Catalytic high octane gasoline fractions and aromatic hydrocarbons

 

(57) Abstract:

The invention relates to an integrated device for the production of high-octane gasoline fractions and/or aromatic hydrocarbons, C6-C10by catalytic processing of organic raw materials on the basis of hydrocarbons, oxygen-containing compounds or mixtures thereof. The installation includes technologically tied distillation columns, separators, heat exchangers, vessels, and pumping equipment and reactor blocks. The reactor unit is a combined flue and installed sequentially, during the feed of the gaseous heat carrier, heat, catalytic reactor shell and tube type and shell and tube heat exchanger. To improve temperature management work is loaded into the tube space of the reactor catalyst at different stages of the process occur with different thermal effects of reactions (including exothermic and endothermic heat effect) submit annulus reactor gas coolant to a specified temperature (100-600oC). The gaseous coolant produced by combustion in the heat of the fuel ASS="ptx2">

The invention relates to an integrated device for the production of unleaded high-octane gasoline fractions and/or aromatic hydrocarbons, C6-C10by catalytic processing of organic raw materials on the basis of hydrocarbons, oxygen-containing organic compounds or their mixtures. Installation possible processing of crude oils and gas condensates, virgin and secondary gasoline fractions, condensate and associated gas, refined reforming, natural gas gasoline, registergui gases, spirit and ether fractions, etc. depending on the nature of the raw materials on the installation you may receive diesel and residual fractions. The unit can be used in compositions of chemical processing, refinery, gas processing, etc. for production and primary processing of oil and gas condensate, and independent operations.

Known catalytic cracking of heavy oil fractions for the production of light petroleum products gasoline and diesel fractions [1] the system includes a catalytic reactor, regenerator, distillation columns, furnace, electrostatic precipitator, boiler, tank, furnace pressure, pumps, blower, pneumodynamic. Uglevodorodnaya gasoline, the oil and hydrocarbon gases. The main disadvantages of catalytic cracking are:

the organization moving catalyst, which complicates instrumentation installation and increases the consumption of the catalyst due to its abrasive wear;

raw materials are heavy petroleum fraction with an initial boiling point of 300oC and above, which makes it almost impossible refining of hydrocarbon fractions, wikipaedia 200oC, and oxygen-containing organic compounds.

Known installation reforming for the processing of straight-run fractions of gas condensate in high-octane unleaded gasoline [2] which contains a furnace for heating and evaporation of raw materials, catalytic reactors adiabatic type, three distillation columns for the separation of the raw materials and reaction products and technologically tied with them separating and heat exchange equipment. Nodes fractionation of raw materials and the reaction products are in continuous mode, and the reactors in a circular diagram in the "reaction-regeneration" (i.e., one reactor operates in the mode of production of gasoline, and the other is in the regeneration mode of the catalyst) with alternating modes. Catechna (> 185oC) fraction.

Known catalytic installation reforming processing gasoline fractions to increase their octane number according to the method of [3] This system includes a furnace for heating raw materials, catalytic reactors adiabatic type for the chemical transformation of raw materials, two distillation columns for the stabilization of raw materials and selection of the target product and technologically tied with them exchangers, coolers, condensers and separators. Nodes fractionation of raw materials and the reaction products are in continuous mode, and the reactor in the reaction-regeneration".

General shortcomings of the described devices [2, 3] are:

the use of adiabatic reactors (i.e., vehicles hollow type without additional supply or removal of heat), which causes the complexity of the regulation of the temperature modes of the catalyst during the production stage of gasoline (the temperature drop over the layer of catalyst, due to the endothermic effect of the reaction) and at the stage of catalyst regeneration (requires removal of heat to prevent the temperature increase resulting from the high exothermic effect of the reaction of combustion of coke);

The closest in technical essence is the catalytic production of gasoline from a hydrocarbon feedstock [4] in Accordance with the selected prototype system includes a technologically tied: two distillation columns; air condensers; capacity-separators; heat exchangers and two reactor-heat unit. Each reactor-heat block (RTB) is a circulating duct consisting of a fan, the heat generator and reactor block containing the set sequentially (in the direction of the gas coolant) superheater materials, catalytic tubular reactor, evaporator raw materials, two heater distillation products of distillation columns and the heater material.

