Catalyst for oxychlorination of ethylene into 1,2-dichloroethane

FIELD: organic synthesis catalysts.

SUBSTANCE: catalyst includes Cu and Mg compounds deposited on alumina as carrier and has copper compounds, expressed as Cu, from 2 to 8%, Mg/Cu atomic ratio ranging from 1.2 to 2.5, wherein concentration of copper atoms is higher in the interior of catalyst particle than on the surface (layer 20-30 Å thick) thereof and concentration of magnesium atoms prevails on the surface of catalyst particle, while specific surface of catalyst ranged from 30 to 130 m2/g. Oxychlorination of ethylene is carried out under fluidized bed conditions using air and/or oxygen as oxidants in presence of above-defined catalyst. Catalyst is prepared by impregnating alumina with aqueous Cu and Mg solutions acidified with hydrochloric acid solution or other strong acids using volume of solution equal or lesser than porosity of alumina.

EFFECT: increased activity of catalyst at high temperatures and avoided adhesion of catalyst particles and loss of active components.

8 cl, 2 tbl, 5 ex

 

The present invention relates to catalysts for the oxychlorination process of ethylene to dichloroethane ((DCE)(EDC)), capable of providing a high degree of conversion without compromising selectivity at work in the fluidized bed at high temperatures, and to the way in which used catalyst.

The dichloroethane is an important intermediate product to obtain vinyl chloride, and consequently PVC, one of the most widely used polymeric materials.

Various technologies are used in the reaction oxychlorination process. The reactor can be a fixed bed or fluidized bed, and the air and/or oxygen can be used as oxidant.

The way fluidized bed is preferred over method with a fixed layer, because it has several advantages: low cost reactors (because they are not made of steel), nearly isothermal temperature distribution without hot spots (so with high selectivity and limited phenomena of aging).

In ways fluidized bed using catalysts based on copper salts, preferably, CuCl2mixed with various accelerators, such as salts of alkali metals, alkaline earth metals and rare earth metals. As carriers use what are media based on alumina or aluminum silicate (attapulgite, montmorillonite, silica, clay and so on); and alumina, having a particle size suitable for good pseudouridine, is usually preferred.

The catalysts should provide the following characteristics:

- to provide the most possible high output dichloroethane in the presence of a satisfactory selectivity and high activity (high degree of conversion of chloride-hydrogen acid);

to be able to work with good conditions pseudouridine, avoiding adhesion (stickiness of the polymer particles due to form CuCl2with low melting point); adhesion can be avoided by lowering the ratio between HCl and ethylene, but it is clear that this inevitably reduces the output dichloroethane;

to avoid loss of active elements and accelerators, which in addition to the deterioration of catalytic activity are the problem of pollution of wastewater;

to ensure high flexibility in production can be adapted to the high market requirements; in this case it is necessary to have catalysts that can operate at higher temperatures without deterioration of the selectivity and without increasing the loss of the active element and the accelerator.

Currently, the most competitive way fluidized bed is the way in which use color the d as oxidant: in these conditions the reaction is carried out with partial transformation and therefore recycling neprevyshenie ethylene and carbon oxides, which are the by-products in the reaction oxychlorination process. This technology has some important advantages: the transformation of hydrochloric acid is essentially complete; the effectiveness in relation to ethylene is in average higher than the efficiency obtained in the method using air (because ethylene is fully converted); the release of non-condensable gases in the atmosphere (vented) dramatically reduced because there is no need to remove it from the loop, as in the case of the method using air, nitrogen, supplied together with air.

This aspect is particularly important from the point of view of impact on the environment due to the low production of harmful chlorinated compounds in the environment; vented product can be discharged into the atmosphere without additional expensive treatments. Another advantage is the exception in comparison with the method using the air section of absorption and distillation of ethylene dichloride contained in the gases leaving the system.

An important parameter that can affect the yield of the reaction is the molar ratio of HCl/C2H4in the mixture of the reaction gases entering the reactor: the specified value is not stoichiometric (2), but is close to the stoichiometric value in the method using the receiving air (1,9-1.96) and is between 1.7 and 1.9 in the method using oxygen, since the concentration of ethylene include ethylene, which is fed back to the reactor with recirculation gas.

