Process of producing benzene, ethylene, and synthesis gas

FIELD: petrochemical processes.

SUBSTANCE: process of producing benzene, ethylene, and synthesis gas from methane comprises following stages: (i) supplying into reactor initial gas containing methane and carbon dioxide; (ii) oxidation of methane in reactor under specific reaction conditions using first catalytic material and/or additional oxidant; and (iii) removal from reactor of gas stream formed containing benzene, ethylene, and synthesis gas, inside wall of reactor having been treated with first catalytic material.

EFFECT: increased conversion of methane and selectivity regarding benzene at reduced accumulation of coke fragments.

20 cl, 9 tbl, 9 ex

 

The technical field to which the invention relates.

The present invention relates to a method for benzene, ethylene and synthesis gas from methane.

The partial oxidation of methane is of great industrial value or the production of synthesis gas or the production of higher hydrocarbons and aromatic hydrocarbons, such as benzene.

Currently benzene often get in the way, which includes the production of the product of catalytic reforming, production of pyrolysis gasoline production by dealkylation of toluene and production by aromatization of the CIS (liquefied petroleum gas).

Prior art

In U.S. patent 4239658 described that if the methane to pass through the multi-component catalyst, the product can detect benzene. It is assumed that the methane dissociates the metal to the particles Me-CHx, then formed ethane and ethylene, and interacts with the metal oxide forming the carbide of the metal. Ultimately, the carbide is converted into benzene. Usually benzene appears in large numbers at a temperature above approximately 899°and up to 6-10 wt.% at a temperature of from 1204 until 1301°With or at higher temperatures. In U.S. patent 4239658 high temperature and pyrolysis of pure methane contribute to the formation of significant quantities of a fragment of the polymer coke in the form of inactive material.

There have been many attempts to catalyze these reactions at a lower and more appropriate temperature, but such attempts were unsuccessful.

In the United Kingdom patent 2148933 described the transformation of low molecular weight hydrocarbons of high molecular weight hydrocarbons. This method is used a catalyst containing boron compound, a high reaction temperature higher than 1000°and a high volumetric rate of gas is higher than 3200 h-1. The catalyst containing boron compound, provides a degree of conversion of low molecular weight hydrocarbons of approximately 19%, and this degree of conversion is only supported for about three hours at this temperature and flow rate. High temperature and low degree of conversion of methane is responsible for low yield of high molecular weight hydrocarbons.

Methane can also be converted into higher hydrocarbons without the use of an oxidant by thermal condensation (mating). Thermal methods of conversion of methane into higher hydrocarbons is well known. One of these methods is the way the company Hüls (see H. Gladish a Method of producing acetylene in an arc DC firm Hüls. Pet. Refiner. 1962. 41 (6), 159-165), which operate in more than 50 years. In these methods, the key obtained by the product of the two is as acetylene.

In the method of BASF thermal conversion of methane (see Forbath T.P. and Gaffhey B.J. Acetylene by way of BASF. Pet. Refiner, 1954, 33 (12), 160-165) heat for the endothermic conversion of methane to ethylene is provided by combustion of part of the raw methane in oxygen.

Thermal conversion of methane into higher hydrocarbons in the mode of joint materials studied in U.S. patent 4507517 to the reaction mixture of CH4/O2=10:1 in the presence of a catalyst of Pt/Cr/Ba/Mg/Al2O3. At temperatures below C not detected aromatic hydrocarbons.

In recent years, research related to the non-oxidizing dehydropolymerization methane in the absence of oxygen using zeolites containing molybdenum or other transition metal ions. The General formula of such a catalyst is a Me-HZSM-5 (Me - metal). The degree of conversion and selectivity in the conversion of methane when using such a catalyst at 700°in a stream of pure methane is 7.9-8.0% 72-73,4% respectively, see Bert .Weskhuysen, Wang Dingjun, Michael P.Rsynek, ..Lunsford, J. Catal. 175, 338 (1998). The yield of benzene is about 6%. The catalyst loses activity during the reaction after 3 hours due to the accumulation of coke on the catalyst surface.

