A device for implementing partial oxidation and partial oxidation method

 

(57) Abstract:

The device for performing partial oxidation reactions mainly includes four working zones: zone (A), the distribution zone () with a constant or tapering cross-section along the axis of the device in the direction of the gas, preferably represents a massive part in the form of a cylinder, a truncated cone or truncated pyramid, consisting of one or more parts of the above solid piece with an optional replacement of the external or internal surface of the envelope curved surface in which the angle () generatrix with respect to the vertical line, parallel to the aforementioned axis, ranges from 0 to 65oFrom, the reaction zone (S) comprising the catalyst bed with an expanding cross-section along the axis of the device in the propagation direction of the gas associated with the above-mentioned area of distribution of the total cross-section, preferably represents a massive part in the shape of a truncated cone or truncated pyramid, consisting of one or more parts of the above solid piece with an optional replacement of the external or internal surface of the envelope curved surface in which the angle (a) forming in relation to vertical to improve the quality of the process when reducing the size of the device. 2 C. and 17 C.p. f-crystals, 2 ill., 3 table.

The invention relates to a device for the partial oxidation using an appropriate catalyst and to a method of partial oxidation.

This particular device may be used to produce synthesis gas by partial oxidation of natural gas in the presence of oxygen and/or air through the implementation of the following reactions:

CH4+ 1/2 O2---> CO + 2H2(1)

On an industrial scale partial oxidation of natural gas is carried out by using the technical solutions of the two types.

When applying technical solutions of the first type are non-catalytic reactors in which the reaction gases are mixed in the burner with water cooling and react in the combustion chamber (T=1300-1500oC) lined with refractory materials. In this process the reaction of partial oxidation (OP) (1) proceed in the following complete oxidation reactions (2) and cracking reactions (3):

CH4+ 2O2---> CO2+ 2H2O (2)

CH4---> C + 2H2(3)

In addition substoichiometrically combustion reaction cause a radical reaction dehydrogenization molecules with two or B. what estwennikami carbon residue.

The reaction products come at a temperature of 1400oC in the heat exchanger design and operation of which is complicated due to a combination of factors associated with high temperatures and the presence of carbonaceous residues. For elimination of carbonaceous residues from the product synthesis gas is washed with water.

The selectivity and conversion are dependent on various factors, among which the most important are the following:

- the design of the burner,

- the ratio of O2/C (gram-molecule of oxygen/gram-molecules of carbon atoms) in a mixture of reagents,

- reduced the residence time inside the reactor,

- rapid cooling of the reaction products, which are at intermediate temperatures (700-400oC) can still recombine for reforming methane and H2O using reaction

CO + 3H2---> CH4+ H2O (4)

When applying technical solutions of the second type are used Autoterminal catalytic reactors.

During this process, the flow of heated reactants are mixed at a temperature of 500-600oC in the burner located at the entrance of the reactor, generating a turbulent flame which extends into the combustion chamber, located between goralka the use of the natural gas to form a mixture of carbon monoxide and steam, and also generate heat required for the following strictly the endothermic reaction of the steam reforming process (5), and CO2(6):

CH4+ H2O ---> CO + 3H2(5)

CH4+ CO2---> 2CO + 2H2(6)

The latter takes place in the catalyst bed under the combustion chamber, filled with a catalyst based on Ni (15-30% by weight, precipitated spinel from oxides of aluminum and magnesium with high heat resistance). These reactors operate at an average hourly rate of gas supply, which is usually 5000-10000 NL (Lcat h) (IO/(lcat. hour), and in any case not higher than 15000 NL (Lcat h) (IO/lcat. hours).

As already mentioned, in the case of non-catalytic processes produced synthesis gas must be cleaned by flushing with water. On the other hand, in autothermal reactors unsaturated molecules and carbon residues are decomposed in the catalyst bed, making the flushing gas is unnecessary, the temperature at the outlet of the reactor are lower (typically 950oC). These characteristics simplify the characteristics of the heat exchangers for heat recovery gas emerging from the reactor and increase thermal efficiency of the process.

Recently, was published a number of patent applications (WO-95/18062, EP-576096, EP-EE at high pressure (P = 1-150 bar) in tubular reactors with an average hourly rate of gas flow from 20000 to 20000000 NL (Lcat h) (Nl/l cat. h).