Installation of the prototype works as follows. The feedstock is heated in heaters raw materials both RTB and served in the extractive distillation column, heat input in which is carried through the circulation through the heater both RTB part of the cubic product of the column, the carrying of which take away from the installation. Riding raw column distillate, which is cooled and condensed in overhead condenser and sent to the capacity of the separator, from Katie columns, as part of the on catalytic processing in one of the RTB (another RTB operates in the regeneration mode of the catalyst). In RTB raw material process flows sequentially through the evaporator and the superheater in a tubular catalytic reactor loaded with catalyst reforming IR-30, which is the chemical conversion of hydrocarbon raw materials. After the reactor, the reaction products are cooled in the heat exchanger, condense in the air condenser and sent to the capacity of the separator, where hydrocarbon gases away from the installation, and the liquid fraction is directed through the heat exchanger in the product distillation column. Heat input to the column is carried out by circulating through the heater both RTB part of the cubic product of the column, the carrying of which take away from the installation. Top of the column select petrol fumes, which is cooled and condensed in overhead condenser and sent to the capacity of the separator. Separated hydrocarbon gases from the separator away from the installation, and the liquid distillate is partially directed to the irrigation of the column and a portion is directed to a commodity Park as the target of gasoline.

The processes of heating and evaporation of raw materials, processes, rectification, maintenance zadarnowski on flues reactor-thermal blocks. Each RTB gaseous fluid is prepared by mixing a portion of the circulating and cooled in RTB to a temperature of 320-360oC heat flue gases obtained by burning in the heat of the hydrocarbon gas. After the heat source hot coolant with a temperature of 550-600oC pass through the annulus of the superheater, reactor, evaporator, two heaters distillation products of columns and heater feedstock, where it is cooled by the heat of the respective threads. Part of the cooled coolant is served by fan to circulate the coolant, a heat source for cooking hot fluid with a temperature of 550-600oC, and excess dropping in the candle.

The main disadvantages of the installation of the prototype are:

application for the installation of the reactor-heating units in the form of the circulation duct containing the fan, the heater, superheater materials, catalytic tubular reactor, evaporator, two heater distillation products of distillation columns and the heater substrate; applying to the installation of the reactor device of this construction leads to the complication of R is the mode of operation of the reactor section of RTB by changing the temperature or amount of gaseous coolant change mode works heaters, associated with distillation columns, and, as a consequence, the change of temperature modes of the columns, which entails changing the composition and quality of products of the columns;

complex design of the reactor, a heat block;

application for the installation of gas coolant with a temperature of 550 - 600oC, which makes it difficult to regulate the temperature in the reactor during the flow therein exothermic chemical reactions (including at the stage of regeneration of the catalyst), because in order to avoid adiabatic heating of the catalyst required removal of the heat of chemical reactions; limited range of recycled raw materials.

The objective of the present invention is the simplification of regulation and ensuring a more stable temperature modes of the individual devices installation and operation modes of the catalyst in the reactor.

This object is achieved in that the catalytic high octane gasoline fractions and/or aromatic hydrocarbons, C6-C10from raw materials on the basis of hydrocarbons and/or oxygen-containing organic compounds contains a distillation column, reactor blocks for catalytic converted is tnou and separation technology equipment, device for force feeding of liquids and gases.

In Fig. 1 shows the reaction block, which represents a set of technological devices 1-3, combined to feed them in gas cooled flue 4 and which are positioned successively in the direction of travel of the gaseous coolant in the following order: the heat source 3, the reactor shell and tube type 1 and shell and tube heat exchanger 2. When this gas coolant with the preset temperature is prepared by mixing in a ratio of air and flue gases obtained by burning in the heat (3) hydrocarbon fuel gas.

