Porous ceramic catalytical module and method of synthesis gas preparation in its presence

FIELD: chemistry; processing of hydrocarbon material to synthesis gas.

SUBSTANCE: porous ceramic catalytical module represents the product of exothermic finely dispersed nickel-aluminium mixture exposed to vibration compaction and to sintering. The said product contains: nickel 55.93-96.31 Wt%; aluminium 3.69-44.07 Wt%. Porous ceramic catalytical module may contain up to 20 Wt% (based on the module weight) of titanium carbide as well as catalytic coating including following groups: La and MgO, or Ce and MgO, or La, Ce and MgO, or ZrO2, Y2O3 and MgO, or Pt and MgO, or W2O5 and MgO in quantity 0,002-6 Wt% based on the module weight synthesis gas is produced by conversion of methane and carbon dioxide mixture on porous ceramic catalytical module in filtration mode The process conditions are as follows: temperature 450-700°C, pressure 1-10 atm, rate of CH4-CO2 mixture delivery to catalytical module 500-5000 l/dm3*hr.

EFFECT: inventions permit to carry out the process at lower temperatures.

5 cl, 37 dwg

 

The present invention relates to the field of processing of hydrocarbons and CO2in the synthesis gas, namely, the carbon dioxide reforming of methane (MRH).

Currently, natural gas is the main source of hydrogen and synthesis gas, which in the industry get in the various modifications of the energy-intensive processes steam reforming of methane. Another important issue is the need to include carbon dioxide cycle-critical processes. This problem is caused by a giant emission of CO2as a result of anthropogenic activities leading to irreversible loss of organic deposits on the planet.

The main fuel processing circuit of methane to liquid hydrocarbons using the synthesis gas is connected with the processes of synthesis of methanol, dimethyl ether Fischer-Tropsch process.

There are three methods of oxidative conversion of methane to synthesis gas:

steam conversion

partial oxidation with oxygen

carbon dioxide conversion

The industry uses almost the only method of steam reforming of methane, proceeding according to the equation (1). The reaction is carried out on the deposited Ni-catalyst at high temperature (700-900°). In addition energoemko is a considerable disadvantage of this process is the low stability of the catalyst in relation to coking.

Regarding the reaction of partial oxidation of methane with oxygen according to the equation (2), on the basis of the company "Shell" was developed technological process in non-catalytic version at very high temperatures (1100-1300° (C)that is implemented at a small factory in Malaysia. According to recent reports, the accident, this plant is not working now (Ovilo "carbon dioxide conversion of methane to synthesis gas").

A method for production of synthesis gas by carbon dioxide reforming of methane flowing through reaction (3), is still in the stage of laboratory and pilot tests (Ovilo "carbon dioxide conversion of methane to synthesis gas"). However, future development of this approach is the possibility of a significant expansion of raw material resources and a significant return CO2in organic products, including fuel.

Carbon dioxide reforming the methane (MRH) is devoted many works, mainly describing the processes in traditional flow-through reactors with a bulk catalyst, in which a high conversion of the reactants is achieved by high temperatures (800-1100°).

Disproportionation of methane to form carbon deposits under such conditions is very high, which leads to poisoning of the most catalysts, and therefore there is a necessity for regular regeneration.

The performance of the MRH in the presence of catalysts based on noble metals (Pt, Pd) allows to reduce the process temperature on average 200 degrees and reduce coke formation, but their high cost makes the process uneconomical.

The analysis of the patent literature on complex processing of gases containing methane and CO2showed that the known membrane ways MRH, using a dense membrane with a so-called oxygen conductivity and manufactured on the basis of complex oxides, mainly perovskite structure.

Thus, in patent CA 2420337 A1 and US 6492290 B1 processing of associated gas is conducted by the oxidation of methane on an ion-conductive membranes.

However, the performance of the described processes is very low. In addition, due to solid-state diffusion of lattice oxygen membrane material is subjected to mechanical failure.

In this regard, one of the most promising new approaches to addressing the processing of natural and associated gases can be considered a process-based porous catalytic membrane represents an ensemble of microreactors.

