Catalyst and a method for production of high-octane fuels and propane-butane fraction using this catalyst

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

 

The present invention relates to methods for high-octane fuels and propane-butane fraction by processing of hydrocarbon raw materials on the basis of a predominantly aliphatic hydrocarbon, C2-C12in particular, gas condensates and straight-run gasoline, and catalysts for producing high-octane fuels and propane-butane fraction. The invention can be used in the refining and petrochemical industry.

Known catalysts for the conversion of aliphatic hydrocarbons, C2-C12are zeolites. There are several ways of obtaining high-octane gasoline or aromatic hydrocarbons from hydrocarbon feedstock, where as an active ingredient often act pentasil with the structure of ZSM-5 or ZSM-11 or zeolite type Y. To increase the octane number of the resulting product catalysts promotirovat metals or their oxides (usually noble or rare earth metals and zinc, gallium, iron, magnesium, cobalt, molybdenum). In addition, as modifiers can be phosphide, and fluoride zinc, cremniter and some other compounds. Content promoting component is from 0.1 to 15 %. The modifying agent is introduced either during the synthesis or by postsinapticheskih processing (impregnation salts according to the corresponding metals, mechanical mixing zeolite with the promoter). For forming catalyst can be used from 10 to 90% of the binder.

A known catalyst for the conversion of aliphatic hydrocarbons, C2-C12in high-octane gasoline or aromatic hydrocarbons (RF patent No. 2148431, 1998 CL 01 J 29/40)containing 50-75 wt.% zeolite, 0.9 to 5.0 wt.% phosphide of zinc, a binder component (Al2O3) - the rest. Modification of zinc and phosphorus carried out by a method of mixing salt phosphide zinc zeolite.

A known catalyst for the conversion of aliphatic hydrocarbons, C2-C6in high-octane gasoline or aromatic hydrocarbons (RF patent No. 2155099, 1998 CL 01 J 29/40). The catalyst contains a zeolite type pentasil with silicate module SiO2/Al2O3=35-50 modified with fluoride zinc. Zinc-containing catalyst produced by the method of mixing the powder decationizing of zeolite and zinc fluoride, followed by molding with aluminum oxide as a binder. As a result, the catalyst has the following components: zeolite - 60-75 wt.%, fluoride zinc - 1,4-4.6 wt.%, binding - rest.

A significant drawback of the above catalysts is the fact that modification methods used do not allow to obtain a fine distribution of the active components is NTA, resulting in reduced efficiency of its use.

A known catalyst for the conversion of aliphatic hydrocarbons, C2-C12in high-octane gasoline or concentrate of aromatic hydrocarbons containing zeolite group pentasil a molar ratio of SiO2/Al2O3=20-150 and oxides of zinc, iron, magnesium and calcium. Metals-promoters introduced into the catalyst or zeolite to ion exchange with solutions of the corresponding salts in the form of oxides or salts that decompose upon calcination, when mixing the catalyst mass or impregnation of the catalyst with a solution of salts (patent RF №2169043, 2000, CL 01 J 29/46).

The disadvantage of this catalyst is to use multiple modifiers, sequentially deposited on the catalyst, which increases the number of intermediate stages of preparation of the catalyst.

Closest to the proposed catalyst is a catalyst containing oxides of silicon, aluminum and zinc where zinc forms part of the crystal lattice of the catalyst (U.S. patent No. 6177374, 2001, CL 01 J 029/06). Porous crystalline catalyst has a General formula of M2/nO, l2O3, SiO2, zZnO, where M is the proton and/or a metal cation, n is the valence of the cation, x, y and z represent the number of moles of Al2About3, SiO2, ZnO, respectively. Respect to the deposits y/x and y/z are in the range of 5-1000. The process of preparation of the catalyst is to obtain a reaction medium consisting of water, a source of silicon, a source of aluminum, soluble salts of zinc and source of the structure-forming agent having an organic cation. The reaction mixture is heated in the temperature range from 80 to 230°C, then selected the solid residue is heated to temperatures above 400°C to remove organic compounds. The catalyst has a zeolite with structure type MFI (ZSM-5), in which zinc is part of the crystal lattice.