The main distinguishing features of the invention are:

use in the installation of the reactor blocks, each of which consists of sequentially combined flue boiler, reactor shell and tube type and shell and tube heat exchanger;

application for the installation of gas-fluid prepared by mixing air with the combustion gases obtained by burning in the heat of the hydrocarbon fuel gas.

The use of the proposed installation, containing the striated type and shell and tube heat exchanger in which the gas fluid is prepared by mixing air with the combustion gases, obtained by burning in the heat of the hydrocarbon gas, allows to simplify the regulation of the temperature modes of the individual technological devices installation and simplifies the regulation of the reaction temperature in the reactor and provides a better and stable temperature modes of the catalyst (located in the tube space of the reactor) during the flow as endothermic and exothermic chemical reactions.

Simplification of regulation of temperature modes of the individual technological devices in comparison with the installation of the prototype provide by separating the heating systems of distillation columns from the heat supply systems of the reactor blocks, so changing the mode of operation of the same process node setup does not change the operation mode of other technology nodes.

Improvement and stabilization of the temperature modes of the catalyst in the reactor with the flow as endothermic and exothermic chemical reactions provide the possibility of obtaining in the reactor block by mixing in a ratio of air generated in the heat-viscotemp which allows both supply additional heat to the catalyst in the reactor, and eat an excessive amount of heat leakage, respectively endothermic and exothermic chemical reactions. Leakage on the catalyst (in the tube space of the reactor) endothermic chemical reactions (when receiving gasoline fractions and/or aromatic hydrocarbons of the paraffin-naphthenic feedstock) maintaining the process temperature in the pipe space (i.e., preventing the temperature drop due to the chemical absorption of heat) provide the heat supply by feeding annulus reactor gas coolant with a temperature higher than the reaction temperature. During the flow of exothermic chemical reactions (production of gasoline, aromatic hydrocarbons from registergui gases, spirit and ether fractions; at the stage of catalyst regeneration) maintaining the process temperature in the pipe space (i.e., preventing the growth temperature of the reaction due to chemical heat release) provide the surplus heat removal by filing annulus reactor gas coolant with a temperature lower than the reaction temperature.

When the same design reaktoren proposed installation may vary, that allows to process various organic raw materials on the basis of hydrocarbons (oil and gas condensates; virgin and secondary gasoline; petroleum gas, and so on) and/or oxygen-containing compounds (spirit-ether fractions, fusel oils, etc). Depending on the process conditions, the nature of the raw materials, schemes of the nodes of raw material preparation and separation of the products on the installation is possible in addition to high-octane gasoline fractions and/or aromatic hydrocarbons, C6-C10to produce kerosene, diesel fraction and oil. Installation depending on the source of raw materials may not contain, or may contain from 1 to 4 distillation columns for the separation of raw materials. For example, in the processing of hydrocarbon gas or methanol to install does not contain a distillation column for the separation of raw materials; oil processing installation can have up to 4 columns for the fractionation of oil emitting kerosene, diesel fraction, fuel oil and gasoline, then subjected to contacting with the catalyst. When the operation mode of the production of aromatic hydrocarbons installation may not contain (the production of aromatic fractions), and may contain from 1 to 4 RLA, xylenes).

In Fig. 2 for example shows the schematic diagram of the catalytic high octane gasoline fractions and/or aromatic hydrocarbons, C6-C10from hydrocarbon process Zeoforming. In this embodiment, the system includes a technologically bound: distillation columns 5 and 6; heat exchangers and heaters 7, coolers, and condensers 8, separators 9, the vessel 10, the blower 11, the pump 12 and the reactor blocks RB-1, RB-2. Each reactor unit (Fig. 1) contains the combined flue 4 heat 3, shell-and-tube reactor 1 with a stationary catalyst bed shell-and-tube heat exchanger - evaporator-superheater 2. The tube space of the reactor loaded with catalyst reforming. In the diagram (Fig. 2) shows the main process flow: raw material straight-run gasoline fraction I, the reaction products II, hydrocarbon gases III and V, unstable catalysate IV, stable catalysate VI, high-octane gasoline VII, the residual fraction catalyzate VIII, regenerating gas IX, gases regeneration X, XI air, fuel gas XII, gas coolant XIII, exhaust coolant XIV.

