RU2674158C1 - Installation for producing liquid hydrocarbons from biomass - Google Patents

Abstract

FIELD: technological processes.SUBSTANCE: invention relates to an installation for the conversion of biomass to liquid hydrocarbons, used as a component of aviation fuel. Installation for producing liquid hydrocarbons from biomass includes sequentially connected units: a syngas production unit, a SG (syngas) purification and dehydration unit and a hydrocarbon synthesis unit, characterized in that in the unit for producing SG, the process of two-stage thermal conversion of biomass into syngas is realized, combining pyrolysis with high-temperature cracking of volatile products on the carbon residue of the processed raw material, and the hydrocarbon synthesis unit includes two successively connected reactors – a reactor for the synthesis of oxygenates (methanol, DME) and light hydrocarbons of the gasoline series (P1) and a reactor for the synthesis of aromatic hydrocarbons (P2) from oxygenates formed in the first reactor, after their separation from the hydrocarbon part product, while the aromatic hydrocarbons formed in P2 are mixed in various proportions with the hydrocarbons of the gasoline series formed in the first reactor to form a hydrocarbon (h/c) mixture used later as the initial component of aviation fuel.EFFECT: production of good quality syngas that does not require additional operations in the subsequent transformation, its almost complete use, almost complete absence of harmful emissions, the energy efficiency of the installation as a whole.6 cl, 6 tbl, 2 dwg

Description

The present invention relates to the field of producing liquid hydrocarbons from biomass, and in particular to a plant for converting biomass (wood, peat, agricultural waste, food industry waste, sewage sludge, etc.) into liquid hydrocarbons (w / w), hereinafter used as gasoline component.

The installation can be used in the petrochemical and gas industries for the utilization of biomass to produce synthesis gas (SG), oxygenates, liquid hydrocarbons, including aromatic ones, during processing. Hydrocarbons, which are obtained at the facility, can be used in the future as the starting component of aviation gasolines.

The proposed technology for the catalytic processing of biomass into liquid chemical products is the link between the well-known processing technologies "biomass - gas synthesis - crude methanol - u / v" and the processing technology "aromatic hydrocarbon concentrate - marketable aromatic hydrocarbons - products for their further processing", which allows to receive the basic component of jet fuel not from hydrocarbon raw materials, but from more affordable and inexpensive raw materials.

In Germany, Choren has developed a process whereby SG is first obtained from biomass using the Carbo-V process, and then fuel (the so-called SunDiesel fuel) is produced using the Fischer-Tropsch process. The specified method "Carbo-V" is a three-stage method of gasification, including the following intermediate operations:

gasification at low temperature,

gasification at high temperature,

endothermic smoke gasification.

During the first operation of the method, continuous carbonization (carbonization) of biomass (water content 15-20%) is carried out by partial oxidation (carbonization) of air or oxygen at a temperature of from 400 to 500 ° C, i.e. biomass is destroyed with the formation of tar-containing gas (volatile fractions) and solid carbon (biocox).

During the second operation of the method, repeated substoichiometric oxidation of the resinous gas with air and / or oxygen is performed in the combustion chamber at a temperature above the melting temperature of the ash of combustible materials, resulting in a hot gasification medium.

During the third operation of the method, biocoke, crushed to form pulverized fuel, is blown into the hot gasification medium. Thus, in the gasification reactor, an endothermic reaction occurs between the pulverized fuel and the gasification medium, leading to the formation of crude synthesis gas. After appropriate treatment, the resulting gas can be used as combustible gas to generate electricity, water vapor and heat, or synthesis gas, which is converted to SunDiesel using the Fischer-Tropsch process. The disadvantages of this method are multi-stage gasification and the need for grinding biocoke. In addition, this method is not suitable for gasification of waste of all types.

The disadvantage of all known methods and installations for producing liquid hydrocarbons from carbon-containing raw materials is that the range of raw materials used is very limited. So, at the stage of producing SG, in most cases, light carbon-containing raw materials (natural and associated petroleum gas) are used, which are converted to oxygenates or hydrocarbons by traditional steam or oxidative conversion, and in the case of oxidative conversion with air, they are strongly ballasted with nitrogen (inert) SG, the conversion of which into valuable products (oxygenates, in / in) is very complicated.