The disadvantage of this catalytic system is that stated by the authors of the zeolite ZSM-5 with atoms of zinc frame by calcination to remove the organic template is the output of zinc atoms from the lattice. This process is accompanied by partial destruction of the zeolite framework to the formation of defects that violate the regularity of the porous structure.

Obtaining high-octane fuels from hydrocarbon containing C2-C12hydrocarbons, is a complex process involving the reactions of cracking, isomerization, aromatization, alkylation, etc. in Addition to liquid gasoline fraction are formed propane-butane fraction (LPG), as well as ethane and methane. The efficiency of the process is higher, the greater the yield of liquid fraction. In the gas phase is predpochtitelno to have the propane-butane fraction, which can also be used as fuel. Methane and ethane are the least valuable products, the output of which should be minimized.

The process is carried out in the presence of a catalyst at temperatures of 350-650°C., a pressure of 1-40 ATM, the speed of feed of 0.1-10 h-1. The process may be carried out in an atmosphere of hydrogen containing gas, and hydrogen-free technology, where as the diluent gas are nitrogen, inert gases or C2-C3hydrocarbon gases. The target octane of the product depends on a balanced content of aromatic, cyclic, branched and unbranched hydrocarbons.

A method of obtaining gasoline fractions, in which the increase knock resistance of gasoline is achieved through the use of aluminosilicate catalyst composition (0,02-0,32)PA2Al2O3(0,003-2,4)EnAboutm(28-212)SiO2where enAboutm- one or two oxide elements II, III, V, VI, VIII groups of the periodic system, or aluminosilicate of the composition applied to the carrier in the amount of 30-70%, or a catalyst of the composition, modified of 0.05-0.5 wt.% palladium. Tests have shown an increase in the octane number of gasoline from 65 to 96 units on the research method (A.S. No. 1325892 A1, 1984., CL 10 G 11/05, 01 J 29/30).

A method of obtaining high-octane gasoline and aromatic hydrocarbons (RF patent No. 2141993, 1998 CL 10 G 035/095, 01 J 29/06, 29/86). Aliphatic paraffins and olefins, C2-C12contact with a catalyst containing 50-75 wt.% zeolite, 0.9 to 5.0 wt.% phosphide of zinc, a binder component (Al2About3) - the rest. The contacting is carried out at 280-580° C, 0.15 To 2.0 MPa and space velocity of the raw material of 0.5 to 5.0 h-1.

There is a method of transformation of aliphatic hydrocarbon, C2-C6in high-octane gasoline or aromatic hydrocarbons (see RF patent №2155099, 1998 CL 01 J 29/40, With 10 G 035/095//(B 01 J 29/40, 103:20, 105:50, 101:32)). The catalyst contains a zeolite type pentasil with silicate module SiO2/Al2O3=35-50 modified with fluoride zinc. The conversion of aliphatic hydrocarbons to high octane gasoline or aromatic hydrocarbons in the presence of this catalyst is carried out in the temperature range 280-550° C, pressure of 0.15-2.0 MPa and space velocity of the gaseous raw material 360-1200 h-1.

The disadvantage of the above methods is small duration mezhregionalnogo mileage, which necessitates frequent oxidative regenerations.

There is a method of refining gasoline, when the process is carried out at elevated t is perature and pressure, preferably at 200-400° C, a pressure of 0.1-1 MPa, the catalyst containing 0.5-5 wt.% sverkhvysokochastotnogo zeolite type pentasil a molar ratio of silicon oxide to aluminum oxide, equal 25-90, amorphous silica-alumina basis. As the modifier can act as the oxides of zinc or gallium (RF patent No. 2049806, 1994, CL 10 G 35/095, 01 J 29/40).

The disadvantage of this method is a slight increase in the octane number of the product, due to the low content of the zeolite component in the catalyst.

Closest to the proposed method to the technical essence is a method of obtaining LPG and high octane aromatic products from low-value hydrocarbons on the catalyst containing the oxides of silicon, aluminum and zinc where zinc forms part of the crystal lattice of the catalyst (U.S. patent No. 5961818, 1999, CL 10 G 035/095). Porous crystalline catalyst has a General formula of M2/nO, l2About3, ySiO2, zZnO, where M is the proton and/or a metal cation, n is the valence of the cation, and x, y and z represent the number of moles of Al2O3, SiO2, ZnO, respectively. Relationship y/x and y/z are in the range of 5-1000.