In experiments conducted in the laboratories of the applicant, it was found that conditions of high temperature and high pressure, as claimed in these patents, challenging at pressures of 10 atmospheres and temperatures above 950oC described in terms of dynamic fluid as a mixture of the reactants and products are consumed in the gas phase, causing complete combustion of hydrocarbons with loss of selectivity towards CO and H2and the formation of carbon soot, which quickly clog the catalyst bed.

In a recent patent application by the same applicant (EP-640559) proposed a combined catalytic partial oxidation for the production of CO and H2and methanol synthesis, simple dimethyl ether and FT, in which formaldehyde is also produced, and these processes are carried out at temperatures from 100 to 950oC, at pressures from 1 to 40 atmospheres and at an average hourly rate of gas supply from 20,000 to 1,500,000 NL (Lcat h) (Nl/(l cat. h).

In this process, the working conditions are less stringent than in the three patents cited above, from which it also differs in the possibility of carrying out reactions with ratios2/CH4> 0,5 (vol/vol). Conditions the pressure exceeds 15 atmospheres.

Here the claimed catalytic reactor that improves the quality of the process proposed in the previous application of the present applicant, ensure the implementation of the partial oxidation reaction, which, besides having a considerably smaller compared to those used in industrial processes, does not require a burner and allows the catalytic reaction of partial oxidation, maintaining the velocity of the mixture of reactants is higher than the speed of combustion and avoiding the pressure drop due to the expansion of the gaseous mixture of the reaction products.

The device, which is the main subject of the present invention, includes four sequentially arranged work areas, namely:

- input area (A);

- the distribution zone (B) with constant or tapering cross-section along the axis of the device in the propagation direction of gas;

- the reaction zone (C), consisting of a layer of the catalyst with an expanding cross-section along the axis of the device in the propagation direction of the gas associated with the above distribution area by the total cross-section;

zone expansion gas (D).

Area distribution (B) preferably is a massive de is Anna massive detail with optional substitution of the form of their external or internal surface, envelope curved surface, where the angle (a) forming with the vertical, parallel to the aforementioned axis, ranges from 0 to 65omore preferably, from 10 to 45o.

Area distribution device filled with foam monoliths and/or particles of a ceramic material.

Preferably, the porous ceramic material is chosen from-Al2O3, AlxMgyOz, ZrO2and SiC.

The reaction zone (C) preferably represents a massive part in the form of a truncated cone or truncated pyramid, consisting of one or more parts of the above solid piece with an optional replacement of the form of their external or internal surface of the envelope curved surface in which the angle (a) forming with the vertical, parallel to the aforementioned axis, ranges from 5 to 65omore preferably, from 10 to 45o.

Area distribution performs the following functions:

- acts as a barrier to the spread of radical reactions towards the intake of raw materials as by accelerating the fluid, and due to the presence of inert surfaces, capable of capturing radicals;

- evenly distributes the fluid in the following functions:

- activates the reaction section, where the velocity of the gas is highest;

- carries out the further expansion of the fluid due to the increase in the number of gram-molecules and temperature without the problems caused by high losses of raw materials;

- maintaining speed on the surface in the entire layer above a critical value, which causes inflammation and the formation of carbon soot.

The terms of the dynamics of the fluid within the reaction zone should be such that not only avoid overheating of the reaction mixture, but also the pressure drop in the direction of propagation of the gas. The pressure drop occurs due to the rapid growth of the volume of the gaseous mixture in accordance with the narrowing of the catalytic zone. The stagnation of the mixture of the reagent before narrowing causes overheating and ignition, therefore, this stagnation should be avoided.

The change in the diameter of the reaction zone and, consequently, a decrease in gas velocity reduces the effect of the pressure drop. Different filling layer of catalyst particles with increasing diameter along the direction of propagation of the gas reduces the pressure drop.

The device which is the subject of the present invention, may have system> The method of partial oxidation using a device according to any one of PP 1-6, which is the second objective of the present invention mainly consists of the following steps:

- preliminary mixing and, after activation, pre-heated to temperatures from 200 to 600oC below the temperature of ignition, and the reagents include natural gas, oxygen or air, or air enriched with oxygen, optional steam and/or CO2so as to maintain the surface speed of the reaction gases above the speed of ignition and that the temperature of the mixture of reagents in the zone preceding layer of catalyst was below their ignition temperature;

- response by interaction of the catalyst and a mixture of the reactants in the reaction zone, the reaction is activated at a temperature of from 200 to 600oC and is carried out at space velocities of from 10000 to 10000000 NL reagents/L cat h (IO reagents/l cat. hour), more preferably from 100,000 to 5000000, with a temperature of from 700 to 1350oC.

