The method of producing dimethylnaphthalene

 

(57) Abstract:

The invention relates to a method of producing dimethylnaphthalene or mixture of dimethylnaphthalenes the dehydrogenation mixture of dimethylaniline in the liquid phase in the presence of a dehydrogenation catalyst noble metal on an inert carrier at an elevated temperature, preferably 200-300oC, and a pressure sufficient to maintain the original product in the liquid phase. This method allows to obtain dimethylnaphthalene with high yield and selectivity for certain isomers dimethylnaphthalene. 8 C.p. f-crystals, 1 table.

The invention generally relates to a method of obtaining dimethylnaphthalene, and in particular, offers a way to obtain dimethylnaphthalene from the original product containing at least 80 wt.% dimethylethylene or mixture of dimethylmethylene the dehydrogenation reaction in the presence of a catalyst.

Description of previous works

Dimethylnaphthalene are required parent compounds to obtain the corresponding naphthaleneboronic acid by oxidation.

Naphthalenesulphonate acid is a monomer, which, as is well known, may be suitable for polucheniya, has the best thermal stability and mechanical properties than polyethylene terephthalate and useful in the production of films and rubbers.

Usually dimethylnaphthalene get when cleaning gases from coal in the form of a mixture of all ten possible isomers. However, the separation of these isomers is very time consuming and expensive. Therefore, the way to obtain the individual isomers dimethylnaphthalene or a mixture of two or three isomers dimethylnaphthalene high purity and quality are highly desirable. One such method is a multistage synthesis, including (1) formation of alkenylbenzene the reaction of o-, m-, or p-xylene with butadiene, (2) the cyclization of the obtained alkenylbenzene with the formation of one or more dimethylethylene related to one or two of the three groups of isomeric dimethylethylene, group a contains 1,5-, 1,6-and 2,5 - and 2,6-dimethylaniline, group b contains 1,7-, 1,8-, 2,7 - and 2,8-dimethylethylene and group C contains 1,3-, 1,4-, 2,3-, 5,7-, 5,8- and 6,7-dimethylmethylene (3) dehydrogenation of dimethylmethylene with the formation of the corresponding dimethylnaphthalenes and (4) the isomerization of the resulting dimethylnaphthalenes to the desired isomer dimethylnaphthalene.

For example, Thompson in patents With whom methyltyramine at 200-450oWith the presence of any suitable solid acidic cyclization catalyst such as an acid crystalline zeolite, such as silicon, aluminum, silicon and magnesium, and silicon-aluminum-zirconium and phosphoric acid, followed by dehydration of the obtained dimethylethylene in the vapor phase to the corresponding dimethylnaphthalenes in an atmosphere of hydrogen at 300 to 500oC and in the presence of solid catalysts for dehydrogenation as noble metals on carriers and oxides homoalanine, and then isomerization of each of the above dimethylnaphthalene in the desired isomer in the triad of dimethylnaphthalenes to which this isomer belonged when 275-500oC in the presence of a solid acid isomerization catalyst of the same type as described for the cyclization. On the other hand, cyclization and isomerization can be carried out in the liquid phase, in this case, the cyclization is carried out at 200-275oC solid postinoculation catalyst, at 70-140oC with an acid ion exchange resin, acidic crystalline zeolite, hydrofluoric or sulfuric acid, or silicon porous catalyst.

In particular, U.S. patent 3 775 496 (1) describes the cyclization of 5-/m-tol the phase isomerized to 2,6 - and 2,7-dimethylnaphthalene respectively.

U.S. patent 3 775 497 (2) reveals the cyclization of 5-phenylhexane-2 to 1.4-dimethylethylene that digitalout to 1,4-dimethylnaphthalene, which in turn isomerized 2.3-dimethylnaphthalene.