The system works as is, working in the mode of production of gasoline RB-1 (RB-2 operates in the regeneration mode of the catalyst). In RB-1 raw I enters the tube space of the evaporator-superheater 2/1, where it is evaporated and overheat to a temperature 340-480oC. From the evaporator-superheater 2/1 overheated raw material is fed into the tube space of the reactor 1/1, which is fixed catalyst bed of reforming IR-30. In the reactor 1/1 catalyst IR-30 as the result of chemical reactions at the reaction temperature 340-480oC and a gauge pressure is the conversion of low-octane components of raw materials into high-octane and gaseous hydrocarbons.

After the reactor 1/1 products of reaction II is cooled and condensed in heat exchange apparatus 7, 8, and separated in separator 9 with the release of hydrocarbon gases III and unstable liquid catalyzate IV. Unstable catalysate IV sent to distillation column stabilizer 5, technologically bound heat exchanger 7, 8 and 9 separating apparatus, where the removal of dissolved gases V. the Bottom of the column 5 assign stable catalysate VI, which is sent to distillation column 6, technologically bound heat exchanger 7, 8, and capacity is irout and take away with the installation of the target product high-octane gasoline VII. The bottom of the column 6 select the residual fraction (FR. > 185oC) catalyzate VIII which take away from the installation as a by-product.

When working RB-1 in the mode of production of gasoline, RB-2 operates in the regeneration mode zakoksovanie in the mode of production of gasoline catalyst. Stage regeneration zakoksovanie catalyst is regulated (at a certain temperature) Vigie coke regenerating gas with a specific oxygen content. Regenerating gas IX served in the tube space of the evaporator-superheater 2/2, where it is heated depending on the mode of regeneration of the catalyst to a temperature of 340 - 540oC. the Heated regenerating gas from the evaporator-superheater 2/2 enters the tube space of the reactor 1/2, where at a temperature of 500 to 550oC is the regeneration process zakoksovanie catalyst. After the reactor gases regeneration XIV dumped on the "candle" or in the chimney.

After the loss of catalytic activity of the catalyst in the reactor 1/1 due to its coking switch feed with RB-1, RB-2, in which Zeoforming raw materials, and RB-1 carry out a stage of regeneration of catalysis of the apparatus and reactor) in each reactor block provide for the expense of feeding them on flues 4 gas carrier with the required temperature (100-600oC). Gas coolant XIII is produced by combustion in furnaces heat 3/1, 3/2 mixture of fuel gas XII with air, followed by mixing in the mixing chambers of the heat-formed high-temperature flue gases with air XI, supplied by the blower 11. Working gas coolant XIII of the heat-3/1, 3/2 on flues 4 comes initially in the annulus of the reactor 1/1, 1/2, and then through gas ducts 4 in the annulus evaporators-superheaters 2/1, 2/2, after which the spent coolant XIV dumped on the chimney. For the supply of an additional quantity of heat to the catalyst in the reactor under reforming flowing generally to the chemical absorption of heat (endothermic heat effect of reaction), annulus reactor serves gas coolant with a temperature of 500-600oC; for removal of excess heat from the reactor released at the stage of catalyst regeneration (exothermic heat effect of reaction), annulus reactor serves gas coolant with a temperature of 300-500oC.