In the method using air with high ratios of HCl/S2H4selectivity is usually high, but the limitation is represented by the transformation chloride-hydrogen acid and defluidization.

In the method using oxygen with low molar ratios of HCl/C2H4turning chloride-hydrogen acid is facilitated, but, unfortunately, the reaction of combustion to carbon oxides is also facilitated, resulting in a loss of selectivity and therefore higher specific consumption of ethylene.

In order to compensate for this aspect, the temperature of the fluidized bed is typically low (215-225°): thus, the final yield of the reaction is more than 98 mol.% (the moth received EDC relative to the moles filed ethylene). The specific productivity of the system is low.

This fact is at odds with the modern trend of technology: manufacturer EDC seeks to increase the specific productivity of the system without the use of difficult investment in new reactors. To accomplish this, the flow rate of the reactants at the inlet of the reactor increases, correspondingly reducing the conversion of reagents(especially chloride-hydrogen acid), and this entails a reduction of the yield of way, but also causes serious problems associated with corrosion arising from neprevyshenie chloride-hydrogen acid. To solve this problem, increase the temperature of the fluidized bed, but this causes an increase in combustion reactions and the formation of undesirable chlorinated by-products that are not compensated by the decrease in residence time.

Therefore, in this area felt a great need to be the catalyst for oxychlorination process, which is capable of providing high selectivity at high temperatures (>230° (C) as in the method using oxygen and method using air.

Various patents, published patent literature, describe catalysts that have high selectivity at high temperatures.

For example, the application EP-A-582165 describes a catalyst based on copper salts, which contains various accelerators (salts of Mg, K and rare earth elements). The synergistic action of three accelerators, apparently, allows to obtain good selectivity.

Maximum operating temperature is 240°; selectivity of ethylene relative to pure dichloroethane is 94,98 mol.%; the selectivity to products of combustion extending t is 3,86 mol.%. The selectivity towards Triana (1,1,2-trichloroethane, the most important by-product of chlorination) is of 0.71%. Spend catalytic tests of the method using air; information regarding methods using oxygen is not given. The method of impregnation of the carrier is the way to "wet" (i.e. the way dry impregnation using a volume of solution equal to or less than the porosity of the substrate is not used).

U.S. patent 5227548 describes a catalyst which contains copper chloride and chlorides of Mg and K, which have a synergistic effect in the reduction of combustion of ethylene to CO and CO2. By the way get used in the examples is wet impregnation; used catalyst with a ratio of Mg/Cu, 0.3.

U.S. patent 5527734 describes a catalyst which contains copper chloride and chlorides of Mg and Cs deposited on gamma alumina, where the atomic ratio of Mg/Cu is at least 0.3 and can reach up to 2.6, but, preferably, not greater than 1.5 and, more preferably, 1.

The combined use of chlorides Mg and Cs is necessary in order to avoid contamination of the surface of the pipes used for cooling the fluidized bed.

The content of Cu in the catalyst, preferably, about 5-6 wt.%. The specified content is high: nooblet adhesion and adverse reactions (combustion and rich education 1,1,2-trichloroethane); the catalyst was prepared by dry impregnation, but without the use of acid solutions (chloride-hydrogen acid or other acids).

U.S. patent 4587230 describes a catalyst which contains copper chloride and chloride Mg in a ratio of Mg/Cu, 0.2 to 1.1, where the Cu atoms are located largely inside the catalyst particles than on its surface (the ratio X/Y is not less than 1.4, where X=Al/Cu inside the catalyst, and Y=Al/Cu on the surface).

Obtaining carried out by dry impregnation, the use of acid solutions of salts of Cu and Mg chloride-hydrogen acid or other acids in quantities of 1 mEq/g-atom Cu or treatment of a catalyst which contains si industrial type acidic chloride solution Mg.

The ratio of Mg/Cu, preferably, is (0,5-0,8):1.

The catalyst has good selectivity to EDC until temperature 230°C.

Now unexpectedly found that it is possible to obtain catalysts for oxychlorination process of ethylene to 1,2-dichloroethane (EDC) in the fluidized bed, which is able to provide the best performance (especially the selectivity at high temperatures)than known so far catalysts.