U.S. patent 3 775 498 (3) describes the cyclization of 5-(o-tolyl)-pentene-2 - 1.5-dimethylethylene, which is then digitalout to 1.5-dimethylnaphthalene, which in turn isomerized 2.6-dimethylnaphthalene.

U.S. patent 3 775 500 (4) describes the cyclization of 5-/p-tolyl/- pentene-2 to 1.7-dimethylethylene that digitalout to 1.7-dimethylnaphthalene, which in turn isomerized 2.7-dimethylnaphthalene.

The problem with all methods of previous works is the presence of other isomers dimethylnaphthalene, unreacted dimethylethylene and alkenylbenzene as impurities and by-products in the final desired specific isomer dimethylnaphthalene. The presence of these impurities and by-products significantly reduces the usefulness and commercial value of the required isomer dimethylnaphthalene, especially as a source for obtaining naphthaleneboronic acid for use as a monomer in the production of polymers. Moreover, at high temperatures, as a result, the om is highly desirable to use a liquid-phase processes at a relatively low temperature and to improve the completeness and selectivity of each stage of the above-described multi-stage synthesis of the required product.

The purpose of the invention

The purpose of this invention is to provide an improved method of obtaining the best yield and selectivity of a specific isomer of dimethylnaphthalene or number of isomers dimethylnaphthalene by cyclization of alkenylbenzene with the formation of specific isomer of dimethylethylene, or the number of isomers dimethylethylene, with their subsequent dehydrogenation.

Another purpose of this invention is to provide an improved method of obtaining a high yield and selectivity of a specific isomer of dimethylnaphthalene by cyclization of alkenylbenzene with the formation of specific isomer of dimethylmethylene or number of isomers dimethylethylene their subsequent dehydrogenation and isomerization of the resulting dimethylnaphthalenes.

Other objectives and advantages of the method of the present invention become apparent from the following detailed description and appended claims.

The essence of the invention

These objectives are achieved using an improved method of producing dimethylethylene from 5-/o-, m - and p-tolyl/pentene-1 or -2 or 5-phenyl-hexene-1 or -2 as the first source material, including: interaction in the liquid phase escolares sieve, which is substantially free of adsorbed water in the temperature range from about 120oC to about 250oC and at high enough pressure to maintain the original substance in the liquid phase at this starting material, the water content of which does not exceed 0.5% by weight, cyclized with the formation of the first liquid product containing a mixture of dimethylaniline, and when (a) the first starting material contains 5-(o-tolyl)-penten-1 or -2, receive a mixture containing at least 80% by weight obtained 1,5-, 1,6-, 2,5 - or 2,6 - dimethylaniline, (b) when first starting material contains 5-m-tolyl penten -1 or -2, receive 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6-, 2,7- or 2.8-dimethylethylene or a mixture comprising at least 80% by weight of the obtained dimethylethylene, (c) when first starting material contains 5-(p-tolyl)-penten-1 or -2, receive 1,7-, 1,8-, 2,7 - or 2,8-dimethylethylene or their mixture, containing at least 80% by weight of the obtained dimethylethylene, (d), the first starting material contains 5-phenylhexane-1 or -2, receive 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethylethylene or a mixture containing at least 80% by weight of the obtained dimethylethylene.

A suitable source for use in protego invention by stage cyclization preferably should stage dehydrogenation.

When the initial stage cyclization of the present invention is 5-/o-tolyl/-penten-1 or -2, it formed 1,5-, 1,6-and 2,5 - or 2,6-dimethylaniline or a mixture containing at least 80%, preferably at least 85% of dimethylmethylene, which, in turn, are the source and undergo dehydrogenation to the corresponding 1,5-, 1,6 - and 2,6-dimethylnaphthalenes, which then are the initial stage of isomerization of the present invention and converted into 2,6-dimethylnaphthalene.