More active catalysts described in the work of Zhi-Thao Xiong, Hong-Bin Zhang, Guo-Dong Lin, and Tin-Long Zeng. Catal. Lett. V.74, N3-4, 2001. This catalyst them is l composition of 3% W - 1,5% Li/HZSM-5. The degree of conversion of methane through 105 minutes of flow of methane is 21,0% with a selectivity of 61.5%. After 300 minutes experience the activity of the catalyst becomes low, the degree of transformation is equal to 17,0%, the selectivity for benzene 50%, and the yield of benzene is equal to 8.5%.

In addition, the described catalyst Zn-W-H2SO4/HZSM-5 (in the work of Jin-Long Zeng, Zhi-Tao Xiong, Hong-Bin Zhang, Guo-Dong Lin, K.R.Tsai, Catal. Lett. 53 (1998) 119-124), which is more active and selective. The yield of benzene is 22%. However, the catalyst loses activity during the reaction due to the accumulation of coke on the surface and inside the channels of zeolite. The sulfur component of the catalyst is unstable at 700°and during the reaction evaporates. For all catalysts containing Me/HZSM-5, a characteristic induction period of approximately from 1.5 to 6 hours, after which the catalyst begins to work, while his active centers will not be blocked due to the formation of fragments of coke. After regeneration by oxidation in air, the operation of the catalyst may be renewed, however, recovery of the catalyst after regeneration to form the active material is from about 1.5 to 3 hours, and after a few cycles of the performance of the regenerated catalyst deteriorate.

As a result, the way of aromatization of methane using zeolites OC has the disadvantages: very long induction period of the reaction due to the need metal recovery, present on the zeolite; a very brief period of reaction due to the accumulation of fragments of coke in the catalyst; significant loss of methane in the form of fragments of coke, which must be removed from the catalyst; the formation of significant quantities of naphthalene formed on the catalyst; stable output benzene in these ways using aromatization of methane on zeolite catalysts does not exceed 8%; significant loss of methane as carbon dioxide in the induction period when the recovery of the metal on the zeolite; the formation of fragments of coke inside the channels of the zeolite, resulting in reduced stability of the catalyst and to the destruction of the catalyst particles; and an insufficient degree of conversion of methane.

Disclosure of inventions

The aim of the present invention is to develop a method of producing benzene, which eliminated the disadvantages of the prior art, and specifically developed method for the simultaneous production of benzene, ethylene and synthesis gas with a high degree of conversion of methane, high selectivity and good yield of benzene.

This goal is achieved in a method of producing benzene, ethylene and synthesis gas, which includes the stages of: i) introducing into the reactor a flow of a source gas containing methane and carbon dioxide, (ii) the oxidation of methane in the reactor under certain reaction conditions, it is selected using the first catalytic material and/or additional oxidant; and (iii) removing from the reactor the flow of gas formed, containing benzene, ethylene and synthesis gas.

Preferably, the first catalytic material selected from the group consisting of Mn(NO3)2Si(WO4)2, KNO3, NaOH and/or NVO3.

Specifically, the inner wall of the reactor is treated first catalytic material, which is preferably mixed with the Sol-gel SiO2.

In addition, for the method of the present invention may use type fixed layer in the reactor, and this stationary layer may contain Al2O3and/or SiO2.

In one variant embodiment, the oxidant is introduced together with the flow of the source gas or after the termination of the current source gas.

Preferably, the additional oxidant is an oxygen, air or a mixture of methane with oxygen and/or air.

Also the preferred method in which the concentration of the oxidizing agent relative to the amount of source gas flow does not exceed 2%.

At too high concentrations of oxidant yield of benzene is reduced as a result of deep oxidation of methane to co and CO2.

More preferably the method is carried out in isothermal or non-isothermal conditions when the reactor there is a temperature profile of approximately 600°exit react the RA to about 1500° With the entrance into the reactor, preferably from about 700°With up to 1000°C.

In accordance with an additional variant embodiment of the invention the flow of the source gas is introduced at a temperature of approximately 965°and the flow of gas formed is removed from the reactor at a temperature of about 715°C.