A known method of producing synthetic gasoline from synthesis gas by contacting the feedstock in the first stage with an oxide catalyst for the synthesis of methanol from carbon monoxide and hydrogen and a solid acidic inorganic dehydration catalyst at 149-372 ° C, followed by contacting in the second stage the products of the first stage at 260- 455 ° С with crystalline zeolite characterized by the ratio of the first order rate constants when cracking n-hexane and 3-methylpentane at a cracking temperature of 288-510 ° С equal to 1-12 (USSR AS N 632296, cl. 07S 1/01, B01J 23/80, 1978). According to the invention, a mixture of copper, chromium, zinc and lanthanum oxides taken in an amount of 50-70 is used as an oxide catalyst for methanol synthesis; 5-15; 15-25; 5-15 weight. hours, respectively.

The main disadvantage of this method is the low yield of the liquid fraction of C ₅₊ hydrocarbons based on convertible carbon monoxide. In addition, only a mixture of CO and H _{2 is} used as raw material, and dimethyl ether (DME) is not the target synthesis product.

A known method of producing hydrocarbons by processing synthesis gas containing hydrogen and carbon oxides and having a molar ratio of CO / H ₂ above 1 and provided that the synthesis gas entering the conversion has a molar ratio of CO / CO ₂ from 5 to 20 ( U.S. Patent No. 4,481,305, CL C07C 1/04, C07C 1/20, 1984). According to the invention, the process is carried out in two successive reactors at a pressure of 5-100 atm. without intermediate separation of products after the first reactor. In the first reactor, the synthesis gas is in contact with one or more catalysts that convert the synthesis gas at a temperature of 150-400 ° C to methanol and then in the same reactor in DME. Next, the gas mixture is sent to the second reactor, where in the presence of a zeolite catalyst at a temperature of 150-600 ° C, DME converts to hydrocarbons, mainly liquid under normal conditions.

The main disadvantages of this method are:

- low yield of gasoline fraction on the fed "carbon" of the feedstock (29 wt.%);

- the need to remove from raw materials a significant amount of undesirable CO ₂ , which is 55 wt. % (mass fraction of "carbon" removed from CO ₂ , referred to the supplied "carbon" of the feedstock);

- the process does not provide for obtaining DME as the target product. The one-step synthesis of DME from a mixture of CO, CO ₂ and H _{2 is} more efficient and

It requires less capital expenditures, compared with the production of DME from synthesis gas in two stages - through the synthesis of methanol.

A known method of producing DME and / or high-octane gasoline from methanol, developed by the company "Mobil Oil Corporation" (US patent N 4587373, CL C07C 1/20, 1986). According to this method, methanol is fed into a reactor containing a ZSM-5 type catalyst at elevated temperature and pressure of 3-20 atm. The reaction products are sequentially separated in separators, an absorber and distillation columns with the release according to option 1 - DME, stable gasoline and olefins, according to option 2 - only stable gasoline and olefins. DME, together with methanol and water in option 2, is recycled to be converted to hydrocarbons. The claimed method differs from the analogue in the type of processed raw materials and the catalyst used.

Closest to the present invention is a METHOD FOR PRODUCING MOTOR FUELS FROM CARBON-CONTAINING RAW MATERIALS (RF patent No. 2143417), where an increase in the yield of a liquid fraction of C ₅₊ hydrocarbons based on supplied carbon oxides is achieved by catalytic processing of a mixture of CO, CO ₂ and H ₂ in two stages so that in the first stage, the feedstock is contacted with a catalyst consisting of a ZSM-5 type zeolite and a metal oxide component containing mass. %: CuO 38-64, ZnO 24-34, Cr ₂ O ₃ 0-22, Al ₂ O ₃ 6-9, mixed in the mass ratio (20-50) :( 80-50), the gas stream after the first stage reactor without separation, they are sent to the second stage, where in contact with a catalyst consisting of a zeolite of the ZSM-5 type and a metal oxide component containing (wt.%): ZnO 65-70, Cr ₂ O ₃ 29-34, W ₂ O ₅ 1, mixed in the ratio (30-90): (70-1), dimethyl ether and the components of the synthesis gas are converted into a gasoline fraction, gaseous hydrocarbons and an aqueous fraction.

The disadvantages of the proposed method is that:

- the examples show the results of the production of oxygenates and a further gasoline fraction when operating on synthesis gas with a ratio of Н ₂ / СО (Н ₂ - 68, СО - 29 and СО ₂ - 3), which is practically optimal for methanol synthesis, while not considering work options with poor in H ₂ synthesis gas.

