraction.

15 cl, 1 dwg, 1 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to hydrofining catalysts. Described is a bead catalyst for hydrofining oil fractions, which consists of an aluminium oxide support, active components - molybdenum, nickel or cobalt compounds in form of oxides and/or sulphides and, optionally, additional zeolite Y in hydrogen form, which is in form of spherical or elliptical granules, characterised by that the catalyst granules have packed density of 0.4-0.5 g/ml and pore volume of not less than 1.2 ml/g. Described is a method of preparing said catalyst, involving peptisation of the starting powder - an aluminium oxide source with aqueous solution of an organic acid to obtain a pseudo-sol, moulding the obtained pseudo-sol in ammonia solution, drying and calcination of the support with subsequent embedding of active components therein, with optional embedding of zeolite Y in hydrogen form, drying and calcination of the catalyst in an air current, wherein the starting powder - aluminium oxide source used is weakly crystalline pseudo-boehmite; peptisation thereof is carried out using aqueous solution of an organic acid with concentration of 1-15 wt % and granulation (moulding) is carried out by drip moulding with the solid to liquid ratio in the pseudo-sol of not less than 1:2 and pH of the ammonia solution of not less than 11.0.

EFFECT: high activity, selectivity and stability of the catalyst.

3 cl, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: described is method of obtaining catalyst composition for hydroprocessing of hydrocarbons, which contains from 0.5% wt to 20% wt of metal component, selected from group consisting of cobalt and nickel, and from 0.5% wt to 50% wt of metal component, selected from group, consisting of molybdenum and tungsten, where said method includes: introduction of metal-containing solution into carrier to obtain carrier material with introduced in it metal; introduction of hydrocarbon oil into said carrier with introduced in it metal to obtain oil-impregnated composition; processing of said carrier material with introduced in it metal and said hydrocarbon oil with hydrogen; and contact of said carrier material with introduced in it metal and said hydrocarbon oil, further processed with hydrogen, with sulphur-containing compound. Described is catalyst composition, obtained by method described above. Described is method of hydrodesulphurisation, which includes: contact of initial hydrocarbon raw material with said composition at reaction temperature in the range from 200°C to 420°C and pressure within the range from 689.5 kPa (100 lbs/square inch) to 13879 kPa (2000 lbs/square inch).

EFFECT: claimed method makes it possible to obtain catalyst compositions for hydroprocessing, which possess high catalytic activity.

9 cl, 1 tbl, 1 dwg, 2 ex

FIELD: oil and gas industry.

SUBSTANCE: at least one reactor with fluidised bed is used in hydroconversion method; besides, raw material is added to gas space above the specified reactor. The above method involves separation of the above raw material in reactor into steam-like fraction and liquid fraction. The invention also refers to the reactor design allowing to implement the above method.

EFFECT: improvement of use efficiency of hydroconversion and performance characteristics of the process.

21 cl, 4 dwg, 3 tbl, 1 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of processing tall oil resin. The method of processing tall oil resin, which contains sterol alcohols, and, possibly, wood alcohols of fatty acids and resin acids, the source of which is tall oil, is characterised by the fact that, at least, a part of the fatty acids and resin acids is released from sterol ethers and ethers of wood alcohols and converted into lower alkyl ethers; alkyl ethers, obtained in he said way, are extracted by evaporation from resin, then condensed, with the further hydration of the obtained condensate. The product, obtained by the claimed method and the application of the method for fuel production are also claimed.

EFFECT: application of tall oil resin, which usually represents a waste product, for obtaining fuel or a fuel component.

17 cl, 1 dwg

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