The process of obtaining LPG and high octane aromatic products from low-value hydrocarbons is carried out in the range rate is the atur 300-600° C, a pressure of from 1 to 30 atmospheres, a feed rate of the raw material 1 to 10 h-1and a molar ratio of nitrogen/hydrocarbon from 1 to 4.

The advantages of this method include the insensitivity of the catalyst to changes in the composition of hydrocarbons, hydrogen-free technology, serologically active component. In addition, we observed no loss of activity for at least after 17 regenerations, which is explained by the method of preparation of the catalyst, stabilizing the zinc and to avoid entrainment in the reducing environment of the process.

The disadvantage of this method is the instability of the composition of the products from the first hours of the process. The reduction of the conversion of raw materials 2.7% for 3 hours the reaction shows a significant rate of deactivation of the catalyst. This effect is connected with the peculiarities of synthesis and pretreatment of the catalyst. The output of zinc atoms from the zeolite lattice during annealing leads to the formation of defects, which serve as active centers of coke formation. In addition, the formed particles of zinc oxide prevent the movement of bulk molecules in the pores of the zeolite, gradually blocking the output of products.

The present invention is directed to an improvement in the processing of hydrocarbon raw materials, increasing the octane number of esinovich fractions, getting the propane-butane fraction as the main component of the gaseous products and the increase mezhregionalnogo mileage catalyst through the use of a specific catalyst composition.

The problem is solved in that the catalyst comprising a zeolite of type pentasil with the General formula hmm2/nOh, l2About3, SiO2, zMe2/mO, where M is the proton and/or a metal cation, x, y, z - the number of moles of Al2O3, SiO2, Me2/mO, respectively, the relationship of y/x and y/z are in the range of 5-1000, Me - metal II or VIII groups of the periodic system, n is the valence of cation M, m is the valence of the metal Me, according to the invention, the metal oxide IU2/mO formed in the calcination in the presence of oxygen IU-containing insoluble compounds obtained in the reaction medium for the synthesis of zeolite. The preparation of the catalyst in this way leads to a highly dispersed distribution of the modifier, without affecting the crystal structure of the zeolite.

The metal oxide IU2/mOh, where Me is the metal (II) or (VIII groups of the periodic system, in particular, formed as the result of annealing in the presence of oxygen IU-containing insoluble sulfide or oxalate obtained in the reaction medium for the synthesis of zeolite. Such sulfides or oxalate insoluble in water and is egco are formed by the interaction of the metal ion Me and sulfide or oxalate ion. Metal Me, in particular, are zinc or Nickel, has established itself as the active components of many processes of hydrocarbon processing. The proposed catalyst can be used with a binder necessary for forming and giving the required strength characteristics of the granules of the catalyst.

The problem is solved in a method of producing high-octane fuels and propane-butane fraction by conversion of hydrocarbons in the feed and contacting the heated catalyst comprising a zeolite of type pentasil with the General formula hmm2/nOh, l2About3, ySiO2, zMe2/mO, where M is the proton and/or the cation of the metal, Me is a metal II or VIII groups of the periodic system, n is the valence of cation M, m is the valence of the metal Me, x, y, z - the number of moles of Al2O3, SiO2, Me2/mO, respectively, the relationship of y/x and y/z are in the range of 5-1000 placed in the reactor, which serves gas diluent at elevated pressure, according to the invention, the catalyst contains a metal oxide IU2/mOh, which is formed in the calcination in the presence of oxygen IU-containing insoluble compounds obtained in the reaction medium for the synthesis of zeolite.

The proposed method, with all the advantages of the prototype, ceteris paribus allows the t with the best stability to obtain a product with a higher octane due to the high dispersion and homogeneous distribution of the modifier IU 2/mAbout while maintaining the structural integrity of the zeolite. The gas phase (C1-C4hydrocarbons) consists mainly of propane and butane, methane and ethane is insignificant and is not more than 2 wt.%.