- the conversion of dimethyl ether and methanol to the gasoline fraction in the reactor of the 2nd stage occurs under rather severe conditions at a temperature of 380-420 ° C and a pressure of 80 atm., which requires additional compression.

- the installation uses costly recirculation to the reactor of the 1st stage. So, gas washed from dimethyl ether, composition (vol.%): H ₂ - 67.3, СО - 28.4, СО ₂ - 3.3, DME - 0.7 and methanol - 0.3 after the wash column They are divided into two streams, one of which is mixed with raw synthesis gas.

The technical task of the present invention is the creation of an energy-efficient installation for producing liquid hydrocarbons from biomass, which are used hereinafter as the basic component of aviation gasoline, as well as simplifying the technological scheme for the production of air-conditioning and reducing capital costs.

To achieve the technical objective, a plant is proposed for the production of liquid hydrocarbons from biomass, which includes blocks connected in series: the SG production unit, the SG cleaning and drying unit, and the hydrocarbon synthesis unit, including aromatic.

The invention is illustrated in FIG. one.

The drawing (Fig. 1) schematically shows a schematic process diagram of an installation for producing liquid hydrocarbons from biomass. The diagram does not show auxiliary elements of technological equipment, such as pumps, shut-off and control valves, gas blowers, sensors and actuators of the automatic control system, etc., as well as a unit for collecting and storing the resulting basic component of aviation gasoline.

In the SG production unit, a two-stage thermal conversion of biomass to synthesis gas is implemented, combining pyrolysis with high-temperature cracking of volatile products on the coke residue of the processed raw materials. Condensed fuel to gas conversion methods can be divided into two main types: gasification and pyrolysis.

Gasification is a process of partial oxidation of carbon-containing raw materials (biomass) to produce a generator gas, which consists of CO, H ₂ , CH ₄ CO ₂ , C _n H _m , H ₂ O, N ₂ (with air blasting) and various impurities, such like resins, particles of carbonaceous matter and ash [Geletukha GG, Zheleznaya T.A. // Overview of biomass gasification technologies // Ecotechnologies and resource saving, 1998. - No. 2. - S. 21-29]. Air, oxygen, water vapor or mixtures of these substances can be used as an oxidizing agent during gasification. During air gasification, generator gas is produced with a lower calorific value not higher than 6 MJ / nm ³ [VV Kosov, VF Kosov, IL Maikov et al. // High calorific gas mixture produced by pyrolysis of wood and peat // Proc. of 17 ^th European Biomass Conference and Exhibition, Hamburg, Germany, 29 June - 3 July 2009. - P. 1085-1088]. This gas can be burned in boilers, after purification - in gas engines or turbines. The energy content of the resulting gaseous fuel is up to 80-90% of the original. Gasification using oxygen gives medium calorific gas (10-12 MJ / nm ³ ), which is also suitable for use as synthesis gas for the production of methanol and aviation fuel components. Middle-calorie gas (15-20 MJ / nm ³ ) can also be obtained by steam (pyrolytic) gasification in a two-stage process, implemented in two fluidized bed reactors [Geletukha G.G., Zheleznaya T.A. Overview of biomass gasification technologies. - Ecotechnology and resource conservation, 1998. - No. 2. - S. 21-29]. However, during oxygen or vapor-air gasification, the air separation unit or a steam generator must be present in the process chain, which entails a significant increase in the cost of the final product.