The catalysts according to the invention include a compound of copper, preferably copper chloride, in a quantity expressed by Cu, 2 to 8 wt.%, and the magnesium compound, preferably chloride, deposited on alumina as a carrier and is characterized by:

- the atomic ratio of Mg/Cu is equal to or greater 1,2, preferably between 1.3 and 2.5;

- distribution of copper atoms to a greater extent inside the catalyst particles than on its surface (layer 20-30 E) and a higher distribution of magnesium atoms on the surface (layer 20-30 E)than inside the particle;

- specific surface of the catalyst 30-130 m2/g, preferably 70-100 m2/year

In addition, it was found that the use of gamma-alumina containing less than 50 hours per million of impurities derived sodium compounds (expressed by Na), preferably, less than 10 hours/million, gives the catalysts that are more durable (less crumbly), have a high resistance to abrasion, do not give in the reaction of small particles, which can be lost through cyclone separators and/or can be deposited on the bottom of the tubes, cooling the layer, thus violating the heat transfer and, consequently, the regulation of the response.

As already noted, the catalysts allow you to work at very high temperatures, preferably above 235°With, in particular, from 240 to 265°without compromising EDC-selectivity of the catalyst. Higher heat transfer that can be achieved at higher temperatures than commonly used heat transfer, significantly increased the ü system performance. At the same productivity the surface of the cooling pipes, which are used, is smaller, and therefore the reactor is smaller. Higher activity of the catalyst, which can be obtained at high temperatures, however, without compromising EDC-selectivity, allows the use of less catalyst.

In addition, the catalysts can:

to avoid clumping when working with high molar ratios of Cl/S and loss of the active component and accelerator for industrial use;

to reduce the loss of small particles through the cyclone separators and copper compounds in the process;

- to increase the receiving dichloroethane with increasing total flow rate of the reagents without modification of the reactor.

The catalysts produced by the method of dry impregnation, i.e. when the volume of solution that is equal to or less than the porosity of the media.

Use acidic solutions chlorotoluron acid and/or other strong acids in quantities of, preferably, equal to 1-2 mEq/g-atom Cu.

The solution is sprayed onto the alumina is placed in the container, which is supported in rotation or also use the treatment in the fluidized bed.

After impregnation the catalyst is dried, for example, at 130°With during the night.

Used salts are preferably the chlorides, but also can what about the use of other salts, such as nitrates and carbonates, if they are soluble.

Determination of the distribution of copper and magnesium is performed by the XPS method (RFU) (x-ray photoemission spectroscopy). The method determines the surface concentration (layer 20-30 Å) atoms of Cu and Mg, i.e. the surface ratio of Al/Cu and Al/Mg.

For more information on this methodology, reference is made to U.S. patent 4587230 and 4871707.

In particular, the catalysts according to the present invention the ratio X=Al/Cu on the surface and Y=Al/Cu inside of the catalyst are such that X/Y is more than 1.2, and can reach up to 2.7 (for the atomic ratio of Mg/Cu is 2); the ratio of Al/Mg=Z on the surface and V=Al/Mg inside of the catalyst are such that V/Z is between 1.5 and 3. In particular, the Cu content of about 4 wt.% and the content of Mg to 2.1-2.3 wt.% and for ratios of Mg/Cu is 1.3 and 1.4, the ratio X/Y is 1.4 and 1.6.

The content of copper compounds expressed by Cu in the catalyst is preferably 4-5 wt.%.

The alumina used as the carrier has a surface area of 80-200 m2/g and is selected so that the catalyst has a surface 60-110 m2/g pore Volume is 0.4-0.5 g/ml; the distribution of particle size is preferably such that the catalyst fraction smaller than 40 μm is between 50 and 80 wt.% actually the exception fractions smaller than 20 microns.

The following examples lead to illustrate, not limit the invention.

Description of the method of producing catalyst

Various catalysts obtained using gamma-alumina with specific characteristics such as surface area (80-200 m2/g), pore volume (0.4-0.5 ml/g), purity(Na<2 hours/mn, Fe<15 hours/million) and the distribution of particle size as defined in the tables. The specified alumina is weighed and then impregnated with a solution which contains a salt of copper and accelerators, which corresponds to approximately 90% of the pore volume. Used salts are typically copper chloride (CuCl2·2H2O) and magnesium chloride (MgCl2·6N2O). To the solution was added HCl in the amount of 2.5 g (37 wt.% HCl), 100 g of alumina.