Most preferably, the method is carried out in a reactor made of quartz, ceramic, aluminum alloys, stainless steel or similar materials. Quartz reactor is preferred because, for example, in a metal reactor, the yield of benzene is low due to the profound destruction of methane on the surface of the metal.

In addition, preferably, the second catalytic material is present in the reactor, preferably at the inlet of the heating zone of the reactor, preferably at the top of the reactor. Preferably the second catalytic material is fixed quartz fiber on both sides inside the reactor.

Preferably, the second catalyst is a basic oxide, such as MnO2WO3, SrO, La2About3the mixture MnO2with WO3or a mixture of SrO with La2About3or any mixture, most preferably 2-20%)W-Mn3O4/(2-20%)Sr-La2O3. From the description of the latter catalyst can understand that from 2 to 20 wt.% wolf is AMA embedded in a mass of Mn 3O4or from 2 to 20 wt.% strontium embedded in a mass of La2O3.

More preferably the pressure in the reactor is from about 0.1 to 200 bar (10-20000 kPa).

According to the invention the contact time of the first catalytic material with a gas flow of approximately from 0.1 to 90 seconds.

In one variant embodiment of the invention the ratio of methane to carbon dioxide in the flow of the source gas is about 1-99 mol.%: 99-1 mol.%, preferably about 40-60 mol.%: 70-30 mol.% and even preferably about 50 mol.%: 50 mol.%.

Preferably, the reactor had an inner diameter of approximately 2 to 1000 mm

In addition, preferably the ratio of the length of the reactor diameter is approximately from 1 to 200, preferably from about 5 to 100.

Moreover, preferably the method is carried out continuously or as a periodic way.

In an additional variant embodiment, at least part of the flow of the formed gas is recycled back into the reactor together with the flow of the source gas.

In yet another variant embodiment, at least part of the flow of the formed gas is rapidly cooled at the outlet of the reactor to further reduce the decomposition products. This quenching gas may be performed using cooling flux is s, such as water vapor, nitrogen, oil, or any reaction products such as hydrogen, toluene, heavy aromatic hydrocarbons, benzene, etc.

Eventually, after removal of the flux generated gas from the reactor can be carried out stage of regeneration for the oxidation and combustion of coke. Regeneration can be performed using air and/or methane and/or air mixture, ethane and carbon dioxide. Coming from the stage regeneration gases are mainly carbon dioxide and/or carbon monoxide, hydrogen and/or benzene.

Unexpectedly it was found that the method of the present invention provides a process for the production of benzene, ethylene and synthesis gas, and this method has a high degree of conversion of methane, high selectivity and yield of benzene. In addition, the method produces a small amount of high molecular weight heavy aromatic hydrocarbons such as toluene, naphthalene, methylphenylamine, anthracene, styrene, acetonaphthone, phenanthrene and the like. The method provides a stable output benzene for more than two days, while the selectivity for fragments of coke in three to four times less than the selectivity for benzene. Fragments of coke that were accumulated during the reaction, can be converted into synthesis gas by processing reactor with a mixture of methane and who the ear, preferably at the stage of regeneration, which allows to obtain a synthesis gas having a ratio of carbon monoxide to hydrogen is about 1:3, when the degree of conversion of methane to 35%. The use of carbon dioxide in the method of the present invention allows to oxidize the coke fragments, accumulated during the reaction, in particular carbon dioxide, which is a mild oxidizing agent, shifts the equilibrium and increases the degree of conversion of methane. As diluent carbon dioxide reduces the partial pressure of methane and reduces the formation of coke.

At low partial pressure of methane is possible to avoid the formation of carbon. Dilution with carbon dioxide allows a high degree of conversion of methane. In addition, the presence of carbon dioxide in a mixture of methane, the formation of active fragments of coke and reduces the formation of graphite forms coke. Below is further illustrates that the dilution of carbon dioxide reduces the concentration of heavy aromatic hydrocarbons such as toluene, naphthalene, acetonaphthone, phenanthrene and inhibits the formation of coke. Carbon dioxide interacts with the coke and hydrogen, forming a synthesis gas, which is important for the synthesis of methanol.