Pyrolysis is the thermal decomposition of raw materials without the access of an oxidizing agent. The products of pyrolysis are a gas mixture consisting mainly of H ₂ , CO, CO ₂ , CH ₄ , C _n H _m and N ₂ , the liquid fraction, which is a mixture of pyrogenetic water and resins, as well as a solid coke residue. Gas mixtures obtained from biomass have a lower calorific value of up to 20 MJ / nm ³ . The mass fraction of coke residue mainly depends on the final process temperature and is usually 20-30% relative to dry weight for wood raw materials. The mass ratio of liquid and gaseous products is approximately 1.5 and most significantly depends on the heating rate [Kislitsyn A.N. Pyrolysis of wood: chemistry, kinetics, products, new processes. - Moscow, Timber industry, 1990. - 313 p.]. The main disadvantages of pyrolysis from the point of view of obtaining gas mixtures are the relatively low specific gas yield, which does not exceed 0.3-0.4 nm ³ per 1 kg of raw materials and a high content of carbon dioxide (up to 30% vol.). This leads to low efficiency of energy conversion of the feedstock into gaseous products: the ratio of the energy content of pyrolysis gas to the calorific value of the feedstock does not exceed 0.3. Therefore, the main tasks in the development of technologies for the thermal conversion of biomass based on the pyrolysis process are to increase the degree of conversion of raw materials to the gas fraction and to reduce the content of carbon dioxide. An increase in the degree of conversion of raw materials can be achieved by processing the liquid fraction into gas, for which they are used as catalytic [Dayton D.A. // Review of the Literature on Catalytic Biomass Tar Destruction. Milestone Completion Report. - NREL / TP-510-32815. - National Renewable Energy Laboratory. - USA, 2002], and non-catalytic methods [Snehalatha K. Chembukulam, Arunkumar S. Dandge, Narasimhan L. Kovilur et al. // Smokeless fuel from carbonized sawdust // Chem. Prod. Res. Dev. - 1981. - V. 20. - P. 714-719].

In this installation, we used the cracking of a vapor – gas mixture of pyrolysis products formed during the heating of raw materials blown through a porous carbon medium maintained at a fixed temperature. The two-stage process of thermal conversion of biomass to SG realized in the SG production unit made it possible to obtain a specific volume of the formed SG of 1.35 nm ³ / kg, the total content of H ₂ and CO was 95 vol. %, and the ratio of H ₂ : CO was in the range of 0.98-1.23 and mainly depends on the duration of the interaction of gaseous pyrolysis products and hot coke residue. The synthesis gas obtained in the SG production unit, dried and cleaned of carbon particles from microparticles, was suitable for use as a fuel for autonomous energy complexes based on gas reciprocating and gas turbine power units, as well as for the synthesis of dimethyl ether and methanol with a two-layer loading of methanol catalyst and γ-Al ₂ O ₃ .

From the point of view of converting biomass to a gaseous energy carrier, in addition to creating autonomous energy complexes based on gas reciprocating and gas turbine power units, one of the urgent tasks is the production of dimethyl ether (DME) and methanol, from which the basic component of aviation fuel can be obtained.

The SG purification unit includes intermediate tanks connected in series to the scrubbers and a solvent regeneration system — methanol used to purify the synthesis gas.

At the first stage, pre-compressed to a pressure of 2.1-2.5 MPa, the synthesis gas is fed into a scrubber (1), where it is washed with water using impurities such as HCl, NH ₃ and part of HCN. After washing with water, the synthesis gas, cooled to a temperature of minus 30 to 0 ° C, is fed into the second scrubber (2), where the purification is carried out using methanol. The methanol in the scrubber (2) removes major impurities such as H ₂ S, COS, CS ₂ and HCN. Pure gas after washing contains a certain amount of methanol, not more than 3 g / nm ³ . To reduce the methanol content in the purified synthesis gas at the outlet of the scrubber (2), it is subjected to condensation in a gas cooler. To reduce operating costs, the methanol used in the scrubber (2) is regenerated.

The hydrocarbon synthesis unit includes two series-connected reactors - a methanol, DME and gasoline hydrocarbon synthesis reactor (P1) and an aromatic hydrocarbon synthesis reactor (P2), with oxygenates (methanol and DME) formed in the first reactor after separation from the hydrocarbon parts of the product are further converted to aromatic u / in concentrate, which is subsequently mixed with gasoline hydrocarbons formed in the first reactor to form the mixture used later to the original component of aviation gasoline.

In the reactor P1 of the hydrocarbon synthesis unit, a mixed catalyst is loaded, which is a 1/1/1 mechanical mixture:

- oxide CuO - 62.0; ZnO - 28.0; Al ₂ O ₃ - 10.0 methanol synthesis catalyst,

- aluminum oxide brand A-64 (Ryazan catalyst factory) -mechanical conversion catalyst in DME

- zeolite, such as pentasil, with a silicate module SiO ₂ / Al ₂ O ₃ = 70-80 - a catalyst for the conversion of oxygenates in the on / in the gasoline series, including aromatic ones, which allows the preparation of on / in oxygenates (methanol and DME) gasoline series, including aromatic ones.