The catalyst is heated to a temperature of 350-500° C, gas diluent serves under the pressure of 1-30 ATM, the feed rate is chosen in the range of 0.5-10 h-1. The variation of these process conditions can deliberately get different types of fuels.

As the diluent gas is used, in particular methane, which significantly reduces the cost of the product in the process for the production of natural gas and gas condensate. The ratio of the gas-solvent/raw material varies in the range 1-50, the use of higher ratios impractical due to losses in the amount of condensed liquid fraction. As hydrocarbons, in particular, use gas-condensate or naphtha having a low octane number and require additional processing for use as fuels.

The proposed method makes it possible to obtain two hydrocarbon product is high - octane gasoline fuel with an octane rating of between 80 and 96 (research method) and propane-butane fraction. The duration of catalyst without regeneration SOS is to place more than 400 hours, oxidative regeneration fully restores it to its original activity. The simplicity of the method, hydrogen-free technology, the use of natural gas as a diluent, the insensitivity of the catalyst to sulfur-containing compounds makes it possible to use the proposed method as in refineries, and in situ production of oil and gas condensate.

Further, the invention is illustrated with specific examples of its implementation and the accompanying drawings, on which:

figure 1 shows the change in the content of aromatics in time for the proposed catalyst and the two catalysts are compared.

figure 2 - change the content of hydrocarbons of normal structure;

figure 3 - change the content of cyclic hydrocarbons and ISO-structure;

figure 4 - change the content of the propane-butane fraction.

The catalyst according to the invention is a zeolite of type pentasil with the General formula hmm2/nOh, l2About3, ySiO2, zMe2/mO, where M is the proton and/or the cation of the metal, Me is a metal II or VIII groups of the periodic system, n is the valence of cation M, m is the valence of the metal Me, x, y, z - the number of moles of Al2O3, SiO2, Me2/mO, respectively, the relationship of y/x and y/z nahodatsa is in the range of 5-1000. The metal oxide IU2/mAbout formed in the calcination in the presence of oxygen IU-containing insoluble compounds obtained in the reaction medium for the synthesis of zeolite.

The metal oxide IU2/mOh, where Me is the metal (II) or (VIII groups of the periodic system, in particular, formed in postsinteticescuu oxidation of Metal-containing sulfide obtained in the reaction medium to the stage of synthesis of the zeolite. The metal is zinc or Nickel.

The synthesis of the catalyst is to obtain a reaction medium consisting of water, a source of silica (sodium silicate), aluminum (aluminum sulfate), source metal Me II or VIII group of the periodic system (water-soluble salt of zinc or Nickel), the source of sulfide ion (sodium sulfide) and source of the structure-forming agent having an organic cation (tetrapropylammonium). The reaction mixture was crystallized in an autoclave for 72 hours at a temperature of 140° C. After crystallization highlighted the solid residue washed with water and dried, and then calcined 3-5 hours at a temperature above 450° With removal of organic compounds. A feature of the catalyst is taking place during annealing in the presence of oxygen transfer formed in the first stage of sulfides of metals of the II or VIII group of the periodic system in the oxide of the second form. To obtain the proton form of the zeolite used ion exchange in a solution of ammonium nitrate, followed by calcination at 500° C. To determine the composition of the catalyst was used the data of elemental analysis, the type of crystal structure was confirmed by the method of x-ray phase analysis. All the obtained catalyst had a zeolite structure type of pentasil containing nanoparticles of metal oxides II or VIII group of the periodic system. For granulation of the catalyst may be used a binder, such as alumina.

Example 1

The catalyst was prepared as follows: 32.1 g of sodium silicate (Na2O - 70 g/l, SiO2- 240 g/l) are added under stirring of 17.35 g of a solution containing 0,g Al2(SO4)3×N2O, 0,63g Zn(CH3Soo)2×2H2O, 2,63 g tetrapropylammonium and 1.83 g of concentrated H2SO4. The obtained gel is stirred for one hour, then it is added of 3.85 g of a solution containing 0.95 g of Na2S× 9H2O. the Gel is crystallized in an autoclave at 140° C for 72 hours. The crystalline precipitate is filtered, washed with water and dried at room temperature. The obtained sample calcined 3 hours at a temperature of 500° in a stream of air to form zinc oxide and the removal of organs is practical connections. After two ion exchange in a 1M solution of NH4NO3re-annealing at 500° C for 2 hours to convert the zeolite in the H form. The result is a zeolite with structure type pentasil with the General formula 0,01Na2O 0,99H2O, 1Al2O3, 80SiO2, 0,9ZnO and residual sulfur content less than 0.1 wt.%.