The salt solution obtained by dissolving these salts in distilled water, facilitating the dissolution of the weak heat; then the solution is dispersed in the alumina is placed in a cylindrical vessel (capacity 10 l, made of glass or quartz)which is maintained in rotation by means of a special device. The operation is performed slowly so facilitate complete homogenization.

After impregnation the catalyst is dried at 130°C overnight and then loaded into the reactor.

Used salts are usually chlorides, but you can use other salts, such as nitrates, carbonates and the like, if they are soluble.

The impregnation can be carried out in a cylindrical vessel or in the fluidized bed.

Determine chemical and physical characteristics of the thus obtained catalysts; their characteristics are shown in table 1. In addition, conduct research using the RFU to determine the distribution of copper and magnesium.

The description of the device used for catalytic tests

A device used to determine characteristics of various catalysts, consists of a glass reactor system flow control and chemical injection, cooling system for condensation and recovery of condensable products (EDC, H2O, containing HCl, chlorinated by-products). Non-condensable products (N2O2, CO, CO2, Ar) define, analyze by gas chromatography and discharged into the atmosphere. During the test (which lasts one hour) condensed products are collected in two phases, an aqueous phase and an organic phase. The two phases are separated and weighed neprevyshenie hydrochloric acid determined in the aqueous phase acid-metric titration, and the organic phase is analyzed by gas chromatography to determine the purity of the EDC and confirm the number of educated chlorinated FOB is cnyh products (especially in relation to 1,1,2-trichloroethane). As indicated, non-condensable gases identify and analyze by gas chromatography to determine2H4, CO2,, O2and N2. This way you can receive the full balance and to determine the characteristics of the catalyst, such as the conversion of chloride-hydrogen acid and ethylene selectivity of ethylene and chloride-hydrogen acid to EDC and the EDC purity.

The size of reactor: internal diameter 37 mm, height 300 see

Testing is carried out under pressure (4 kg/cm2with a linear speed of 9-11 cm/s and at operating temperatures from 220 to 265°C. Tests with air as the oxidant is carried out at a molar ratio Cl/S, equal 0,97-0,99 and 0.88 to 0.92 with O2(with recycling).

The experimental reactor is able to provide features that can be extrapolated on industrial reactor.

Example 1.

The catalyst with a content of Cu is 4.15% and Mg content 2,12% gain in accordance with the described methodology. The ratio of Mg/Cu is 1,336.

Used media (the same for all catalysts of comparative examples) has the following characteristics:

- surface area: 180 m2/g;

- pore volume: 0.45 ml/g;

- fraction particles from 63 to 40 microns: 40 wt.%;

the fraction of particles smaller than 40 microns: 32 wt.%.

Characteristics of the catalyst are summarized in table 1 which also shows the data relative to the catalysts of examples 2 and 3 and comparative examples 1 and 2. The table also presents data regarding the distribution of atoms of Cu and Mg, a specific method of the RFU, which show that when the ratio of Mg/Cu is increased, the distribution of copper (which in any case preferably distributed within the particles) inside the particles to a greater extent than on the surface, is less desirable, and that the magnesium, in contrast to copper, distributed more preferably on the surface.

All catalysts tested on pilot plant under the following conditions:

- Cl/S=0,89-0,9,

- O2/S2=0,53-0,56,

pressure = 4 kg/cm2,

the time of contact = 18-20,

linear speed = 10 cm/S.

The reaction conditions are typical for the method using oxygen: they are held constant as possible in the process of testing with different catalysts in order to have a meaningful comparison.

The results of various tests conducted at three temperatures (235, 245 and 255° (C)in table 2. The positive effect of increasing the ratio of Mg/Cu is obvious: the transformation of chloride-hydrogen of the acid is increased, EDC selectivity is improved by the reduction reactions of combustion and formation of chlorinated by-products: thus, it is possible to operate at higher temperatures without deterioration of the selectors is Yunosti.

Other improvements were achieved with the catalysts of examples 2 and 3.