A zeolite, such as pentasil, with a silicate module SiO ₂ / Al ₂ O ₃ = 20, which allows the conversion of oxygenates (methanol and DME) obtained in P1, into a mixture of high-octane hydrocarbons, mainly aromatic, which are further sent for mixing with gasoline / in isolated from the product obtained in P1. The catalyst is characterized in that it is capable of operating at elevated temperatures and is resistant to water vapor, since it contains HZSM-5 zeolite that has undergone thermocouple treatment (TPO), and a composition of silicon and aluminum oxides is used as a binder component.

The installation additionally includes a recuperative heater of methanol, DME and water vapors obtained and isolated from the product obtained in P1.

The installation allows you to process such types of biomass as wood, peat, agricultural waste, food industry waste, sewage sludge, etc.

A plant for the production of chemical products, including the basic component of aviation gasoline, from biomass includes the following blocks: 1. Block for producing SG (1)

A schematic diagram of a unit for converting biomass to synthesis gas is shown in FIG. 2. In the SG production unit, the biomass from the feed hopper (9) is fed in portions to the pyrolysis reactor (16) using a piston (11) reciprocating; the role of the power mechanism is played by a hydraulic cylinder (10) connected to the pumping station (13) through a control valve (12) having electromagnetic control. The biomass is compacted, creating a sealed plug at the inlet of the reactor, which prevents the exit of gaseous pyrolysis products to the outside, and then moves in the form of a compressed briquette through the pyrolysis reactor due to the arrival of new portions. Biomass heating occurs through the wall from hot combustion products formed in the furnace (20) or burner when burning any available fuel necessary to support the conversion process. In the pyrolysis reactor, biomass is gradually heated to a temperature of about 600-700 ° C and volatiles are released, which, through perforation, enter gas collectors, through which they are transported to a hopper filled with coke residue of the processed biomass, a cracking reactor (18). The temperature of the cracking reactor is maintained at a level of 900 -1000 ° C, also due to the supply of heat through the wall from the combustion products. Pyrolysis gases pass through a layer of hot coke residue, turning into synthesis gas, and then are diverted for purification, cooling and further use. In the coke residue bunker (19), which can be periodically unloaded, an excess of coke residue, which is formed during the processing of biomass and can be used both in the process itself (to provide for its own needs for thermal energy), naturally enters from the cracking reactor goals. The outer casing (17) has a bypass (14) and dampers (15), which allow regulating the flow of combustion products in the pyrolysis zone to maintain the required temperature.

2. The SG cleaning and drying unit (3) includes in series scrubbers intermediate tanks and a solvent recovery system - methanol used for the synthesis gas purification.

In the first stage, pre-compressed to a pressure of 2.1-2.5 MPa, the synthesis gas is fed into a scrubber, where it is washed with water using impurities such as HCl, NH ₃ and part of HCN. After washing with water, the synthesis gas, cooled to a temperature of minus 30 to 0 ° C, is fed into the second scrubber, where the cleaning is carried out using methanol. Methanol in a scrubber removes major impurities such as H ₂ S, COS, CS ₂ and HCN. Pure gas after washing contains a certain amount of methanol, not more than 3 g / nm ³ . To reduce the methanol content in the purified synthesis gas, it is condensed at the outlet of the scrubber in a gas cooler. To reduce operating costs, the methanol used in the scrubber is regenerated.

3. Block for the synthesis of liquid hydrocarbons.

The SG from the cleaning and drying unit of the SG (3) after the reciprocating compressor (4) enters the reactor P1 (6) for the synthesis of oxygenates and UV. In the reactor on a low-temperature catalyst at a pressure of up to 5 MPa and a temperature of up to 220-260 ° C, a reaction of synthesis of oxygenates (methanol and DME) takes place and at the same time light liquid hydrocarbon-derived liquid form from oxygenates.

Leaving reactor P1 (6), the reaction mixture is cooled in a heat exchanger (2) and enters a three-phase separator (5), where the lungs are separated from the air in the gasoline series. The resulting water-methanol phase is mixed with unreacted SH, containing DME and gas taken away by gas flux, is heated in the heat exchanger (2) with hot SH leaving the biomass gasifier, and enters P2 (7), where at a pressure of 0, 3-1 MPa and a temperature of up to 360-440 ° С the reaction of aromatic u / c synthesis takes place. Leaving reactor P2 (7), the reaction mixture is cooled in a heat exchanger (2) and enters a three-phase separator (8), where the UV are separated, consisting mainly of high-octane aromatic UV, which are mixed with light UV in the gasoline range. The resulting mixture is subsequently used as a component of aviation gasoline.

