Installation of catalytic conversion of light hydrocarbons

 

The invention relates to an integrated device for the production of a component of high-octane gasoline and aromatic hydrocarbons. The unit can be used both on the production and primary processing of oil and gas condensate, and independent operations. Catalytic processing of a light hydrocarbon feedstock includes a unit for production of aromatic concentrate, containing regenerative heat exchanger, a furnace and a catalytic reactor, the resultant catalysate which through recuperative heat exchanger is connected with a fridge, connected in turn with the separator. At the exit of the liquid phase from the separator is "hot" separator, is provided in the lower part of the coil for the Stripping of light hydrocarbons in the upper part of the centrifugal elements to capettini. The installation also includes a power receiving component of high-octane gasoline comprising a regenerative heat exchanger, furnace, catalytic reactor, a fridge, a separator and a hot separator, is provided in the lower part of the coil for Stripping the propane-butane fraction in the upper part of the centrifugal elements to capettini. Output propane-butanone reactor block for aromatic concentrate through the recuperative heat exchanger and furnace. Technical result: simplifying installation, simultaneous production of high-octane gasoline and aromatic hydrocarbons. 4 C.p. f-crystals, 1 Il.

The invention relates to an integrated device for the production of a component of high-octane gasoline and aromatic hydrocarbons by catalytic processing of organic raw materials. The unit can be used both on the production and primary processing of oil and gas condensate, and independent operations.

Known catalytic refining gasoline fractions to increase their octane number. This system includes a furnace for heating and evaporation of raw materials, catalytic reactors adiabatic type for the chemical transformation of raw materials, 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" (see RF patent 2098173, op. 10.12.97,, IPC C 10 G 35/04).

The common features of known and proposed facilities as follows: - anouki are: - the complexity of the technological scheme; - relatively high losses in the calculation of raw materials, because the processing is subjected to only the liquid raw material, the propane-butane fraction output as a by-product; - the use of flue gas as a regenerating gas needs to be cleaned from soot, which is inevitably formed during the combustion of hydrocarbon gas, which requires the installation of expensive fine filter and leads to a decrease in the activity of the catalyst during regeneration; - the use of a distillation column, which also complicates the process.

Known installation method of processing aliphatic hydrocarbon, C2-C12in aromatic hydrocarbons or high-octane gasoline, which is the closest to the technical essence and the achieved result to offer (see RF patent 2175959, op. 20.11.01,, IPC C 07 C 2/02; 2/76). The apparatus comprises a reactor, furnace, heat exchangers, coolers, separators and stabilization column, connected by pipelines.

The common features of known and proposed facilities:
- bake;
catalytic reactor;
- recuperative heat exchanger;
- refrigerator;
- gas separator;
the resultant catalysate of kataliticheski what eparation.

The disadvantages of the known installations lie in the complexity of the technological scheme in General, the complexity of the design of a catalytic reactor and not high enough efficiency in the use of complex distillation equipment. Carrying out the reaction of aromatization of hydrocarbons2-C4on the first shelf of the reactor leads to the formation of aromatic products6-C10which are then fed to the second shelf of the reactor, where the transform straight-run gasoline. Coming on top of aromatic products, in particular naphthalene, inevitably chemisorbents on the catalyst on the second shelf, because the layer is supported by a lower temperature 360oWith against 640oOn the first shelf. This leads to additional coking of the catalyst and reduction of the reaction cycle. The complex construction of the reactor creates difficulties when loading and unloading the catalyst. In addition, the catalyst in the first zone will lose activity under more severe conditions of the process much earlier than in the second zone, which will require its regeneration when still quite active catalyst in the second zone. All this leads to lower efficiency of the reactor. When the installation is impossible ro2-C4requires, according to literature data, a lower pressure than the processing of straight-run gasoline in the second zone.

The technical task of the invention is to simplify the regulation and provision of efficient and stable operation, receiving at the same time high-octane gasoline and aromatic hydrocarbons, as well as reduced capital and operating costs.

This object is achieved in that the catalytic processing of light hydrocarbons containing block for aromatic concentrate, containing regenerative heat exchanger, a furnace and a catalytic reactor, the resultant catalysate which through recuperative heat exchanger is connected with a fridge, connected in turn with the separator, at the outlet of the liquid phase from the separator is additionally installed hot separator, is provided in the lower part of the coil for the Stripping of light hydrocarbons in the upper part of the centrifugal elements to capettini, in addition, the installation is further provided with a block of high octane gasoline comprising a regenerative heat exchanger, furnace, catalytic reactor, refrigerator, g and in the upper part of the centrifugal elements to capettini, the yield of propane-butane fraction from the hot separator unit producing high-octane gasoline is connected to a catalytic reactor unit for aromatic concentrate through the recuperative heat exchanger and furnace of this block.