When the source for the cyclization stage is a 5-m-tolyl/ penten-1 or -2, it is obtained 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6-, 2,7- or 2.8-dimethylethylene or a mixture containing at least 80%, preferably at least 85% by weight, dimethylmethylene, which, in turn, are the source and undergo dehydrogenation to the corresponding 1,5-, 1,6-, 1,7-, 1,8-, 2,6- and 2.7 - dimethylnaphthalene, who then are the initial stage of isomerization and converted into 2,6 - and 2,7 - dimethylnaphthalene.

When the source for the cyclization stage is 5-/p-tolyl/hepten-1 or -2 it turns 1,7-, 1,8-, 2,7 - or 2,8-dimethylnaphthalene or a mixture containing at least 80%, preferably at least 85%, dimethylmethylene, to naftalina, who then are the original and transformed on stage isomerization of 2,7-dimethylnaphthalene.

When the source for the cyclization stage is a 5 - phenylhexane-1 or -2, it is obtained 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethylethylene or a mixture containing at least 80%, preferably at least 85% of dimethylmethylene, which in turn are the source and dehidrirana to the corresponding 1,3-, 1,4 - and 2,3 - dimethylnaphthalene, which then are the source and at the stage of isomerization into 2,3-dimethylnaphthalene.

In the method of the present invention, the dehydrogenation reaction is conducted in the liquid phase at elevated temperature and under high pressure, in order to maintain the product in the liquid phase. The dehydrogenation reaction is carried out in the temperature range from about 200oC, preferably 220oC, up to about 300oC, preferably 270oC and usually in the range of pressures from 0.5, preferably of 0.8 to about 5, preferably of 1.3 ATA.

The dehydrogenation reaction can be carried out with a solvent or without solvent for the corresponding source. Preferably, however, do not use solvent, if the solvent still is as tetradecane or such aromatic hydrocarbons as anthracene or their mixture, which preferably boils at t 270oC.

The reaction of this invention may be performed periodically or continuously.

The reaction apparatus may be any of known types, such as fixed bed, moving bed, fluidized bed, with a layer of catalyst suspended in the liquid phase, or by mixing solid particles in the liquid in the vessel. In General, however, the use of devices with a porous layer preferably commercially.

The increase in the conversion source and the selectivity of the formation of the desired product or range of products of the dehydrogenation is the result of the selected conditions of temperature and pressure, as well as high activity and selectivity of the used catalyst, which in turn allows the use of less stringent conditions, i.e., lower temperature and pressure and this can be achieved by increased selectivity and reduced deactivation of the catalyst.

Used catalyst in this way any solid dehydrogenation catalyst, able to work and have for a long time activity in your environment, including such catalysts, as noble metals on carriers, such as chibiromano coal or aluminum oxide, containing from about 0.5, preferably from 1 to about 15, preferably 10 weight% of palladium relative to the weight of the catalyst.

If the dehydrogenation is carried out periodically, the catalyst is used in the range of from about 0,005, preferably of 0.01 to about 1.0, preferably 0.2 to percent by weight of noble metal, counting on elemental noble metal-to-weight dimethyltetrahydrofuran source, and the reaction time is from about 1 (preferably 2) to about 20 (preferably 10 hours). If the dehydrogenation is carried out continuously, the volumetric flow rate is from about 0.1, preferably from 10 to about 100, preferably up to 50 parts by weight of the original dimethylethylene on one part of the component containing a noble metal, per hour /counting on elemental noble metal/.

Further, the invention is illustrated in the examples.

Examples 1-6

In each of examples 1-6 liquid source and 5% palladium on coal as a catalyst are placed in a flask and constantly pass nitrogen through the reaction mixture to remove oxygen. The temperature of the reaction mixture raised to the reaction temperature and periodically take samples and analyze them. Hydrogen, obrazovanih products containing up to 13 carbon atoms, % conversion source and % selectivity of the formation of the desired products from the total amount of unreacted source in each of examples 1-6 are shown in table 1.

The results from table 1 show that even under moderate conditions of temperature and pressure in examples 1-6, the dehydration method of the present invention takes place with high conversion and selectivity.