Works devoted MRH in the synthesis gas on porous membranes in the scientific and patent literature, could not be found.

The traditional solution MRH in the synthesis gas process is carried out in a flow reactor at a temperature of 1073 is, a pressure of 1 ATM, bulk catalytic system Ni/Al2O3. In these conditions it is possible to achieve the conversion of methane and CO2about 96%, at a ratio of N2/WITH the order of 0.96. A significant drawback of this process is the rapid deactivation of the catalyst due to the high share of coke formation processes.

The task of the invention is to provide a catalytic systems based on porous membranes, which are active in the method for production of synthesis gas by carbon dioxide reforming of methane.

To solve this problem is proposed porous ceramic catalytic module, which is a product of thermal synthesis compacted by vibrocompression fine exothermic mixture of Nickel and aluminum containing (in wt.%) Nickel 55,93-96,31, aluminum 3,69-44,07.

Porous ceramic catalytic module may contain titanium carbide in an amount of 20 wt.% in relation to the weight of the module.

To increase the activity of the catalytic system in the process for production of synthesis gas porous ceramic catalytic module may contain a catalytic coating comprising La and MgO or CE and MgO, or La, CE and MgO, or ZrO2, Y2O3and MgO, or Pt and MgO, or W2O5and MgO in an amount of 0.002 to 6 wt.% in relation to the weight of the module.

Also for solving the problems is a method for production of synthesis gas by reforming a mixture of methane and carbon dioxide, in which the conversion is carried out at a temperature of 450-700°and a pressure of 1-10 ATM in the filtration mode on the proposed porous ceramic catalytic module at a speed of feed of the mixture of methane and carbon dioxide through the module, equal 500-5000 l/DM3·h, and the ratio of methane to carbon dioxide in the mixture is from 0.5 to 1.5.

The following examples illustrate the present invention but in no way limit its scope.

Preparation of catalytic systems

Example 1. Preparation of sample Ni12Al

Porous ceramic catalytic module is made from compacted by vibrocompression fine exothermic mixture of Nickel and aluminum, including 96,31 wt.% Nickel and 3,69 wt.%. aluminum. The mixture is placed in a vacuum furnace, vacuum to a residual pressure of 1.5 to 10-3PA, raise the temperature before ignition of the mixture, kept at this temperature and then the sample is cooled.

Example 2. Preparation of sample Ni7Al12

Porous module is prepared analogously to example 1 from compacted by vibrocompression fine exothermic mixture comprising 55,93 wt.% Nickel and 44,07 wt.%. aluminum.

Example 3. Sample preparation, TiC 20% wt. + 80% wt. Ni6Al5

Porous ceramic catalytics the third module is prepared analogously to example 1 from compacted by vibrocompression fine exothermic mixture, including 57,84 wt.% Nickel, 22,16 wt.% aluminum, 15,98 wt.% titanium, as 4.02 wt.% of carbon.

Example 4. Preparation of sample Ni7Al12containing a catalytic coating applied La and MgO

On the inner surface of the porous channels of the module obtained in example 2, are lanthanum, taken in an amount of 0.02 wt.% and magnesium oxide, taken in an amount 5,98 wt.% in relation to the weight of the module.

Additional catalytic layer of metal oxides is formed in the internal volume of the porous channels of the module on the basis of organic solutions of metal complex precursors in toluene, taken in predetermined amounts to obtain oxides of a given composition, which after applying dried in vacuum and calcined at 500-600°C.

Example 5. Preparation of sample Ni7Al12containing a catalytic coating applied CE and MgO

On the inner surface of the porous channels of the module obtained in example 2, are cerium, taken in an amount of 0.02 wt.% and magnesium oxide, taken in an amount 5,98 wt.% in relation to the weight of the module. The application of the catalytic coating is carried out analogously to example 4.