Preferably, the reaction is activated at temperatures of from 250 to 450oC, while the flow rate is in the range from 100,000 to 5000000 IO reagents/l cat. hour.

The preferred ratio between the reagents in the reaction mixture, consisting of natural gas, air or air enriched with oxygen, possibly, steam and/or CO2these are:

the ratio between gram-vapor molecules/gram-molecules of carbon atoms in the hydrocarbon (pairs/Sec) ranges from 0 to 3.5, and more preferably from 0.1 to 1.5;

the ratio of gram-molecules of molecular oxygen/gram-molecules of carbon atoms in the hydrocarbon (O2/C) from 0.15 to 0.7, more preferably from 0.4 to 0.6.

The use of these bulk velocities allows you to consume very low amounts of catalyst and to achieve high performance, which is freely exceed the value of about 200000 m3CO + H2/day kg of catalyst, that is two times higher than the values achieved in the known processes for the production of synthesis gas.

Pristerene mixtures of gaseous reagents, allowing you to change the geometry in the reaction zone and to apply a higher pressure at lower surface speeds.

In the reactor used in this process are preferably used such catalysts, in which one or more noble metals (Rh, Ru, Ir, Pd, Pt, and so on) and/or Ni are deposited on the carrier, consisting of a material capable of withstanding high thermal and mechanical stress (usually SiC, AlxMgyOz, -Al2O3, ZrO2, yttrium stabilized Zirconia). These catalysts consist of compounds of one or more noble metals (preferably, Rh, Ru, Ir) and/or compounds of Ni deposited on a suitable carrier in an amount of from 0.05 to 15% by weight, preferably from 0.1 to 5% by weight. This operation is carried out in three ways.

The first method is implemented by using reactions solid - liquid by the interaction between media, dispergirovannykh in an organic solvent and solutions of clusters of noble metals such as Rh4(CO)12Ph6(CO)16Ir4(CO)12, Ru3(CO)12).

The second method is implemented by means of impregnation of solid carriers aqueous solutions SUB>2O, NiN3xH2O).

This method, which involves using a small carbonyl clusters of noble metals, provides the production of particularly active catalysts capable of initiating the reaction of partial oxidation at lower temperatures (typically 250oC). This method, involving the use of inorganic salts of noble metals, leads to the production of catalytic materials that can activate the combustion reaction only at temperatures above 350oC. In both cases, however, the activation temperature is much lower than used in burners non-catalytic reactors or catalytic autothermal reactors.

The third way to obtain catalysts involves the synthesis of intermediate product type hydrotalcite described in the patent application I T MA corresponding application EP-A-0725038 represented by the formula

[RhaENbXcYd(OH)2]Z+(Az/nn) mH2O,

in which X represents a bivalent cation or a monovalent metal, Y is a cation trivalent or tetravalent metal

0 a 0.5, 0 b 0,5, 0,5 c 0,9,

0 d 0.5, and a + b + C + d = 1,

mee is an anion, ISO - or heteropolyanions, anionic complex or organometallics complex having a charge n,

z represents the total charge of the cationic component.

Nuclear relations between the elements are preferably in the following ranges:

0 a 0,33, 0 b 0.33, c 0,66 0,8,

0 d 0,33.

The cation X bivalent metal is preferably selected from Mg, Ni, Co, Zn, Fe, Mn, Cu, Ca and Cd. The cation X monovalent metal preferably is a lithium. The trivalent cation metal preferably is selected from Al, Ga, Ni, Co, Fe, Mn, Cr, V, Ti and In. Cation Y tetravalent metal preferably is a Titan.

Intermediate chemical compound hydrotalcite subjected to heat treatment at temperatures above 700oC before use in catalytic reactions.

Preparation of material hydrotalcite described above may be implemented as described in the document "Catalysis today", 11, 173 (1991) (F. Cavani) (F. Cavani, F. Trifiro and A. Vaccari) and in the document "the increase in volume of clays and other microporous solids" (A. de Roy, S., Forno, K. El Malki and j. R. the Devil), ed. M. L. Ocelli and X. E. Robson, volume 2, Reinhold, new York, 1992, page 108).