DMT - dimethylethylene

DMN - dimethylnaphthalene

1. The method of producing dimethylnaphthalene or mixture of dimethylnaphthalenes, characterized in that it includes the interaction between the source of liquid product containing (a) 1,5-, 1,6-, 2,5 - or 2,6-dimethylethylene or a mixture containing at least 80% of dimethylmethylene, (b) 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6-, 2,7- or 2.8-dimethylethylene or a mixture containing at least 80% of a mixture of dimethylaniline, (c) 1,7-, 1,8-, 2,7 - or 2,8-dimethylethylene or a mixture containing at least 80% of a mixture of dimethylaniline, or (d) 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethylethylene or a mixture containing at least 80% of the mixture obtained dimethylethylene, in the liquid phase with a solid dehydrogenation catalyst in the reaction vessel at elevated temperature and pressure, PT is lechesa in the equilibrium of the dehydrogenation reaction, with the formation of hydrogen and a second liquid product containing a mixture of dimethylnaphthalenes, and removing hydrogen from the reaction vessel, which moves above the equilibrium towards the formation of a mixture of dimethylnaphthalenes, and when the source of liquid product is the product of (a) obtain 1,5-, 1,6 - or 2,6-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes when the initial liquid product is the product of (b) receive 1,5-, 1,6-, 1,7-, 1,8-, 2,6- or 2,7-dimethylnaphthalene or their mixture, containing at least 80% of dimethylnaphthalenes in the second liquid product when the original liquid product is the product of (c), receive 1,7-, 1,8-, 2,7-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes when the initial liquid product is the product of (d) receive 1,3-, 1,4 - or 2,3-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes in the second product.

2. The method according to p. 1, characterized in that when source product using 1,5-, 1,6-, 2,5 - or 2,6-dimethylethylene or a mixture containing at least 80% of dimethylmethylene, the product contains 1,5-, 1,6-, 2,6-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes.

the mixture, containing at least 80% of dimethylaniline as the original product, get 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6- or 2,7-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes.

4. The method according to p. 1, characterized in that when using 1,7-, 1,8-, 2,7 - or 2,8-dimethylethylene or a mixture containing at least 80% of dimethylmethylene receive 1,7-, 1,8 -, or 2,7-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes.

5. The method according to p. 1, characterized in that when used 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethylethylene or a mixture containing at least 80% of dimethylmethylene receive 1,3-, 1,4 - or 2,3-dimethylnaphthalene or a mixture containing at least 80% of dimethylnaphthalenes.

6. The method according to p. 1, characterized in that the dehydrogenation is carried out at a temperature of from about 200 to about 300oC.

7. The method according to p. 1, characterized in that the dehydrogenation is carried out in the temperature range from about 220 to about 270oC.

8. The method according to p. 1, characterized in that the dehydrogenation is carried out at a pressure from about 0.5 to about 5 abs. the ATM.

9. The method according to p. 1, characterized in that the dehydrogenation catalyst of vkluchau relation to the weight of the dehydrogenation catalyst on an inert carrier.

 

Same patents:

The invention relates to a method for selective receipt of dimethylnaphthalenes isomerization of the initial mixture in the presence of a catalyst containing either beta-zeolite or an acidic crystalline zeolite ultrastable (with respect the Y-type having a molar ratio of the oxides of silicon and aluminum from 4:1 to 10: 1 and having a pore size provided dvenadcatiletnie oxygen cycles, and the size of the unit cell from to 24,2 24,7at elevated temperature and pressure sufficient to maintain the mixture to the isomerization in the liquid phase

The invention relates to the field of reception of dimethylmethylene (DMT) of 5 - (o -, m - or p-tolyl)-Penta-1 - or-2-ene or 5-phenyl-Gex-1 - or-2-ene used as an intermediate for obtaining naphthalenesulphonic acids

The invention relates to a method for selective receipt of dimethylnaphthalenes isomerization of the initial mixture in the presence of a catalyst containing either beta-zeolite or an acidic crystalline zeolite ultrastable (with respect the Y-type having a molar ratio of the oxides of silicon and aluminum from 4:1 to 10: 1 and having a pore size provided dvenadcatiletnie oxygen cycles, and the size of the unit cell from to 24,2 24,7at elevated temperature and pressure sufficient to maintain the mixture to the isomerization in the liquid phase

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FIELD: petrochemical processes.