In addition, at the outlet of the liquid phase from the hot separator unit for aromatic concentrate is additionally equipped with a refrigerator and a carbon filter.

In addition, the output of the gas phase from the hot separator unit for aromatic concentrate is additionally equipped with a refrigerator and a separator, the liquid phase from the separator is connected with the inlet of a carbon filter that block.

In addition, at the outlet of the liquid phase from the hot separator unit producing a component of high-octane gasoline is additionally equipped with a refrigerator and a carbon filter.

The furnace unit for aromatic concentrate is equipped with two single coils and automatic regulation of the flow rate of the propane-butane fraction in each coil, and the output of one coil is connected with the top of the catalytic reactor unit for aromatic concentrate, and the output of the second coil is connected with the average hours the particular features of the invention enables processing of gaseous raw materials for small block installations directly on the oil, gas condensate, or gas in remote areas of the Far North and Eastern Siberia, as well as simplifies the regulatory process, since no installation is composed of complex distillation and reactor equipment, and ensures efficient and stable operation of the apparatus setup. In addition, there is a sharp decrease in losses of hydrocarbons From3-C4and improving the efficiency of use of all raw materials. On installation it is possible to independently process a certain type of raw material and receive simultaneously a component of high-octane gasoline and aromatic concentrate.

The drawing shows a schematic diagram of catalytic processing of light hydrocarbons containing block for aromatic concentrate, including the United pipelines recuperative heat exchanger 1, the furnace 2 and the catalytic reactor 3. The resultant catalysate from the reactor 3 is connected through a recuperative heat exchanger 1 with the refrigerator 4, which in turn is connected to the separator 5. At the exit of the liquid phase from the separator 5 has a hot separator 6, is provided in the lower part of the coil for Stripping light Uglevodorody 6 installed refrigerator 7 and a carbon filter 8. The plant is equipped with a power receiving component of high-octane gasoline comprising interconnected by pipelines recuperative heat exchanger 9, the furnace 10 and the catalytic reactor 11.

The resultant catalysate from the reactor 11 through the recuperative heat exchanger 9 is connected to the refrigerator 12, which in turn is connected to the separator 13. At the exit of the liquid phase from the separator 13 is "hot" separator 14, is provided in the lower part of the coil for Stripping the propane-butane fraction and in the upper part of the centrifugal elements to capettini. At the exit of the liquid phase from the hot separator 14 includes a fridge 15 and a carbon filter 16. At the exit of the gas phase from the hot separator 6 is equipped with a refrigerator 17 and the separator 18. The output of the liquid phase from the separator 18 is connected to the input in charcoal filter 8. The plant is equipped with tanks 19, 20, 21 and pumps 22, 23 and 24.

The furnace 2 has two single coils and automatic regulation of the flow rate of the propane-butane fraction in each coil, and the output of one coil is connected with the top of the catalytic reactor 3, and the output of the second coil is connected to the middle part of the reactor for uniform temperature in the catalyst layer is recuperative heat exchanger 9, where it is heated by the heat of reaction products to 190-240oWith, and then into the oven 10. From the furnace 10 raw materials with temperature 330-480oC and a pressure of 1.0-1.2 MPa in the form of a vapor-gas mixture enters the catalytic reactor 11 adiabatic type, filled with high zeolite-containing catalyst. In the reactor 11 at a temperature of 330-460oC and a pressure of 1.0-1.2 MPa is in the process of conversion of low-octane components of straight-run gasoline fraction in the high-octane due to the catalytic isomerization and paraffin aromatization and dehydrogenation of naphthenic hydrocarbons. The reaction products from the reactor 11 are recuperative heat exchanger 9, in which direct heat flow, cooled in the refrigerator for 12 industrial water up to 40-45oWith and into the separator 13. From the top of the separator 13, the dry gas is sent to the fuel system (up to 3% for raw materials). Unstable produce from a bottom of the separator 13 enters the hot separator 14. Cube separator 14 is embedded a coil which is supplied with hot coolant. Hot separator 14 at a temperature of 80-120oC and a pressure of 0.5 MPa from catalyzate allocated gaseous reaction products - propane-butane fraction. Bottom "goik 15, where is cooled to 40oWith production water. Then produce coal passes 16 of the filter, where the adsorption process selection resinous substances from catalyzate. After the filter can produce a component of high-octane gasoline) is collected in the tank 20 and the pump 23 is pumped into the warehouse.