1. The catalyst from example 2 are obtained from the same carrier as the catalysts of example 1 and comparative examples 1 and 2, with the difference that the surface area decreases to 83 m2/year

2. The catalyst of example 3 is obtained in media with different particle size, in which the fraction smaller than 40 μm is 59 wt.%.

The results in table 2 show that the two variants further improve the characteristics.

Comparative examples 1 and 2.

Catalysts receive and test as in example 1 with the only difference that the ratio of Mg/Cu is 0,676 in comparative example 1 and 0,988 in comparative example 2 (see table 1 chemical and physical characteristics and data on particle sizes and table 2 with the results of catalytic tests).

Examples 2 and 3.

Catalysts receive and test as in example 1 with the only difference that the ratio of Mg/Cu is equal to 1.402 in example 2 and 1,391 in example 3, and that the fraction of particles smaller than 40 microns is 59 wt.% the catalyst of example 3, and that the surface area of the two catalysts, respectively 83 and 98,7 m2/g (surface area of two carriers of 150 m2/g).

The catalyst of example 3 are also compared with the catalyst of example 1. When the Deposit is carried out in terms of the way using air, working with a molar ratio of Cl/S, equal 0,97-0,99. The test results confirm the positive effect of the fraction smaller than 40 microns. It is established that the dynamic characteristics of fluidized catalyst layer are satisfactory: the adhesion is not observed.

25,12
Table 1

The chemical composition and physical characteristics of the catalysts
CatalystsSRPSRPAPP.1PRPR
The chemical composition
Cuwt.%3,924,104,154,294,33
Mgwt.%1,0131,552,122,32,30
Mg/Cunuclear soothes.0,6760,9881,336to 1.4021,391
The surface composition (RFU)
Al/Cu wt.(Y)nuclear soothes.27.05 per24,1323,0622,82
Al/Cu RFU (x) wt.(X)nuclear soothes.52,45338,8the 33.438,47
X/Y1,942,111,611,451,69
Al/Mg wt.(V)nuclear soothes.43,8325,4118,0716,4516,40
Al/Mg RFU (Z)nuclear soothes.9,739,147,00of 6.688,83
Z/V0,220,360,390,410,54
V/Z4,502,782,582,46to 1.86
Physical characteristics
Surface aream2/g1301251238398,7
Apparent densityg/ml1,581,61,791,761,77
Fuck the ICH. densityml/d3,193,152,852,752,77
Pore volume.And0,320,3080,210,200,20
The average radius49,149,233,7949,2940,53
The distribution of particles by size
>125mcm0,80,60,510,3
125-90mcm4,55,03,55,81,4
90-63mcm19,223,8a 21.523,24,6
63-40mcm37,241,745,138,431,5
<40mcmto 38.328,929,431,659
<20mcm0,00,00,00,03,2

Table 2

Constant test conditions
Pressure (kg/cm2)4
Cl/S, mol. Rel.0,89-0,9
O2/S, mol. Rel.0,53-0,56
Contact time (s)18-20
Linear velocity (cm/s)10
Temperature (°)235
CatalystTransformationSelectivityPurity EDCOutput
%mol.% C2H4tomol.%mol.%
HClEDCCOxThe TrianaWith2H4to EDC
SRP99,7694,64,810,22199,4294,5
SRP99,6495,73,790,21999,5395,6
Example 1efficiency of 99.7896,62,930,20899,5396,5
Example 299,0198,11,010,16499,5698,0
Temperature (°)245
CatalystTransformationSelectivityPurity EDCOutput
%mol.% With2H4tomol.%mol.%
HClEDCCOxThe TrianaC2H4to EDC
SRP99, 4a 94.25,090,29899,2994,1
SRP99,494,7to 4.680,27899,3394,6
Example 199,695, 63,760,28799,3595,5
Example 299,397,02, 430,28599,3896,9
Example 399,297,61,810,2699,3997,5
Temperature (°)255
CatalystTransformationSelectivityPurity EDCOutput
%mol.% With2H4tomol.%mol.%
HClEDCCOxThe TrianaWith2H4to EDC
SRP97,793,65,520,42899,0493,5
SRPthe 98.994,64,490,37599,2094,5
Example 199,094,64,760,37399,2994,5
Example 2the 98.996,52,800,36899,2696,4
Example 3 the 98.996,662,700,32099,3596,6