As oxidizer carbon dioxide, firstly, is involved in the oxidation is of Rahmanov coke and then, after removal of the fragments of coke, contributes to the formation of the oxidized surface. It is assumed that this method of conversion of methane with carbon dioxide is based on the heterogeneous-homogeneous mechanism, in which the first heterogeneous activation of methane from the formation of various intermediates such as CH3CH2, SN, N2who then take part in radical reactions. Non-isothermal conditions in the reactor of this process contributes to the improvement of selectivity to benzene.

Non-isothermal conditions, namely low temperature at the outlet of the reactor, allows to weaken the possible processes of oxidation, destruction and polymerization and condensation of benzene. The flow of the source gas can be heated to the reaction temperature before entering the reactor.

The method according to the present invention allows on site (in situ) the regeneration of part of the coke fragments under the action of carbon dioxide, as well as provide active fragments of coke (containing hydrogen).

Preferred first catalytic material used in this method is the manganese nitrate, Mn(NO3)2that increases the yield of benzene. Manganese oxide formed from manganese nitrate Mn(NO3)2on the walls of the reactor, significantly SN is continuing accumulation of fragments of coke in the course of the method.

Further advantages and features of the process of the present invention will become apparent from the following detailed examples.

Example 1

The method according to the present invention is carried out in a reactor having a diameter of 10 mm, the inner wall of the reactor is treated with 2 ml of the catalyst (Mn(NO3)2. At a temperature of 965°From the reactor is introduced a mixture of 50 mol.% methane and 50 mol.% of carbon dioxide. The reactor is isothermal and has a temperature profile from 965°at the entrance to 715°With the output gas stream from the reactor. The reactor pressure is 2 bar (200 kPa).

In the following table 1 shows the obtained products and their content in the gas stream formed in the reactor. All the data in the following tables is given in mol.%.

Table 1
Hydrogen24,48
Methane23,84
Ethylene0,73
Carbon monoxide12,57
Carbon dioxide37,10
Benzene0,75
Ethan0,06
Toluene0,025
Water0,45

The degree of conversion of methane is 38 mol.%, the selectivity of p is benzene equal 32,1 mol.%, the yield of benzene is equal to 12.2 mol.%, and selectivity for Cox is 15.2 mol.%.

Example 2

This example is carried out analogously to example 1, but with the flow of the source gas containing 40 mol.% methane and 60 mol.% carbon dioxide is additionally injected from the top of reactor 2 ml of the catalyst (2-20%) W-Mn3O4/(2-20%) Sr-L2O3. Obtained in example 2, the results shown in table 2.

Table 2
Hydrogen22,1
Methane18,1
Ethylene0,26
Carbon monoxide26,64
Carbon dioxide32,44
Benzene0,38
Ethan0,06
Toluene0,02

The degree of conversion of methane is to 39.6 mol.%, the selectivity for benzene equal to 19.2 mol.%, the yield of benzene is equal to 7.7 mol.%, and selectivity for Cox is 10.7 mol.%.

Example 3

Example 3 carried out analogously to example 1, but as the flow of the source gas using the reaction mixture containing 70 mol.% methane and 30 mol.% of carbon dioxide. The results of example 3 are shown in table 3.

Table 3
Hydrogen/td> 35,72
Methane36,7
Ethylene0,99
Carbon monoxide6,04
Carbon dioxide19,30
Benzene1,1
Ethan0,11
Toluene0,04

The degree of conversion of methane is 35,8 mol.%, the selectivity for benzene equal to 32.2 mol.%, the yield of benzene is equal to 11,53 mol.%, and selectivity for Cox is 43.5 mol.%.

Example 4

This example is carried out using the above example 3 conditions, but the maximum reaction temperature is 940°at the entrance to the reactor.

The results of example 4 are shown in table 4.

Table 4
Hydrogen22,90
Methane47,90
Ethylene1,20
Carbon monoxideto 2.57
Carbon dioxide24,54
Benzene0,78
Ethan0,09
Toluene0,02

The degree of conversion of methane is to 22.0 mol.%, the selectivity for benzene equal to 36.0 mol.%, the yield of benzene equal to 8.0 mole%, and selectivity for coke composition is yet 40,2 mol.%.