SUBSTANCE: liquid pyrolysis products are processed to recover C6-C11-fraction, which is then separated into C6-C8 and C9-C11-fractions. C6-C8-Fraction is subjected to catalytic hydrostabilization and hydrofining. C9-C11-Fraction is hydrostabilized in presence of catalyst and then processed to isolate C10-C11-fraction. C6-C8 and C10-C11-fractions are combined at specified proportion and resulting mixture is subjected to thermal hydrodealkylation. Desired benzene and naphthalene products are recovered from hydrodealkylation product via rectification. High-purity benzene is obtained after fine catalytic posttreatment.

EFFECT: increased yield of desired products and service time of hydrostabilization catalyst.

2 cl, 1 dwg, 4 tbl, 10 ex

FIELD: petroleum chemistry.

SUBSTANCE: claimed method includes purification of naphthalene-containing cuts from unsaturated compounds by catalytic polymerization followed by isolation of high purity naphthalene. Polymerization is carried out in presence of aluminum-cobalt-molybdenum catalyst, containing (mass %): cobalt oxide (CoO) 2.0-6.0 and molybdenum trioxide (MoO3) on carrier: Y-Al2O3 under pressure up to 0.6 MPa, at temperature of 180-200°C for 1-10 hours.

EFFECT: increased naphthalene yield.

2 tbl, 5 ex

FIELD: organic chemistry, adamantine derivatives, chemical technology.

SUBSTANCE: invention relates to a method for synthesis of adamantyl-containing derivatives of naphthalene of the general formula: , wherein R1 = R3 means hydrogen atom (H); R2 means Ad (1); R1 means -OH; R2 means H; R3 means Ad (2); R1 means Ad; R2 means -OH; R3 means H (3). Method involves adding naphthalene-containing compound chosen from order involving naphthalene, 1-naphthol and 2-naphthol to 1,3-dehydroadamantane in the mole ratio of reagents = 1:(2-4). The addition reaction is carried out in inert solvent medium, for example, diethyl ether or dioxane, at its boiling point (35-100°C) for 30 min in the presence of catalytic amounts of sulfuric acid. Invention allows to develop a method for synthesis of adamantyl-containing naphthalene derivatives for small stages, enhancing the yield of product and decreasing the reaction time.

EFFECT: improved method of synthesis.

3 ex

FIELD: industrial organic synthesis.

SUBSTANCE: invention relates to production of cyclic α-methylstyrene dimmer, in particular 1,1,3-trimethyl-3-phenylindane, which is used as base for lubricating materials, propellants, and heat carriers. Process is accomplished via dimmerization of α-methylstyrene using, as catalyst, complex AlCl4*CCl3 formed in situ during interaction of activated powdered metallic Al with CCl3 at 50°C and atmospheric pressure, Al/CCl3/α-methylstyrene molar ratio being 10:25:3.9. Reaction time is 2 min. Selectivity of formation of desired product is 94% and α-methylstyrene conversion is 100%.

EFFECT: increased yield of desired product.

FIELD: chemistry.

SUBSTANCE: cyclic sterol dimer (cys- and trans-1-methyl-3-phenylindan) is produced by sterol oligomerisation with ceolite catalyst added in solvent characterised by that catalyst is ZSM-12 ceolite in N-form in amount 20-30 wt %. Reaction enabled in chlorbenzene in ratio sterol: chlorbenzene =1:2÷4 (vol.) and temperature 120-130°C.