Industrial applicability the present invention is confirmed by the, 2) installation of reforming contains technologically bound: distillation columns 5-6; heat exchangers and heaters 7, coolers, and condensers 8, separators 9, the vessel 10, the blower 11, the pump 12 and the reactor blocks RB-1, RB-2. Each reactor unit contains (Fig. 1) the combined flue 4 heat 3, shell-and-tube reactor 1, a shell and tube heat exchanger evaporator-superheater 2. Pipe space reactors contain stationary layers of catalyst reforming IR-30-1. As raw material installation use a straight run gasoline fraction oil octane PTS 57 MM next fractional composition,oC: N. K. 36, about 10. 62, 50% 107, 90% 180, K. K. 195 and containing, by weight. n-paraffins 35,1, isoparaffins and naphthenes 55,1, aromatic hydrocarbons 9,8.

On the installation (Fig. 2) raw material 1 select a pump of raw capacity and under a pressure of 1.0-1.2 MPa is fed through the heat exchanger in the reactor block RB-1 is initially in the tube space of the evaporator-superheater 2/1, where evaporated and overheat to the reaction temperature (360-460oC), and then into the tube space of the reactor 1/1 loaded catalyst reforming. In the tube space of the reactor 1/1 on zeolite katalizatoriai the conversion of low-octane components of raw materials into high-octane and gaseous hydrocarbons. To compensate for loss of catalyst activity caused by its coking, and maintaining the composition and quality of products at the same level, the process of reforming carried out gradually, in the course of 150 hours, the rise of the reaction temperature: the initial temperature of the reaction 360oC, end 460oC. After the loss of catalytic activity of the catalyst in the reactor 1/1 due to its coking (after 150 h of operation) and reached the final reaction temperature switch feed with RB-1, RB-2, in which Zeoforming raw materials, and RB-1 exercise stage of catalyst regeneration. After coking of the catalyst in the reactor 1/2 switch feed from RB-2 RB-1, and so on)

After the reactor, the reaction products II cool and condense in the respective heat-exchange equipment and sent to the capacity of the separator for the separation of hydrocarbon gases III from the liquid unstable catalyzate IV. Unstable catalysate IV from the tank separator selected pump and directed through the heat exchanger where it is heated to a temperature of 100oC, in a distillation column stabilizer 5, where under a pressure of 0.8 MPa is the release of dissolved gases from the gasoline the support and partially condense in the condenser and serves in the capacity of the separator for the separation of hydrocarbon gases V; liquid distillate from the tank separator return in column 5 in the form of cold irrigation. Bottom stabilizer 5 at a temperature of 120oC select stable catalysate VI, part of which is heated in the heat exchanger to a temperature of 150oC and return in column 5 as a "hot jet", and the carrying portion is fed through a heat exchanger where it is reheated to 200oC, in a distillation column 6, where, under the pressure of 0.2 MPa is divided stable catalyzate emitting gasoline fractions (FR. 35-195oC) and residual fraction (FR. > 185oC). From the top of the rectifying column 6 at a temperature of 140oC select a pair of gas, which is cooled and condensed in the condenser and sent to the reflux tank, where the gasoline is fed to the column 6 as cold irrigation, and the carrying portion away from the installation as a target product unleaded high-octane gasoline VII. The bottom of the column 6 at a temperature of 220oC select the residual fraction catalyzate, which partially directed through the heater, where it is reheated to a temperature of 240oC, in column 8 as a "hot jet", and the carrying portion served in a heat exchanger for cooling, and then the PS III and V, or take away from the installation in the quality of products, or use it fully or partially as fuel gas for power supply installation.

When working RB-1 mode seafarming production of gasoline, RB-2 operates in the regeneration mode previously zakoksovanie catalyst, consisting in a regulated Vigie coke deposits regenerating gas with a specific oxygen content. Regenerating gas IX served in the RB-2, originally in the tube space of the evaporator-superheater 2/2, where it is heated to a temperature of 380oC, and then into the tube space of the reactor 1/2, where at a temperature of 500-540oC is the regeneration of the catalyst. After the reactor exhaust gases regeneration X dumped on the "candle" or in the chimney.