Example 5

The process in example 5 is carried out, using the above example 1, but used a reactor with an inner diameter of 25 mm. Pressure in the reactor is equal to 200 kPa. The results are shown in table 5.

Table 5
Hydrogen21,56
Methane27,80
Ethylene0,81
Carbon monoxide8,60
Carbon dioxide40,21
Benzene0,94
Ethan0,06
Toluene0,02

The degree of conversion of methane is 32,0 mol.%, the selectivity for benzene 41.5 mol.%, the yield of benzene is equal to 13.3 mol.%, and selectivity for Cox is 13.7 mol.%.

Example 6

The method of example 6 is carried out using the same conditions as in example 1, but without using a catalyst. The results are shown in table 6.

Table 6
Hydrogen19,35
Methane31,0
Ethylene1,05
Carbon monoxide5,10
Carbon dioxide42,50
0,82
Ethan0,05
Toluene0,02

The degree of conversion of methane is 28,0 mol.%, the selectivity for benzene equal to 40.6 mol.%, the yield of benzene is equal to 12,96 mol.%, and selectivity for Cox is 18.7 mol.%.

Example 7

The method of example 7 is carried out using the same conditions as in example 6, but using the reaction mixture containing 70 mol.% methane and 30 mol.% carbon dioxide.

The results are shown in table 7.

Table 7
Hydrogen35,72
Methane36,7
Ethylene0,99
Carbon monoxide6,04
Carbon dioxide19,31
Benzene1,1
Ethan0,11
Toluene0,04

The degree of conversion of methane is 35, 8 mol.%, the selectivity for benzene equal to 32.2 mol.%, the yield of benzene is equal to 11,53 mol.%, and selectivity for Cox is 43.5 mol.%.

Example 8

The method of example 8 is carried out using the same conditions as in example 6, but using the reaction mixture of 50 mol.% CH4, 40 mol.% CO2and 10 mol.% air, without the use of catalysts of the A.

The results are shown in table 8.

Table 8
Hydrogen18,84
Methane32,90
Ethylene0,88
Carbon monoxide5,32
Carbon dioxide37,08
Benzene0,76
Ethan0,07
Toluene0,02
Nitrogen4,13

The degree of conversion of methane at 25.8 mol.%, the selectivity for benzene equal 39,8 mol.%, the yield of benzene is equal to 10.3 mol.%, and selectivity for Cox is 44,75 mol.%.

Example 9

The method of example 9 is carried out using the same conditions as in example 3, but using a reactor having an inner diameter of 4 mm, the Results are shown in table 9.

Table 9
Hydrogen2,65
Methane65,78
Ethylene1,51
Carbon monoxide1,71
Carbon dioxide27,62
Benzene0,22
Ethan0,47
Toluene0022

The degree of conversion of methane is 10 mol.%, the selectivity for benzene equal to 20 mol.%, the yield of benzene is equal to 2 mol.%, and selectivity for Cox amounts to 19.8 mol.%.

The characteristics disclosed in the foregoing description and in the claims, both individually and in any combination, may constitute a material for carrying out the invention in its various forms.

1. A method of producing benzene, ethylene and synthesis gas, which comprises the following stages:

i) introducing into the reactor a flow of a source gas containing methane and carbon dioxide;

ii) oxidation of methane in the reactor under certain reaction conditions using the first catalytic material and/or additional oxidant;

iii) removing from the reactor the flow of gas formed, containing benzene, ethylene and synthesis gas, with the inner wall of the reactor processed first catalytic material.

2. The method according to claim 1, wherein the first catalytic material selected from the group consisting of Mn(NO3)2Si(WO4)2, KNO3, NaOH, and/or NVO3.

3. The method according to claim 2, in which the first catalytic material is mixed with the Sol-gel SiO2.

4. The method according to claim 1, wherein the oxidant is introduced together with the flow of the source gas or after the termination of the flow of the source gas.

5. Pic is b according to claim 4, where additional oxidant is oxygen, air, or a mixture of methane and oxygen and/or air.