Example 2.

Similar to example 1, the difference lies in the fact that the preparation of the catalyst instead 0,63 g Zn(CH3Soo)2×2H2O was taken 0,61 g with NISO4×7H2O. the Catalyst is a zeolite structure type of Pancasila with the General formula 0,01Na2O 0,99H2O, 1Al2O3, 80SiO2, 0,8NiO, sulfur content less than 0.1%.

Example 3

Similar to example 1, the difference consists in that the zeolite is optionally granulated with binder hydrogel of aluminum hydroxide, followed by drying and calcination at temperatures above 400° C. the Contents of a matrix of aluminum oxide in the obtained catalyst is 30 wt.%.

The proposed method for high-octane fuels and propane-butane fraction is as follows.

Hydrocarbons, such as gas-condensate or naphtha, served in a flow type reactor with a fixed catalyst bed. The catalyst is a zeolite of type pentasil General the th formula hmm 2/nOh, l2OC, ySiO2, zMe2/mO, where M is the proton and/or the cation of the metal, Me is a metal II or VIII groups of the periodic system, n is the valence of cation M, m is the valence of the metal Me, x, y, z - the number of moles of Al2O3, SiO2, Me2/mO, respectively, the relationship of y/x and y/z are in the range of 5-1000. The catalyst is heated to a temperature of 400 to 500° and purge the purge gas (nitrogen, inert or C1-C3hydrocarbon gases). Then in the reactor set temperature of the reaction, the purge gas replace gas diluent, for example methane. Gas diluent serves under the pressure of 1-30 ATM, the feed rate is chosen in the range of 0.5-10 h-1the ratio of the gas-solvent/raw material support in the range 1-50. At the outlet of the reactor the resulting products are separated into liquid and gaseous components determine the chromatographic method.

Example 4

The transformation of gas condensate (No. 1), the composition of which is presented in table 1, high-octane product and propane-butane fraction is as follows: the catalyst of example 1 is placed in a flow reactor, rinsed with nitrogen at a temperature of 450°C, the temperature was then reduced to 400° C, the nitrogen is replaced by methane, pressure up to 10 ATM, and then start the flow of hydrocarbons. Mass / min net is ü feed is 4.3 h -1the ratio of methane/raw materials equal to 7. The results of the experiment are presented in table 2.

Example 5

Similar to example 4, the difference is that using the catalyst according to example 2.

Example 6

Similar to example 4, the difference is that using the catalyst according to example 3, and the raw material is natural gas condensate (No. 2), the composition of which is presented in table 1.

Examples 7-13

The transformation of gas condensate (No. 2), the composition of which is presented in table 1, high-octane product is as follows: the catalyst of example 3 is placed in a flow reactor, rinsed with methane at a temperature of 450°, then set the temperature and the pressure holding process, after which the catalyst is served raw. Conditions of the experiments and the obtained results are presented in table 3.

Example 14

The conversion of straight-run gasoline (No. 3), the composition of which is presented in table 1, high-octane product is as follows: the catalyst of example 3 is placed in a flow reactor, rinsed with methane at a temperature of 450°C, then set the temperature to 375°C and a pressure of 10 ATM, after which the catalyst is served raw with a speed of 3 h-1and the ratio of methane/raw materials equal to 4. The results are presented in table 3.

Example 15

Comparison of the stability of the composition of the products DL the various catalysts. Similar to example 1, the difference lies in the fact that they use two catalyst comparison: zeolites of type ZSM-5 with the ratio of SiO2/Al2O3=70 in the protonated form (HZSM-5) and coated with zinc oxide (ZnO/HZSM-5). Last catalyst obtained by impregnation of the zeolite HZSM-5 with a solution of zinc nitrate, followed by calcination in air flow, the content of zinc was 8 wt.%.