Specifically, in the appropriate proportions salts of rhodium and/or ruthenium, bivalent or monovalent element and the other trivalent or tetravalent element. This solution is added with vigorous stirring and at a temperature of from 30 to 90oC, and preferably from 50 to 70oC, to a solution of carbonate of alkali metal or alkaline, and it is necessary to take measures, also with additional introduction of acids or alkalis, so that the pH value during the deposition was maintained in the range of 7-12, and preferably, 8-11. Thus, there is a simultaneous precipitation of all elements and their mutual thin dispersion. Formed crystalline precipitate is separated and washed with water, preferably hot, until you have a place alkali content, expressed as the oxide, of less than 0.1%. The precipitate is then dried at a temperature of 100oC and calcined in air or nitrogen at a temperature of from 200 to 1100oC, preferably from 350 to 950oC.

If we turn to the composition of the catalysts that can be used simultaneously as rhodium, and ruthenium, or rhodium and Nickel, and rhodium is used in the first layer catalyst layer, and a ruthenium or Nickel, the second layer of the catalyst under first.

In this case, the layer catalysate this configuration can be reduced, if it is necessary due to the lack and/or high cost of the use of rhodium in the entire catalyst bed, by completely replacing it by a ruthenium or Nickel, and the use of compounds with the characteristics of the load and reactions that are less favorable for cracking reactions of hydrocarbons.

With respect to the layer of catalyst, it is desirable to fill it with catalyst having increasing average particle diameter along the direction of propagation of the gas to increase the degree of vacuum and to reduce loss of load.

A particular advantage of the catalytic reactor described above and, accordingly, processes in which it is used, is to ensure the production of synthesis gas using mixtures containing air or air enriched with oxygen, reducing the formation of NOx.

This unexpected advantage allows the use of a catalytic partial oxidation reactor for the production of CO and H2for use in chemical processes, and to generate electric energy, gas turbines, avoiding, thus, the impact of pollution because of the formation of NOx.

Currently, pollution as a result of the under ammonia, the chemical bases which are summarized represented by the equation

NH3+ NOx---> N2+ H2O (7)

One of the embodiments of the present invention shown in Fig. 1, but it should not be considered as restricting the essence of the present invention.

The device comprises a first zone (A), followed by the distribution zone (B) with a tapering cross-section in the shape of a truncated cone having an angle forming with the vertical, 25ofollowed by the reaction zone (C) with section (1) in the form of a circle, in common with the previous area, with an expanding cross-section in the shape of a truncated cone having an angle forming with the vertical equal to the 35ofollowed by expansion area (D), consisting of a carrier (2) with a porous structure and a wider camera.

The following examples provide the best illustration of how a catalytic reactor, and the claimed method.

Example 1 - Comparative

Cylinders of refractory aluminum oxide having a form that allows them to contain the usual cylindrical layer of catalyst (diameter 15 mm, height 20 mm, weight 1 g), was injected into a cylindrical steel reactor, having a thickness of 1 cm and vnutrennyaya in-Al2O3with a porosity of 30 pores per inch (4,65 pores per square centimeter), containing 3% by weight of Ru. This noble metal has been precipitated by filing a drop of water solution of Ru (NO) (NO3)xH2O a monolith; then the monolith was subjected to calcination for 4 hours at a temperature of 550oC for the decomposition of salts of ruthenium. Metal media was subjected to heat treatment in an atmosphere of H2/N2= 1/1 (v/v) (volume/volume) at 600oC for 8 hours before the test catalyst.

The test was carried out at a pressure of 6 ATM, air cooling helped to maintain the temperature of the reactants at the inlet less than 300oC. the Number of thermocouples introduced in two membranes, the inner of which is made of steel and outer made of quartz, is located along the longitudinal section of the reactor, allowed to control the temperature in different places, specifically, on the inlet and outlet of the catalyst layer (respectively, at a distance of 5 and 9 mm from it). The mixture outcoming products were cooled with ceramic water heat exchanger. The duration of the test catalyst was 100 hours. During this test submission (1000 NL/h) (Nl/h) consisted of a mixture of CH4O2and H2O in the ratio of 2/1/1.