6. The method according to claim 4 or 5, in which the concentration of the oxidizing agent relative to the volume flow of the source gas is not more than 2%vol.

7. The method according to claim 1, which is carried out in isothermal or non-isothermal conditions when the reactor there is a temperature profile of approximately 600°at the outlet of the reactor to approximately 1500°at the entrance to the reactor, approximately 700°With up to 1000°C.

8. The method according to claim 7, in which the flow of the source gas is introduced at a temperature of approximately 965°and the flow of gas formed is removed from the reactor at a temperature of about 715°C.

9. The method according to claim 1, in which the reactor is made of quartz, ceramic, aluminum alloys, stainless steel.

10. The method according to claim 1, wherein the second catalytic material is present in the reactor, preferably at the inlet of the heating zone of the reactor, preferably at the top of the reactor.

11. The method according to claim 10, in which the second catalyst is a basic oxide, such as MnO2WO3, SrO, La2About3the mixture MnO2with WO3or a mixture of SrO with La2About3or any mixture.

12. The method according to claim 1, in which the pressure in the reactor is from about 0.1 to 200 bar (10-20000 kPa).

13. The method according to claim 1, in which oterom time of contact of the first catalytic material with a gas flow of approximately from 0.1 to 90 C.

14. The method according to claim 1, in which the ratio of methane to carbon dioxide in the flow of the source gas is about 1-99 mol.%: 99-1 mol.%, preferably 40-60 mol.%: 70-30 mol.%, and more preferably 50 mol.%: 50 mol.%.

15. The method according to claim 1, wherein the reactor has an internal diameter of approximately 2 to 1000 mm

16. The method according to item 15, in which the ratio of the length of the reactor diameter is approximately from 1 to 200, preferably, from about 5 to 100.

17. The method according to claim 1, which is carried out continuously or periodically.

18. The method according to 17, in which at least part of the flow of the formed gas is recycled back into the reactor together with the flow of the source gas.

19. The method according to 17, in which at least part of the flow of the formed gas is rapidly cooled at the outlet of the reactor to further reduce the biodegradable products.

20. The method according to 17, in which, after removal of the flux generated gas from the reactor can be carried out stage of regeneration for the oxidation and combustion of coke.



 

Same patents:

The invention relates to the technology of basic organic synthesis, in particular the methods of chemical processing of natural gas to produce hydrocarbons and their derivatives, such as ethylene, acetylene, benzene, naphthalene, perchlorethylene, carbon tetrachloride, etc

FIELD: petrochemical processes and catalysts.

SUBSTANCE: invention provides high-silica zeolite catalyst comprising molybdenum and a second modifying element, namely nickel, content of the former in catalyst being no higher than 4.0 wt % and that of the latter from 0.1 to 0.5 wt %. Preparation of the catalyst involves modifying zeolite with molybdenum and second promoting element, the two being introduced into zeolite in the form of nano-size metal powders in above-indicated amounts.

EFFECT: enhanced efficiency of non-oxidative methane conversion process due to increased activity and stability of catalyst.

3 cl, 1 tbl, 7 ex

FIELD: production of monomers used for production of high-molecular compounds, alkylation of benzene by lower olefins in alkylator.

SUBSTANCE: proposed method is carried out in three stages: at the first stage, liquid hydrocabons, viz.: dehydrated benzene, polyalkylbenzenes and return benzene are mixed; at the second stage, ethylene and other olefins are introduced in liquid hydrocarbon mixture and at the third stage, aluminum chloride-based catalytic complex is introduced; at all three stages, flow moves in alkylator in turbulent mode; alkylator is provided with turbulization aids. Alkylator includes vertical cylindrical hollow housing with component inlet branch pipes fitted from below; components are delivered also through comb; branch pipes for discharge of reaction mass and gaseous products are mounted in the upper position. Housing is made from contraction tube, diffuser and cylindrical members interconnected coaxially. Initial component inlet branch pipes are located along housing axis; olefin and catalytic complex inlet branch pipes are located at distance from liquid hydrocarbon inlet branch pipes no less than two turbulization sections.

EFFECT: increased yield of alkyl benzene due to continuous process in small-sized equipment.