1. The catalyst for the oxychlorination process of ethylene to 1,2-dichloroethane, comprising compounds of Cu and Mg, deposited on alumina as the carrier, and having a copper content, expressed in Cu, 2 to 8 wt.%, characterized in that the atomic ratio of Mg/Cu is from 1.2 to 2.5 with the distribution of copper atoms to a greater extent inside the catalyst particles than on the surface - layer thickness of 20-30 Åand atoms of magnesium to a greater extent on the surface - layer thickness of 20-30 Åthan inside the particles, and the specific surface of the catalyst ranges from 30 to 130 m2/year

2. The catalyst according to claim 1, characterized in that the ratio of Mg/Cu is from 1.3 to 2, and the distribution of copper atoms is such that the ratio X/Y is from 1.2 to 2.7, where X represents the ratio of Al/Cu on the surface and Y is the ratio of Al/Cu inside the catalyst particles, and the distribution of magnesium atoms is such that the ratio V/Z is from 1.5 to 3, where V represents the ratio of Al/Mg within the catalyst particles, Z is the ratio of Al/Mg on the surface.

3. The catalyst according to claims 1 and 2, characterized in that the specific surface area of the catalyst is 70-100 m2/year

4. Catalyst according to any one of claims 1 to 3, characterized in that the distribution of particles kata is Isadora size is the same what fraction smaller than 40 μm ranges from 50 to 80 wt.%, and the fraction smaller than 20 μm is practically absent.

5. Catalyst according to any one of claims 1 to 4, characterized in that the compound of copper is copper chloride and the magnesium compound is magnesium chloride.

6. Catalyst according to any one of claims 1 to 5, characterized in that the carrier is γ-alumina with such purity that the content of impurities, expressed by Na, is less than 10 hours/million

7. The method of producing dichloroethane oxychloination in the fluidized bed of ethylene using air and/or oxygen as oxidant and molar relationships HCl/C2H4in the mixture of the reaction gases entering the reactor, equal to 1.9-19,6 when using air and 1.7 to 1.9 when using oxygen, and when working at temperatures of reaction from 235 to 265°C, characterized in that the oxychloination carried out in the presence of a catalyst according to any one of claims 1 to 6.

8. The method of producing catalyst according to any one of claims 1 to 6, characterized in that the alumina is impregnated with aqueous solutions of salts of Cu and Mg, which are acidified with hydrochloric acid or other strong acids, using a volume of solution equal to or less than the porosity of the alumina.



 

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The invention relates to the chemical industry and plastics

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EFFECT: improved conversion method.

61 cl, 8 tbl, 32 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer from ethane and ethylene. Method involves generating the outlet flow from reactor by catalytic interaction in common of ethane, ethylene, oxygen and at least one chlorine source taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At the indicated stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst doesn't comprise iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more rare-earth material but not cerium. Indicated outlet flow from reactor is cooled and condensed to form flow of crude product comprising the first part of hydrogen chloride and flow of crude cooled hydrogen chloride comprising the second part of indicated hydrogen chloride. Then method involves separation of indicated flow of crude product for vinyl chloride monomer as the flow product and flow of light fractions comprising the indicated first part of indicated hydrogen chloride. Then indicated flow of light fractions is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at indicated generating stage. Also, invention proposes variants of a method for producing vinyl chloride from ethane and ethylene. Invention provides preparing vinyl (chloride) from ethane and ethylene by the complete extraction of hydrogen chloride from the reactor outlet flow.

EFFECT: improved producing method.

40, 9 tbl, 3 dwg, 31 ex

FIELD: organic chemistry, chemical technology.