Maintaining the temperature of the modes of operation of the catalyst in the reactors 1/1, 1/2 and heating is supplied in the pipe space evaporators-superheaters 2/1, 2/2 material flows (raw materials, regenerating gas) in each reactor block provide for the expense of feeding them on flues 4 gas coolant XIII, which is obtained by mixing in a ratio in the mixing chambers of the heat-3/1, 3/2 high temperature flue gas generated in Teploenergo the first coolant XIII of the heat-3/1, 3/2 on flues 4 comes initially in the annulus of the reactor 1/1, 1/2, and then through gas ducts 4 in the annulus evaporators-superheaters 2/1, 2/2, after which the spent coolant XIV drop in the chimney.

Under reforming stage production of gasoline, the temperature of the catalyst in the reactor by supplying an additional amount of heat to the catalyst (to compensate for the temperature drop process due to the chemical reaction with the endothermic heat effect) provide feed annulus reactor gas coolant with a temperature of 500 - 600oC. At the stage of regeneration of the catalyst temperature of the catalyst by removal of excess heat (to prevent the growth temperature of the reaction due to chemical heat caused by the exothermic heat effect of reaction) provide feed annulus reactor gas coolant with a temperature of 400 to 500oC.

In the processing of straight-run gasoline with an octane rating of 57 MM in the described setup this way from the source of raw materials orodnik gases 36,5% Gasoline fraction has an octane rating of 85.4 MM and 93.8 THEM and contains to 8.1 wt. n-paraffins, 41,3% isoparaffins and naphthenes, 50,6% aromatic hydrocarbons, C6-C10(including C63,5; C714,6; C821,6; C910,2; C100,7); the total yield of aromatic hydrocarbons is 30.7 wt.

Example 2. Catalytic high octane gasoline contains technologically bound: distillation column; heat exchangers and heaters, coolers, and condensers, separators, tanks, blower, pumps and reactor block, similar to the reactor blocks of example 1. As raw material process using methanol raw with a water content of 7 wt.

On the plant raw materials are selected pump from the raw material tank and fed through a recuperative heat exchanger where it is heated by the heat of reaction products, in the tube space of the evaporator-superheater reactor building, where it is evaporated and overheat to a temperature of 360oC, and then is directed into the tube space of the reactor for contact with the catalyst. In the reactor at the reaction temperature 400oC, a pressure of 0.2 MPa and the weight of the feed rate of the raw material 2 h-1at the stationary layer of zeolite-containing catalyst IR-28 is the transformation of raw materials (methanol) in the hydrocarbon, water and condense in the cooler-condenser and sent to a three-phase separator for separating gaseous reaction products, liquid hydrocarbons (catalyzate) and water. Water from the phase separator are taken from the bottom layer and away from the installation.

The liquid hydrocarbon reaction products (produce) from the three-phase separator select the pump with the upper layer and serves through prepodavatel in a distillation column. From the top of the column select gas-vapor mixture, which is cooled in the refrigerator and sent to a separator for separating hydrocarbon gases from gasoline. Hydrocarbon gases from the separator away from the installation, part of the gas from the separator is served in a distillation column as irrigation, and the carrying portion of the gasoline doxological in the refrigerator and take away with the installation of the target product unleaded high-octane gasoline. The bottom of the distillation column select residual fraction catalyzate (FR. > 185oC) partially directed through the heater in column 8 as a "hot jet", and the carrying part is cooled in the refrigerator and away from the installation as a by-product.

After the loss of catalyst activity due to coking (over 400-500 hours) carry out the regeneration of the catalyst as in example 1.

About generiruemyi gas), as well as the temperature of the catalyst in the reactor by venting excess heat (to prevent the growth temperature of the reaction due to chemical heat caused by the exothermic heat effects of the reaction at the stage of conversion of methanol and at a stage of regeneration of the catalyst) is carried out analogously to example 1. The temperature in the annulus of the reactor gas coolant 380oC at the stage of conversion of methanol and 400 to 500oC at the stage of catalyst regeneration.