EFFECT: simplified cyclic sterol dimer production process with higher yield.

1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention refers to method of producing cyclic styrene dimers (cis- and trans-1-methyl-3-phenylindane) by styrene oligomerisation with zeolite catalyst, differing that the catalyst is N-zeolite type ZSM-12 in amount 20-30 wt %. And reaction is performed at temperature 120-130C.

EFFECT: simplified process of high-yield producing cyclic styrene dimers.

1 cl, 5 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: invention refers to method for making cyclic styrene dimers (cis- and trans-1-methyl-3-phenylindan) by oligomerising styrene with N-zeolite type Beta added in the solvent, differing that amount of Beta zeolite is 18-25 wt % with reaction performed in chlorbenzene in ratio styrene:chlorbenzene=1:4 (voi.) and temperature 115-130C.

EFFECT: simplified process for making cyclic styrene dimers.

1 cl, 5 ex, 1 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to organic chemistry and can be used to produce complexing agents, sorbents, biologically active compounds, as well as novel materials with given properties. C60-fullerene reacts with cholesteryl diazoacetate in o-dichlorobenzene in the presence of a three-component catalyst system {Pd(acac)2:2PPh3:4Et3Al} at temperature 80C for 0.5-1.5 hours. Molar ratio C60:diazocompound:Pd(acac)2:PPh3:Et3Al}=1:(3-7):(0.1-0.3):(0.2-0.6):(0.4-1.2), preferably 1:5:0.2:0.4:0.8. Cholesteryl cyclopropa[1,9](C60-Ik,)[5,6]fullerene-3'-carboxylate of formula

is obtained with output 44-68%.

EFFECT: high efficiency of the method.

FIELD: chemistry.

SUBSTANCE: invention relates to compounds of formula (I) and pharmaceutically acceptable salts thereof. In formula (I): X denotes a single bond or a binding group selected from -CO, -SO2-, -CS- or -CH2-; Y denotes a single bond or a divalent binding group obtained from a cyclic structure selected from benzene, pyridine, pyrimidine, pyrazole, imidazole, thiazole, thiophene, quinoline, benzoimidazole, benzothiazole, benzopyrazole, naphthalene and benzothiophene; X and Y are simultaneously single bonds; Z denotes a hydrogen atom or a substitute selected from a group A; m equals 1 or 2; n equals 0-3; in group A and group B, R, R' and R" can, respectively and independently, be identical or different and denote a hydrogen atom or -C1-6-alkyl; said -C1-6-alkyl can be substituted with a group selected from -OH, -O(C1-6-alkyl),-CONH2, -CONH(C1-6-alkyl), -CON(C1-6-alkyl)2, -NH2, -NH(C1-6-alkyl) and -N(C1-6-alkyl)2); Sus denotes a C3-C7 saturated or a C5-C10 unsaturated hydrocarbon ring or a nitrogen-containing C3-C7 heterocyclic ring containing 1-4 nitrogen atoms or containing an additional O, S atom; said C1-6 alkylene in groups A and B can be substituted in positions 1-3 with a -N(C1-6- alkyl)2 group, values of radicals R1, A1, T, B and Q are given in the claim. The invention also relates to a pharmaceutical composition containing said compounds, a PI3K inhibitor and a medicinal agent having PI3K inhibitor properties against a proliferative diseases such as a malignant tumour.

EFFECT: high efficiency of using the compounds.

21 cl, 645 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of converting methane-containing starting material into synthetic gas and an aromatic hydrocarbon (hydrocarbons). The method involves: (a) contacting the methane-containing starting material with a dehydrocyclisation catalyst in conditions sufficient for obtaining a first effluent containing said aromatic hydrocarbons, residual methane and H2, where said first effluent has concentration of aromatic rings which is at least 5 wt % higher than concentration of aromatic rings in said starting material. Further, (b) extracting at least a portion of said aromatic hydrocarbons from said first effluent and then (c) reaction of at least a portion of said H2 and said residual methane from said first effluent with oxygen-containing materials to obtain a second effluent containing H2 and CO, where the total number of moles of H2 and CO in said effluent is greater than the number of moles of H2 and CO in said first effluent.