The propane-butane fraction from the hot separator 14 passes through recuperative heat exchanger 1 where it is heated to 240-260oWith due to the heat of reaction products leaving the reactor 3. Then the propane-butane fraction is fed into the furnace 2 for heating up 450-570oC. In the reactor 3 in the presence of a zeolite catalyst at a temperature of 450-570oC and a pressure of 0,4-0,45 MPa process for the aromatization of propane-butane fraction. Products from the reactor 3 are annulus of the heat exchanger 1, proceed in a water cooler 4, where they are condensed at a temperature of 40oWith and sent to the separator 5 for phase separation. The gas phase from the top of the separator 5, containing primarily hydrogen (80%) and hydrocarbons (C1-C2that goes to the fuel system. Unstable liquid catalysate with the bottom of the separator 5 is sent to a hot separator 6, snabjennyi aromatic concentrate light hydrocarbons. Maintaining the temperature of 60-100oC and a pressure of 0.1-0.2 MPa in the hot separator is Stripping hydrocarbons From3-C4aroma concentrate. Gas stabilization of the hot separator 6, achladies in the refrigerator 17, is supplied to the separator 18 from which it is fuel network. From the bottom of the separator 6 aromatic concentrate enters the water cooler 7 where it is cooled to 30-40oWith production water. Then produce through a carbon filter 8 is directed into the container 21, and a pump 24 at the warehouse. The liquid phase from the bottom of the separator 18 is directed to the Association with catalyzate directed to a carbon filter 8. In the process of installation is a decrease in the activity of the catalyst due to coke deposition on its surface. Therefore, to restore the initial activity of the catalyst conduct its regeneration. Regeneration is the burning of coke from the surface of contact of the nitrogen-air mixture at a temperature 280-550oC. For this part of the unit includes membrane unit for receiving nitrogen purity up to 99.5%. Regeneration of the nitrogen is fed into the furnace 2 and 10, is heated to 280oC and fed to the catalyst with a specified flow rate. In perature in the oven. The final stage of regeneration is the air supply to the catalyst at 550oC.


Claims

1. Installation of catalytic conversion of light hydrocarbons containing block for aromatic concentrate, containing regenerative heat exchanger, a furnace and a catalytic reactor, the resultant catalysate which through recuperative heat exchanger is connected with a fridge, connected in turn with the separator, characterized in that at the outlet of the liquid phase from the separator is additionally installed hot separator, is provided in the lower part of the coil for the Stripping of light hydrocarbons in the upper part of the centrifugal elements to capettini, in addition, the installation is further provided with a power receiving component of high-octane gasoline comprising a regenerative heat exchanger, furnace, catalytic reactor, refrigerator, the separator and a hot separator, is provided in the lower part of the coil for Stripping the propane-butane fraction and in the upper part of the centrifugal elements to capettini with the propane-butane fraction from the hot separator unit producing a component of high-octane by the heat exchanger and the furnace of this block.

2. Installation under item 1, characterized in that at the outlet of the liquid phase from the hot separator unit for aromatic concentrate is additionally equipped with a refrigerator and a carbon filter.

3. Installation on PP.1 and 2, characterized in that at the outlet of the gas phase from the hot separator unit for aromatic concentrate is additionally equipped with a refrigerator and a separator, the liquid phase from the separator is connected with the inlet of a carbon filter that block.

4. Installation on PP.1-3, characterized in that at the outlet of the liquid phase from the hot separator unit producing a component of high-octane gasoline is additionally equipped with a refrigerator and a carbon filter.

5. Installation on PP. 1-4, characterized in that the heater block for aromatic concentrate is equipped with two single coils and automatic regulation of the flow rate of the propane-butane fraction in each coil, and the output of one coil is connected with the top of the reactor block for aromatic concentrate, and the output of the second coil is connected to the middle part of the reactor for uniform temperature in the catalyst bed.

 

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FIELD: petrochemical processes.

SUBSTANCE: high-octane fuels and propane-butane fraction are obtained via conversion of hydrocarbon feedstock on contact with hot catalyst placed in reactor, into which diluting gas is supplied at elevated pressure. Catalyst is Pentasil-type zeolite with general formula xM2/nO,xAl2O3,ySiO2,zMe2/mO wherein M represents hydrogen and/or metal cation, Me group II or VII metal, n is M cation valence, m is Me metal valence, x, y, z are numbers of moles of Al2O3, SiO2, and Me2/mO, respectively, and y/x and y/z ratios lie within a range of 5 to 1000. Metal oxide Me2/mO is formed during calcination, in presence of oxygen, of Me-containing insoluble compound obtained in zeolite reaction mixture.

EFFECT: increased octane number of gasoline fractions with propane-butane fraction as chief component of gas products, and prolonged inter-regeneration time of catalyst.

11 cl, 4 dwg, 3 tbl, 16 ex

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