The gas exiting from the three-phase separator (8) can be used as fuel gas in the biomass gasification unit, and the produced water, which does not contain oxygenates, is used as technical.

The equipment of the liquid hydrocarbon production unit is equipped with connecting pipelines.

The invention is illustrated by the following examples.

1. Process indicators in the block receiving SG

The gasification process in the SG production unit was carried out on two separate installation modules at the same temperatures of the pyrolysis and cracking reactors, while the process indicators on 2 types of biomass are presented: pine shavings and oak sawdust. Table 1 shows: the values of the main input parameters of the installation at the nominal operating mode and the properties of wood biomass.

The biomass feed mode was the same for both options - 1 feed cycle every 15 seconds, however, the biomass mass flow rate was very different. This is due to a significant difference in bulk density between pine shavings and oak sawdust with the same amount of feedstock loaded per feed cycle. The elemental composition of the raw materials for both variants, as can be seen from the data presented, mainly differed slightly. It should only be noted that the hydrogen content in the pine shavings is 0.49 mass. % exceeded the same indicator for oak sawdust, including due to higher humidity. The yield of volatiles during pyrolysis to a final temperature of 700 ° C and 1000 ° C and the elemental composition of the coke residue in both cases also differed insignificantly, which allows us to speak about similar experimental conditions.

Data on the chemical composition and volume of the resulting synthesis gas for two types of biomass are presented in table 2.

As can be seen from the data presented in table 2, the experimental values of the specific volume and chemical composition of the resulting synthesis gas in the transition from laboratory research to a pilot plant of high productivity are in good agreement.

2. Process indicators in the block for producing liquid hydrocarbons.

The calculation was carried out on 1000 m ³ / h of SG supplied to P1. The composition of the raw materials used and the indicators of the process of obtaining oxygenates and / in the gasoline series in P1 are presented in table 3.

From table 3 it is seen that:

- the conversion of CO at the exit from P1 is 46%, which is a fairly high rate of conversion of SG per passage in the synthesis of oxygenates. This CO conversion index, which is superior in value to traditional industrial methanol production methods, can be achieved due to the fact that the mixed catalyst loaded into the reactor in the proposed installation simultaneously with methanol synthesis removes it from the reaction during the formation of DME, as well as into the gasoline series.

- in the composition of the reaction gas leaving P1 and separated into TFS-1, in addition to unreacted SG, it also contains DME (73.8 g) and a gasoline in / out (77.6 g), which are processed into aromatic in / in. in series located in the circuit P2.

- in the composition of liquid products collected in TFS-1, 2 phases are observed: the water-methanol phase containing methanol (10.7 g) and dissolved DME (3.7 g), as well as the in / in phase containing 46.1 g of lungs in / in the gasoline range.

- when combining the flows of the water-methanol phase and gas coming from TFS-1, and when processing this combined stream into R-2, the proposed installation allows additional processing of 166 g of oxygenates to obtain an aromatic hydrocarbon fraction (concentrate).

From table 4 it is seen that in this example, 166 g of oxygenates and y / in can be additionally converted, while during their conversion 120.1 g of synthetic gasoline with an aromatic content of y / 72 of 72% was obtained. The choice of parameters for the process in P2 as part of the proposed installation (pressure in the range of 0.3-1MPa and temperature in the range of 360-440 ° C) allows you to flexibly change the aromatic content in / in the range of 70-90 mass. %

Thus, in this example of the unit’s operation, we obtained 46.1 g of liquid in / in gasoline series already containing up to 5% aromatics in P1, and in addition in P2 we obtained 120.1 g of aromatic water / in concentrate, when mixed as a result, 166.2 g of synthetic gasoline can be obtained, which can later be used as a high-octane base component of aviation gasoline, since it contains more than 30% iso-paraffins and more than 50% aromatic UV (see table 5).

Table 5 presents the hydrocarbon composition of gasoline obtained by mixing in / obtained in P1 and P2 of the proposed installation, and used in the future as a basic component of aviation gasoline.