As a result of processing of crude methanol described in the installation this way, from the initial material as a whole get, wt. water 47,7; hydrocarbon gases 19,1; residual fraction > 185oC 1,7; high-octane gasoline fraction 35-195oC 31,5 (including aromatic hydrocarbons, C6-C1018,5). The yield of hydrocarbon products, wt. hydrocarbon gases 36,6; residual fraction of 3.2; high-octane gasoline fraction 60,2 (including aromatic hydrocarbons and 36.2). Gasoline fraction contains 1.8 wt. n-paraffins, 39.5% of isoparaffins and naphthenes, 58.7% of aromatic hydrocarbons, C6-C10(including C60,8; C711,5; C823,2; C915,1 is oxooctanoate gasoline fractions and aromatic hydrocarbons, C6-C10contains technologically bound: the heat exchanger, a cooler-condenser, the capacity of the separator, compressor, blowers and two reactor units of RB-1, RB-2, a similar reactor blocks of example 1. As raw material units use propane-propylene fraction containing C3H825% C3H675 wt.

Raw materials serves compressor initially in the heat exchanger, where it is heated by the heat of reaction products, and then in the reactor block RB-1, originally in the tube space of the superheater, and then into the tube space of the reactor for contact with a zeolite-containing catalyst IR-30-1. This RB-2 operates in the regeneration mode of the catalyst.

In the tube space of the reactor at the reaction temperature 400oC, a pressure of 0.5 MPa and the weight of the feed rate of raw material 3 h-1on the fixed catalyst bed is the transformation of raw materials with the formation of the reaction product of the following composition, wt. H20.1; paraffins C10,1; C21,2; C346,8; i-C44,3; n-C48,2; C5+3,7; olefins, C2-C43,4; aromatic C61,7; C79,3; C813,1; C95,5; C10+2,6.

After the reactor products contactyou the condenser and serves in the capacity of a separator for separating gaseous hydrocarbons from the liquid catalyzate gasoline fractions (FR. N. K. 220oC), which is the target product installation.

After the loss of catalytic activity of the catalyst in the reactor RB-1 due to its coking (after 40-60 hours of operation) switch feed with RB-1, RB-2, in which the transformation of raw materials, and RB-1 exercise stage regeneration of catalyst as in example 1. After coking of the catalyst in the reactor RB-2 switch feed from RB-2 RB-1, etc.

The provision of heat supplied to the tube space superheaters reactor units of material flows (raw materials, regenerating gas) and the temperature of the catalyst in the reactor by venting excess heat (to prevent the growth temperature of the reaction due to chemical heat caused by the exothermic thermal effects of reactions and phase transformations of raw materials and at the stage of regeneration of the catalyst) is carried out analogously to example 1. The temperature in the annulus of the reactor gas coolant 380oC under transformation of raw materials and 400-500oC at the stage of catalyst regeneration.

In the processing described political hydrocarbon, C6-C1032,2 (including C61,7; C79,3; C813,1; C95,5; C10+2,6). The obtained aromatic fraction has an octane number of 98 PTS MM and can be used as a high-octane component of gasoline or as raw material for the selection of individual aromatic hydrocarbons.

1. Catalytic high octane gasoline fractions and/or aromatic hydrocarbons from a feedstock hydrocarbon-based and/or organic oxygen-containing compounds containing reactor blocks, consisting of the combined flue boiler, heat exchangers and catalytic reactor containing a distillation column and technologically tied with columns and reactor heating units, heat exchangers, vessels, separating technological equipment and devices for force feeding of liquids and gases, characterized in that each reactor unit contains sequentially arranged in the direction of the gas-coolant heat source, the reactor shell and tube type and shell and tube heat exchanger.

2. Installation under item 1, characterized in that the gas coolant in the reactor block floor is

 

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