3 cl, 1 dwg, 3 ex

FIELD: petroleum chemistry.

SUBSTANCE: claimed method includes thermal hydrodealkylation of alkylaromatic compounds (e.g. toluene, benzene-toluene-xylene fraction of pyrocondensate, etc.) at increased temperature and pressure followed by recycling of un-reacted compounds. As additional raw materials phenol or other oxygen-containing aromatic fractions from various manufactures (e.g. phenol fraction from cookery production, phenol resin, acetophenon fraction or p-cumylphenol fraction from phenol production, etc.) are added to starting material in amount of 1-40 mass % based on mass of main raw materials. Process is carried out at 620-740°C, pressure of 2-5 MPa, 100 % hydrogen consumption of 700-1200 nm3/m3 of raw materials.

EFFECT: increased benzene yield, utilization of waste from various manufactures.

6 cl, 1 tbl, 1 dwg, 2 ex

FIELD: petroleum processing and petrochemistry.

SUBSTANCE: catalysate of reforming of long gasoline fractions containing more than 2% benzene is separated by rectification into three fractions: light-boiling fraction containing mainly nonaromatic C4-C6-hydrocarbons and no more than 1%, preferably no more than 0.5%, benzene; high-boiling fraction containing mainly aromatic and nonaromatic hydrocarbons C7 or higher and no more than 1%, preferably no more than 0.5%, benzene; and benzene fraction boiling within a range of 70-95°C and containing no more than 0.1%, preferably no more than 0.02%, toluene and no more than 0.02% nonaromatic hydrocarbons with boiling temperature above 110°C. Benzene fraction is routed into benzene isolation process involving extractive rectification with polar aprotic solvent having ratio of dipole moment to square root of molar volume above 0.3 db/(cm3/g-mole)1/2, preferably above 0.4 db/(cm3/g-mole)1/2, and boiling temperature 150 to 250°C.

EFFECT: improved quality of benzene.

4 dwg, 2 tbl, 5 ex

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: chemical technology.

SUBSTANCE: invention is designated for detoxification of chloroaromatic hydrocarbons or their mixtures by dechlorination method resulting to preparing benzene. Dechlorination process of chloroaromatic hydrocarbons is carried out by hydropyrolysis at temperature 700-850°C and in the mole ratio hydrogen : chloroaromatic hydrocarbons = (7-10):1 under pressure 0.1-5 MPa. Benzene is separated by rectification and the following recirculation unreacted chloroaromatic hydrocarbons. Formed hydrogen chlorine is adsorbed with alkali solution. Invention provides simplified technology, excluding toxic reagents and solvents in using and absence of toxic waste.

EFFECT: improved processing method.

12 ex

FIELD: chemistry of aromatic compounds, organic chemistry, chemical technology.

SUBSTANCE: method involves purification of benzene from thiophene in the presence of diene compounds, water and urotropin by its treatment with sulfuric acid solution at 20-40°C in cascade of mixing units and with fractional (distributed) feeding sulfuric acid solution in mixing units. Method provides simplifying the process and enhanced yield of benzene.

EFFECT: improved method for treatment.

3 cl, 3 tbl, 6 dwg, 7 ex

The invention relates to the chemical industry for the production of chlorobenzene method of chlorination of benzene, and can be used in the production of phenyltrichlorosilane (FTHS), where on the one hand, the chlorobenzene is used as a raw material, and on the other hand in the production FTHS as a by-product is formed benzene, chlorine - and organochlorosilane

The invention relates to a method of producing benzene from mixtures containing benzene and/or alkyl benzenes with a high content of sulfur-containing substances

The invention relates to a method, in which the flow of feedstock containing ethylbenzene, passed through a molecular sieve membrane, and device for its implementation