The results of the catalytic test is shown in figure 1-4. Figure 1 shows the change in the content of aromatic hydrocarbons in the products of the conversion of gas condensate (No. 1) for the proposed catalyst and two catalysts comparison. Figure 2 shows the change in the content of hydrocarbons of normal structure in the products of the conversion of gas condensate (No. 1) for the proposed catalyst and two catalysts comparison. Figure 3 presents the change in the content of cyclic hydrocarbons and out-buildings in the products of the conversion of gas condensate (No. 1) for the proposed catalyst and two catalysts comparison. Figure 4 shows the change in the content of the propane-butane fraction in the products of the conversion of gas condensate (No. 1) for the proposed catalyst and two catalysts comparison.the catalyst according to the proposed method;- HZSM-5;- ZO/HZSM-5.

Comparative analysis shows a significant advantage in the stability of the composition of the product obtained by the method proposed in the present invention.

Example 16

The experiment is conducted as follows: the catalyst of example 3 is placed in a flow reactor, rinsed with methane at a temperature of 450°, then set the temperature to 375° and a pressure of 10 ATM, after which the catalyst is served straight-run gasoline (No. 3) (composition shown in table 1) with a speed of 2 h-1and the ratio of methane/raw materials equal to 7. The process conditions are not changed up until the octane number of the product is reduced to 76 units by the motor method. In a further decline in the catalyst activity is compensated by a slow rise of temperature so that the product had an octane rating no lower than 76 by the motor method. The process in this mode is carried out for 400 hours, the temperature rise was 100° C.

Thus, mainegenealogy period when carrying out the process according to the proposed method of obtaining marketable products - gasoline with an octane rating no lower than 76 MM - not less than 400 hours.

Table 1

The composition of hydrocarbons
ComponentContent wt.%
 Gas condensate (No. 1)Gas condensate (No. 2)Straight-run gasoline (No. 3)
1234
propane1,20,30,0
butane5,65,11,0
branched and cyclopentane7,316,3a 3.9
n-pentane10,021,77,5
branched and cyclohexane7,518,98,8
n-hexane7,311,47,3
branched and Cycloheptane10,212,516,1
n-heptane5,63,56,0
extensive octane10,85,317,8
n-octane4,3 0,8the 4.7
branched nonanes5,61,19,1
n-nonan3,50,22,2
benzene1,31,20,4
Continuation of table 1
1234
toluene2,60,71,3
ethylbenzene and xylenes3,60,43,1
ethylmethylketone and trimethylbenzene2,10,11,1
other paraffin hydrocarbons11,40,59,6
other aromatic hydrocarbons0,10,10,0
Total hydrocarbons:   
aromatic With6+ the 9.72,45,9
n-paraffins With5+33,137,627,8
ISO - and cycloparaffins

With5+
50,454,665,3
With3-C46,8of 5.41,0
Octane number, MM666969

7
Table 2

The composition of the products during the transformation of gas condensates in high-octane fuel
ExampleGas condensateThe product composition, wt.%The estimated octane number*, MI
  aromatic With5+n-paraffins With5+ISO - and cycloparaffins

With5+
the propane-butane fraction
4No. 126,76,9 29,736,795,0
5No. 125,5the 4.729,540,495,0
6No. 212,810,934,641,7to 91.1
* To assess the octane number was used the method proposed by S. C. Tile and others, "Method of gas chromatographic analysis of motor gasoline", Chemistry and technology of fuels and oils, 2001, No. 4, p.44-48. Consideration was given to the hydrocarbon, C5+.

Table 3

The process conditions of high octane fuels and its indicators
ExampleRaw materialsThe process conditionsThe yield of gasoline fraction, %Octane, MI
  temperature, °Cpressure, ATMmass feed rate, h-1the ratio of methane/raw
No. 232510677578,9
8No. 237510276190,5
9No. 24251010775to 78.3
10No. 24003474782,2
11No. 240030475592,4
12No. 240010426790,8
13No. 240010 214592,6
14No. 3375103460of 92.7

1. The catalyst for producing high-octane fuels and propane-butane fraction, representing the zeolite type pentasil with the General formula hmm2/nOh, l2About3, SiO2, z2/mOh, where M is the proton and/or a cation of a metal, Metal - metal II or VIII groups of the Periodic system, n is the valence of cation M, m is the valence of the metal Me, x, y, z - the number of moles of Al2O3, SiO2, Me2/mAbout, respectively, a relationship of y/x and y/z are in the range of 5-1000, characterized in that the metal oxide IU2/mO formed during calcination in the presence of oxygen IU-containing insoluble compounds obtained in the reaction medium for the synthesis of zeolite.