EFFECT: method provides improved conversion of methane into aromatic hydrocarbons.

15 cl, 5 ex

FIELD: basic organic synthesis, chemical technology.

SUBSTANCE: invention relates to the improved method for isomerization reaction of pentane-hexane fraction with aim for preparing high-octane additive for gasoline. Pentane-hexane fraction is subjected for isomerization reaction in reaction-rectifying process using a low-temperature platinum-alumina catalyst. The parent raw is subjected for preliminary separation for pentane and hexane fractions. These fractions are subjected for separate isomerization that is carried out in vapor phase in reaction zone in bottom of reaction-rectifying column. Catalyst is placed under plates of zone and pressure in reaction zone in maintained in the range from 0.6 to 3.6 MPa, temperature - from 110.0oC to 200.0oC in the mole ratio hydrogen : hydrocarbons at inlet into column from 0.03:1 to 4:1. Method provides enhancing conversion of n-pentane, n-hexane and methylpentanes to high-octane isomers, elevating octane number of isomerizate and constructive simplifying the process.

EFFECT: improved preparing method.

1 dwg, 1 ex

FIELD: petrochemical processes catalysts.

SUBSTANCE: catalyst based on crystalline element-alumino-phosphates and having structure A1PO-31 (SATO) is prepared by providing first reaction mixture containing aluminum source, phosphoric acid, and one or more sources of substituting element as well as organic structure-forming compound followed by crystallization of above mixture under hydrothermal conditions required to form crystals with structure A1PO-31 and isolation of solid crystallization product, to which further modifying group VIII metal is added. Structure-forming compound mentioned above is selected from di-n-pentylamine and mixture thereof with other di-n-alkylamines and substituting element is selected from magnesium, zinc, silicon, cobalt, manganese, nickel, and cadmium. Method of isomerization of n-paraffins at elevated temperature and hydrogen pressure in presence of above-described catalyst is also disclosed.

EFFECT: increased activity and selectivity of catalyst.

4 cl, 1 dwg, 3 tbl, 17 ex

FIELD: petrochemical processes.

SUBSTANCE: feedstock is brought into contact with preliminarily activated zeolite-containing catalyst, namely mordenite-supported Pt, at 250-300°C, pressure 1.5-3.5 MPa, hydrogen-containing gas-to-feedstock ratio 300-1000 nm3/m3, and feed flow rate 1.0-4.0 h-1. Preliminary activation of zeolite-containing isomerization catalyst is conducted in two successive steps: drying catalyst in inert gas flow; reducing catalyst in hydrogen-containing gas flow; and supplying feedstock and setting steady-state isomerization process. Drying of zeolite-containing catalyst in inert gas flow is effected under conditions of gradually raised temperature from 120°C at temperature raise rate 10-15°C/h and ageing for 2-5 h at 120°C to 350°C followed by ageing at this temperature, whereupon temperature is lowered to 130°C. Reduction of zeolite-containing catalyst in hydrogen-containing gas flow is effected at gradually raised temperature to 220-350°C at temperature rise rate 15-25°C/h and ageing for 2-6 h at 220-350°C, whereupon temperature is lowered to 180°C. Initial feedstock is supplied at 180°C in circulating hydrogen-containing gas flow, aged for 4 h at 180°C and then gradually heated to 250°C at heating rate 5°C/h, after which further heated at heating rate 5°C a day to achieve process characteristics meeting product quality requirements.

EFFECT: increased catalyst activity, selectivity, and working stability.

2 cl, 2 tbl, 17 ex

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