From table 5 it is seen that in the composition of the base component contains 51.47 mass. % aromatic iv / and 29.79% isoparaffins, compounds having a high octane number.

3. Development of the optimal formulation of aviation gasoline.

In the invention, the following aviation gasoline composition is developed and a prototype composition is prepared:

- basic component - 55% of the mass;

- straight run fraction of 50-100 ° C - 35% of the mass;

- reference isooctane - 10% of the mass;

- ethyl fluid introduced into the composition of 2.0 g / kg

A full analysis of the quality of the obtained prototype aviation gasoline in comparison with the standards TU 38.401-58-47-92 for aviation gasoline B-92, with the exception of the indicators "grade" and "stability period" is shown in table 6. Table 6. Physico-chemical and operational performance of a prototype aviation gasoline obtained from synthesis gas.

* Determined at the pre-production stage and guaranteed by the manufacturer (TP TS).

** Aviation gasoline with an octane rating of at least 99.5 and a grade of at least 130 may contain a blue dye (TP TS).

*** The blue color is due to the presence of dye contained in ethyl fluid.

From table 6 it is seen that by introducing additives into the base component synthesized in the present invention from biomass (pine shavings), a sample of aviation gasoline is obtained that meets the requirements of regulatory documents for aviation gasoline B-92.

The advantages of technical solutions used in the proposed installation is the simplicity of the technological design of the process, as well as the fact that:

- with the help of the installation all types of waste can be disposed of without preliminary complex separation, including biowaste. In the art, a method of this type is known as the Thermoselect method, which is described in European patents EP 1377358 and EP 0790291.

- the synthesis gas obtained in the present invention has a favorable volumetric ratio of carbon monoxide to hydrogen (in the range of H ₂ / CO = 0.98-1.23), and therefore there is no need to additionally shift the volumetric ratio of carbon monoxide to hydrogen in side of hydrogen using a “water shift reaction”.

- the method and installation allows you to use at least 70% of the resulting synthesis gas in the reaction of its conversion into hydrocarbons, while the unused portion of the synthesis gas is used to cover the energy costs necessary for the implementation of the disposal method.

Thus, the advantage of the proposed installation is the zero energy balance. In addition, a significant advantage of this method and installation is the almost complete absence of harmful emissions during its implementation.

Claims (6)

1. Installation for producing liquid hydrocarbons from biomass, which includes series-connected blocks: a synthesis gas production unit, an SG purification and drying unit and a hydrocarbon synthesis unit, characterized in that a two-stage thermal conversion of biomass to synthesis is implemented in the SG production unit gas combining pyrolysis with high-temperature cracking of volatile products on the coke residue of the processed raw materials, and the hydrocarbon synthesis unit includes two series-connected reactors - a synthesis reactor ok Igenates (methanol, DME) and light gasoline hydrocarbons (P1) and a reactor for the synthesis of aromatic hydrocarbons (P2) from oxygenates formed in the first reactor, after their separation from the hydrocarbon part of the product, while aromatic hydrocarbons formed in P2 in various proportions mixed with gasoline hydrocarbons formed in the first reactor, with the formation of hydrocarbon (u / in) mixture, which is used in the future as the starting component of aviation gasoline. 2. Installation according to claim 1, characterized in that the SG production unit is made in the form of a reactor in which a two-stage thermal conversion of biomass to synthesis gas is implemented, combining pyrolysis with high temperature cracking of volatile products on the coke residue of the processed raw materials. 3. Installation according to claim 1, characterized in that the SG cleaning and drying unit is made in the form of a scrubber system in which the synthesis gas is purified and dried by methyl alcohol in countercurrent flow. 4. Installation according to claim 1, characterized in that the hydrocarbon synthesis unit further includes a regenerative heater for the crude methanol vapor and DME obtained in the oxygenate synthesis reactor. 5. Installation according to claim 1, characterized in that a mixed catalyst is loaded into the reactor P1 of the hydrocarbon synthesis unit, which is a mechanical mixture of 1/1/1 oxide CuO-ZnO-Al ₂ O ₃ methanol synthesis catalyst, aluminum oxide - methanol conversion catalyst in DME and a pentasil-type zeolite — a catalyst for the conversion of oxygenates to iv. 6. Installation according to claim 1, characterized in that wood, peat, agricultural waste, food industry waste, sewage sludge are used as biomass.

Images