Examples 2-5

The cylinders of the refractory oxide of aluminum shaped to provide education zone gas distribution layer catalyst in the form of an hourglass, as schematically shown in Fig. 2, is introduced into a cylindrical steel reactor, having a thickness of 1 cm and an internal diameter of 5 cm

The device includes:

the first input area (A), which are loaded reagents, equipped with a cooling system using a suitable fluid medium (F);

- the distribution zone (B) with a tapering cross-section in the shape of a truncated cone having an angle forming with the vertical equal to the 20o, the outside of which is the cooling system;

the reaction zone (C) with section (1) in the form of a circle, in common with the previous area, with an expanding cross-section in the shape of a truncated cone having an angle forming with the vertical, 30owith the outer side of which there is a cooling system:

- postreaction area, including the carrier (2) with cellular structure and a wider camera, equipped with a cooling system.

Was obtained distribution system of the mixture of reagents using spherical particles of aluminum oxide (d = 1, 5-2 mm), subjected to calcination for 4 SUB>) 5 mm and a length (L) 20 mm Layer of catalyst (2,45 g) was formed using such particles of aluminum oxide, as used in the dispenser containing 0.5% Rh. Noble metal was deposited on the aluminum oxide by contact with a solution of Ru4(CO)12in n-hexane. After drying, the catalyst was loaded into the reactor and used in the reaction without any activating processing. The reaction zone has the following dimensions:

ri= 5 mm, rf= 25 mm, L = 20 mm

As a support for a spherical catalyst particles used porous monolithic ceramic disk with a porosity of 40 pores per square inch (6.2 pores per square centimeter) aluminum oxide (diameter 40 mm, thickness 20 mm).

The test was carried out at a pressure of 10 ATM. Thermocouple for temperature control at the inlet and outlet of the catalyst layer were located at distances of 25 and 27 mm, the test Length of the catalyst was 20 hours. The pressure drop was about 0.2 ATM. In these examples CH4/O2served in a volume ratio from 2.4 to 6. During testing of the catalyst gas temperature at the entrance to the distribution zone was maintained in the range from 250 to 300oC.

4and O2have also filed CO2in the ratio 8:4:1.

The results obtained are presented in table 2.

Examples 7-9

In this case, the distribution zone has a diameter at the inlet (ri) 15 mm diameter on the release (rf) 5 mm and a length (L) of 20 mm, while the catalytic reaction zone is characterized by ri5 mm, rf33 mm and a length of 30 mm

The catalyst was obtained with the use of such spherical particles of aluminum oxide, as described in examples 2-6, but with an increasing diameter from 1.5 to 5 mm as a support for the catalyst used porous ceramic disc zirconium oxide (40 pores per square inch) with a diameter of 40 mm and a thickness of 20 mm, the Test of the catalyst was carried out at a pressure of 17 ATM. To increase the heat and reduce the temperature at the inlet, used circuit air cooling system, consisting of a perforated copper tube having a ring shape and located around the reactor core. Thermocouple for temperature control at the inlet and outlet catalyst layer in both cases were located at a distance of 25 mm In the example 7 a mixture of reactants consisting of CH4< lodged in the ratio 4:2:1. Other experimental conditions were the same as in example 1. Operating conditions and results of tests of the catalyst described in examples 7, 8 and 9 schematically presented in table 3.

1. A device for implementing partial oxidation containing a working zone and a working zone of a reaction involving the catalyst, characterized in that it contains four sequentially arranged working area, the working area of the submission (A) is the working area of distribution (V) with constant or tapering cross-section along the axis of the device in the propagation direction of the gas, then is the working reaction zone (C) with a layer of catalyst and with an expanding cross-section along the axis of the device in the propagation direction of the gas associated with the said zone of distribution of the total cross-section, and the working area of the gas expansion.

2. The device under item 1, characterized in that the area of distribution (V) with constant or tapering cross-section is a massive piece in the form of a cylinder, a truncated cone or truncated pyramid, consisting of one or more parts mentioned solid piece, with optional substitution of the form of their external or internal surface of the envelope izobrazevanje, ranges from 0 to 65oand the reaction zone (C) With an expanding cross-section associated with the area of distribution of the total cross-section, is a massive piece in the shape of a truncated cone or truncated pyramid, consisting of one or more parts mentioned solid piece with an optional replacement of the form of their external or internal surface of the envelope curved surface in which the angle () generatrix with respect to the vertical line, parallel to the axis of the equipment mentioned above, is from 5 to 65o.

3. The device according to p. 2, characterized in that the angle () is from 10 to 45oand the angle () is from 10 to 45o.

4. The device under item 1, characterized in that the feed area is equipped with a cooling system of the reactants.

5. The device under item 1, characterized in that the expansion area is equipped with a cooling system.

6. The device under item 1, characterized in that the area of distribution and/or the reaction zone is equipped with a cooling system.