SUBSTANCE: invention relates to a method for preparing vinyl chloride monomer. Method involves generating outlet flow from reactor by catalytic interaction in common ethane, ethylene, oxygen and at least one source of chlorine taken among hydrogen chloride, chlorine or chlorohydrocarbon wherein the mole ratio of indicated ethane to indicated ethylene is in the range from 0.02 to 50. At this stage of catalytic interaction method involves using a catalyst comprising component of rare-earth material under condition that catalyst has no iron and copper practically and under additional condition that when component of rare-earth material represents cerium then catalyst comprises additionally at least one more component of rare-earth material being except for cerium. Indicated outlet flow from reactor is quenched to form flow of crude product that doesn't comprise hydrogen chloride practically. Flow of crude product is separated for vinyl chloride monomer flow and light fractions flow and the latter flow is recycled for catalytic interaction in common with indicated ethane, indicated ethylene, indicated oxygen and indicated chlorine source at the indicated generating stage. Also, invention proposes variants of a method in producing vinyl chloride. Invention provides the complete extraction of hydrogen chloride from the reactor outlet flow after conversion of ethane/ethylene to vinyl (chloride).

EFFECT: improved producing method.

30 cl, 5 dwg, 9 tbl, 30 ex

The invention relates to the industrial catalyst, its acquisition and its use, especially for the production of 1,2-dichloroethane (EDC) oxychloination of ethylene in the reactor with a fluidized bed or in a reactor with a fixed layer

The invention relates to a method for producing 1,2-dichloroethane by reacting Athena with hydrogen chloride and oxygen or oxygen-containing gas on copper-containing catalyst in the fluidized bed

The invention relates to methods for organochlorine products and can be used in the chemical industry for the improvement of the production of vinyl chloride from ethylene

FIELD: petrochemical process catalysts.

SUBSTANCE: invention relates to synthesis of C5-C100-hydrocarbons from CO and H2, which catalyst contains carrier based on alumina prepared from gibbsite-structure aluminum hydroxide and cobalt in concentration of 15 to 50%. Carrier is prepared by mixing dry cobalt compound with dry gibbsite-structure aluminum hydroxide at cobalt-to aluminum molar ratio between 1:1 and 1:30, followed by calcination, impregnation (in two or more steps) with aqueous cobalt salt solution, and heat treatment. Invention also discloses process of producing C5-C100-hydrocarbons using above catalyst.

EFFECT: increased selectivity of catalyst regarding production of high-molecular hydrocarbons at reduced yield of methane.

7 cl, 1 tbl, 10 ex

FIELD: gas treatment catalysts.

SUBSTANCE: invention provides catalyst consisted of inert carrier and catalytic coating containing platinum, rhodium, and oxide substrate, wherein catalytic coating includes: (i) at least one first substrate material selected from group consisted of first active aluminum oxide enriched with cerium oxide; mixed oxide, which is cerium oxide/zirconium dioxide; and zirconium dioxide component; provided that catalytic component in at least one first substrate material is first portion of the total quantity of catalyst platinum, wherein concentration of the first portion of the total quantity of catalyst platinum lies within a range of 0.01 to 5.0% of the total mass of catalyst-containing materials; and (ii) a second substrate material containing second portion of total quantity of platinum and rhodium as catalytic component, said second substrate material being second active aluminum oxide, wherein concentration of platinum plus rhodium on the second substrate material lies within a range of 0.5 to 20% of the total mass of the second substrate material. Method for preparing above catalyst is also provided.

EFFECT: increased catalytic activity and reduced catalyst preparation expenses.

17 cl, 3 dwg, 5 tbl, 3 ex

FIELD: catalyst preparation methods.

SUBSTANCE: invention relates to a method for preparing catalyst and to catalyst no honeycomb-structure block ceramic and metallic carrier. Preparation procedure includes preliminarily calcining inert honeycomb block carrier and simultaneously applying onto its surface intermediate coating composed of modified alumina and active phase of one or several platinum group metals from water-alcohol suspension containing, wt %: boehmite 15-30, aluminum nitrate 1-2, cerium nitrate 4-8, 25% ammonium hydroxide solution 10-20, one or several precipitate group metal salts (calculated as metals) 0.020-0.052, water-to-alcohol weight ratio being 1:5 to 1:10; drying; and reduction. Thus prepared catalyst has following characteristics: specific coating area 100-200 m2/g, Al2O3 content 5-13%, CeO2 content 0.5-1,3%, active phase (on conversion to platinum group metals) 0.12-0.26%.

EFFECT: simplified technology due to reduced number of stages, accelerated operation, and high-efficiency catalyst.

5 cl, 1 tbl, 10 ex

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