2. The catalyst according to claim 1, characterized in that the metal oxide IU2/mAbout formed by the oxidation of sulfide metal II or VIII groups of the Periodic system, obtained in the reaction medium for the synthesis of zeolite.

3. The catalyst according to any one of claims 1 and 2, characterized in that as the metal IU use zinc or Nickel.

4. Catalyst according to any one of claims 1 to 3, characterized in that kata is isator molded with a binder.

5. The method of obtaining high-octane fuels and propane-butane fraction by conversion of hydrocarbons in the feed and contacting the heated catalyst comprising a zeolite of type pentasil with the General formula hmm2/nOh, l2About3, SiO2, z2/mOh, where M is the proton and/or a cation of a metal, Metal - metal II or VIII groups of the Periodic system, n is the valence of cation M, m is the valence of the metal Me, x, y, z - the number of moles of Al2About3, SiO2, Me2/mAbout, respectively, a relationship of y/x and y/z are in the range of 5-1000, and placed in the reactor, which serves gas diluent at elevated pressure, characterized in that the catalyst contains a metal oxide IU2/mOh, which is formed in the process of annealing in the presence of oxygen IU-containing insoluble compounds obtained in the reaction medium for the synthesis of zeolite.

6. The method according to claim 5, characterized in that the catalyst is heated to a temperature of 320-500°C.

7. The method according to any of pp.5 and 6, characterized in that the gas diluent serves at a pressure of 1-30 ATM.

8. The method according to any of pp.5-7, characterized in that as the diluent gas using methane.

9. The method according to any of pp.5-8, characterized in that the ratio of the gas-solvent/raw material varies in the range 1-50.

10. The method according to any of pp.5-9, featuring the the action scene, the feed rate is chosen in the range of 0.5-10 h-1.

11. The method according to any of pp.5-10, characterized in that hydrocarbons using gas-condensate or naphtha.



 

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The invention relates to the field of chemistry, and in particular to methods of preparation of catalysts for the conversion of light hydrocarbons to high octane motor fuel components

The invention relates to compositions that can be used for the conversion of hydrocarbons in the C6-C8aromatic hydrocarbon and the olefin, to a method for producing the composition and method of using the composition for the conversion of hydrocarbons in the C6-C8aromatic hydrocarbon and olefin

The invention relates to improved compared with the prior art catalyst to produce liquid hydrocarbons of low molecular weight oxygenated organic compounds comprising crystalline aluminosilicate type pentasil with the value of the molar relationship of silicon oxide to aluminum oxide from 25 to 120, sodium oxide, zinc oxide, oxides of rare earth elements and a binder, where the oxides of rare earth elements it contains the oxides of the following composition, mol.%:

the cerium oxide - 3,0

the oxide of lanthanum - 65,0

the oxide of neodymium - 21,0

the oxide of praseodymium - Rest

moreover, each value of silicon oxide to aluminum oxide in the crystalline aluminosilicate type pentasil corresponds to a certain range of values of the content of sodium oxide, in the following ratio of catalyst components, wt.%:

Crystalline aluminosilicate type pentasil - 63,0-70,0

The sodium oxide - 0,12-0,30

Zinc oxide - 0,5-3,0

The oxide of rare earth elements in the specified composition - 0,1-3,0

Binding - Rest

This catalyst has a higher activity

The invention relates to a method for selective receipt of paraxylene, which includes the interaction of toluene with methanol in the presence of a catalyst containing a porous crystalline aluminosilicate zeolite having a diffusion parameter for 2,2-Dimethylbutane about 0.1-15 sec-1measured at a temperature of 120oC and a pressure of 2.2-Dimethylbutane (8 kPa)

The invention relates to the refining, namely, the processing of the waste refinery gases for obtaining aromatic concentrate to increase the octane characteristics of low-octane straight-run gasoline or gas condensate

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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