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to the improved method for oxidation of (C2-C4)-alkane and preparing the corresponding alkene and carboxylic acid. Method involves addition of this alkane to contact with molecular oxygen-containing gas in oxidative reaction zone and optionally at least one corresponding alkene and water in the presence of at least two catalysts with different selectivity. Each catalyst is effective in oxidation of alkane to corresponding alkene and carboxylic acid resulting to formation of product comprising alkene, carboxylic acid and water wherein the molar ratio between alkene and carboxylic acid synthesized in the reaction zone is regulated or maintained at the required level by regulation the relative amounts of at least two catalyst in the oxidative reaction zone. Also, invention relates to the combined method for preparing alkyl carboxylate comprising abovementioned stage in preparing alkene and carboxylic acid in the first reaction zone. Then method involves the stage for addition of at least part of each alkene and carboxylic acid prepared in the first reaction zone to the inter-contacting in the second reaction zone the presence of at least one catalyst that is effective in preparing alkyl carboxylate to yield this alkyl carboxylate. Also, invention relates to a method for preparing alkenyl carboxylate comprising the abovementioned stage for preparing alkene and carboxylic acid in the first reaction zone and stage for inter-contacting in the second reaction zone of at least part of each alkene and carboxylic acid synthesized in the first reaction zone and molecular oxygen-containing gas in the presence of at least one catalyst that is effective in preparing alkenyl carboxylate and resulting to preparing this alkenyl carboxylate.

EFFECT: improved method for oxidation.

30 cl, 1 dwg, 5 tbl, 14 ex

FIELD: petrochemical processes.

SUBSTANCE: invention relates to improved C2-C4-alkane oxidation process to produce corresponding alkene and carboxylic acid, which process comprises bringing indicated alkane in oxidation reaction zone into contact with molecular oxygen-containing gas and corresponding alkene and optionally with water in presence of at least one catalyst efficient for oxidation of alkane into corresponding alkene and carboxylic acid. Resulting product contains alkene, carboxylic acid, and water, wherein alkene-to-carboxylic acid molar ratio in oxidation reaction zone is controlled or maintained at desired level by way of controlling alkene and optional water concentrations in oxidation reaction zone and also, optionally, controlling one or several from following parameters: pressure, temperature, and residence time in oxidation reaction zone. Invention also relates to integrated process of producing alkyl carboxylate including above-indicated stage of producing alkene and carboxylic acid in first reaction zone and stage of bringing, in second reaction zone, at least part of each of alkene and carboxylic acid obtained in first reaction zone in contact with each other in presence of at least one catalyst effective in production of alkyl carboxylate to produce the same. Invention further relates to production of alkenyl carboxylate including above-indicated stage of producing alkene and carboxylic acid in first reaction zone and stage of bringing, in second reaction zone, at least part of each of alkene and carboxylic acid obtained in first reaction zone plus molecular oxygen-containing gas into contact with each other in presence of at least one catalyst effective in production of alkenyl carboxylate to produce the same.

EFFECT: enhanced process efficiency.

55 cl, 1 dwg, 7 tbl, 22 ex

FIELD: organic chemistry, petroleum chemistry, chemical technology.

SUBSTANCE: method involves preparing ethylene and hexane-1 from butene-1 by the exchange reaction of butene-1 and the isomerization reaction of synthesized hexane-3 to hexane-1. The parent material represents a mixed butene flow wherein butene-1 is isomerized to butene-2 after separation of isobutylene followed by the isomerization reaction of butene-2 to butene-1. Butene-1 is a raw for the exchange reaction.

EFFECT: improved preparing method, simplified technology process.

32 cl, 4 tbl, 4 ex

The invention relates to the chemical industry, namely, catalytic process for the production of ethylene from methane

The invention relates to the production of vinyl chloride

The invention relates to a method for obtaining enriched C2H4- fraction of the product from the purified, in particular, is exempt from CO2and dried hydrocarbon source faction

The invention relates to catalysts on the substrate, deposited on inorganic carriers, the following formula (I) ethylene, which is used in the basic reactions, including polymerization, copolymerization and polycondensation in the petrochemical industry and in fine organic synthesis, and their preparation

MA Pc/S

In addition, the invention relates to a new method of producing ethylene by means of direct conversion of methane or purified natural gas in the presence of the above catalyst and nitrogen at a temperature of from about 670 to 810oC, preferably in the range from 710 to 810oC, which is significantly below the reaction temperature normal synthesis of hydrocarbon(s) by dehydrogenation
Up!