7. The method of partial oxidation using a device according to any one of paragraphs. 1 to 6, comprising the following stages: pre-mixing and after the activation of pre-heated to temperatures from 200 to 600C below the oxygen, optional steam and/or CO2so as to maintain the surface speed of the reaction gases above the speed of ignition and that the temperature of the mixture of reagents in the zone preceding layer of catalyst was below the ignition temperature response through the interaction of the catalyst and a mixture of the reactants in the reaction zone, and the reaction activate at temperatures from 200 to 600C and is carried out at space velocities of from 10000 to 10000000 IO reagents/l cat. h with the achievement of temperatures from 700 to 1350C.

8. The method according to p. 7, characterized in that the reaction is activated at temperatures of from 250 to 450C, while the flow rate is in the range from 100,000 to 5000000 IO reagents/l cat. h

9. The method according to p. 7, characterized in that among the reagents ratio between gram-vapor molecules/gram-molecules of carbon atoms in the hydrocarbon (pairs/Sec) ranges from 0 to 3.5, and the ratio of gram-molecules of molecular oxygen/gram-molecules of carbon atoms of the hydrocarbons (O2/C) is from 0.15 to 0.7.

10. The method according to p. 9, characterized in that the ratio between gram-vapor molecules/gram-molecules of carbon atoms in the hydrocarbon (pairs/Sec) ranges from 0.1 to 1.5, and the ratio of the leaves from 0.4 to 0.6.

11. The method according to p. 7, characterized in that the distribution device filled with foam monoliths and/or particles of a ceramic material.

12. The method according to p. 9, characterized in that the porous ceramic material is chosen from-Al2O3, AlxMgyOz, ZrO2and SiC.

13. The method according to p. 7, characterized in that the catalyst consists of a connection of one or more noble metals and/or compounds of Nickel deposited on a suitable carrier in an amount of from 0.05 to 15 wt.%.

14. The method according to p. 13, characterized in that the noble metal and/or Nickel deposited on the carrier are present in amounts of from 0.1 to 5 wt.%.

15. The method according to p. 13, characterized in that the noble metal is selected from rhodium, ruthenium, iridium, palladium and platinum.

16. The method according to p. 13, characterized in that the metals are rhodium and ruthenium or rhodium or Nickel, and rhodium are used in the first layer catalyst layer, and a ruthenium or Nickel in the second catalyst layer, located below the first.

17. The method according to p. 16, characterized in that the layer of catalyst containing rhodium, is from 20 to 35 vol.% from the entire catalyst layer.

18. The method according to p. 7, verhoeve heat treatment at temperatures above 700C before use in catalytic reactions, and has the following formula

[RhaENinXcYd(OH)2]z+(Az/nn)m H2OH,

where X represents a bivalent cation or a monovalent metal;

Y represents a cation trivalent or tetravalent metal

0 And 0.5, b 0,5, 0,5 to 0,9

0 d 0.5, and a + b + c + d = l,

m represents zero or a positive number,

And may be a hydroxide, any inorganic, organic anion, ISO - or heteropolyanions, anionic complex or organometallics complex having a charge n,

z represents the total charge of the cationic component.

19. The method according to p. 7, characterized in that the catalyst layer filled with a catalyst having increasing average particle diameter along the direction of propagation of the gas.

 

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FIELD: sorption neutralization of gases.

SUBSTANCE: proposed device includes two parallel horizontal gas-tight reactors arranged in casing at spaced relation; each reactor includes at least two sections filled with bulk granulated adsorbent and closed over ends with partitions carrying ejection pneumatic haulage units mounted above flow divider; device is provided with inlet and outlet branch pipes for delivery and discharge of gas; provision is made for V-shaped slide at angle of generatrices exceeding slope of repose for bulk adsorbent; V-shaped slide of each reactor is provided with drain branch pipe; walls of central reservoir are combined with hood excluding bridging of adsorbent; hood is equidistant relative to slide. Mechanism for hermetic discharge of used adsorbent includes longitudinal screw feeder and discharge pipe fitted with swivel gate valve; direction of turn of spiral provided on screw feeder of discharge mechanism is opposite to direction of main spiral.

EFFECT: improved quality of neutralization of gases; enhanced operational safety.

2 cl, 6 dwg

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