Example 6. Preparation of sample Ni7Al12containing a catalytic coating applied La, Ce and MgO

On the inner surface of the porous channels of the module obtained in example 2, on osat lanthanum, taken in an amount of 0.02 wt.%, cerium, taken in an amount of 0.002 wt.% and magnesium oxide, taken in the amount of 6 wt.% in relation to the weight of the module. The application of the catalytic coating is carried out analogously to example 4.

Example 7. Preparation of sample Ni7Al12containing a catalytic coating applied La, Ce and Al2About3

On the inner surface of the porous channels of the module obtained in example 2, are lanthanum, taken in an amount of 0.02 wt.%, cerium, taken in an amount of 0.002 wt.% and aluminum oxide, taken in the amount of 6 wt.% in relation to the weight of the module. The application of the catalytic coating is carried out analogously to example 4.

Example 8. Preparation of sample Ni7Al12containing a catalytic coating applied ZrO2,Y2O3and MgO

On the inner surface of the porous channels of the module obtained in example 2, are zirconium oxide, taken in an amount of 0.02 wt.%, yttrium oxide, taken in an amount of 0.002 wt.% and magnesium oxide, taken in the amount of 6 wt.% in relation to the weight of the module. The application of the catalytic coating is carried out analogously to example 4.

Example 9.

Preparation of sample Ni7Al12containing a catalytic coating applied Pt and MgO.

On the inner surface of the porous channels of the module obtained in example 2, applied platinum taken in the quantity of a 0.012 wt.%, and magnesium oxide, taken in the amount of 6 wt.% in relation to the weight of the module. The application of the catalytic coating is carried out analogously to example 4.

Example 10. Preparation of sample Ni7Al12containing a catalytic coating applied W2O5and MgO.

On the inner surface of the porous channels of the module obtained in example 2, applied tungsten V, taken in an amount of 0.02 wt.%, and magnesium oxide, taken in the amount of 6 wt.% in relation to the weight of the module. The application of the catalytic coating is carried out analogously to example 4.

Obtaining synthesis gas by carbon dioxide methane conversion

Example 11 (sample TiC 20% + 80% Ni6Al5)

Carbon dioxide conversion of methane is carried out at a temperature of 600°and a pressure of 3 atmospheres in the filtration mode on porous ceramic catalytic module, prepared according to example 3 and fixed in the reactor volume, at a feed rate of the source gas mixture through the module 3000 l/DM3·h, and the ratio of CH4/CO2in a mixture of 0.75.

Converted gas mixture output from the external surface of the porous ceramic module from the reactor and sent to the analyzing device. Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that make up 44,58 and 19,39% is respectively, the composition of the synthesis gas H2/CO - 1,72, the productivity of the synthesis gas 1811,22 l/DM3module·h, coke formation 42%.

Example 12 (sample Ni12Al)

Conduct carbon dioxide methane conversion as in example 11 except that the porous ceramic module prepared according to example 1.

Determine the concentration of components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that make up and 29.67 per 16.69 per cent respectively, the composition of the synthesis gas H2/CO - 1,33, the productivity of the synthesis gas 1335,15 l/DM3module·h, coke formation 25%.

Example 13 (sample Ni7Al12)

Conduct carbon dioxide conversion of methane analogously to example 11, except that the porous ceramic module prepared according to example 2.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that are 35 and 25.2 percent, respectively, the composition of the synthesis gas H2/CO - 1,04, the productivity of the synthesis-gas - 1764 l/DM3module·h, coke formation 4%.

Example 14 (sample Ni7Al12containing catalytic coating La and MgO)

Conduct carbon dioxide conversion of methane analogously to example 11, except that the porous KERS the ical module prepared according to example 4.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who are 42 and 24,26%, respectively, the composition of the synthesis gas H2/WITH - 1,3, performance synthesis gas 1911,60 l/DM3module·h, coke formation 23%.

Example 15 (sample Ni7Al12containing catalytic coating CE and MgO)

Conduct carbon dioxide conversion of methane, as in example 11 except that the porous ceramic module prepared according to example 5.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who is 39 and 23,99%, respectively, the composition of the synthesis gas H2/CO - 1,22, the productivity of the synthesis gas 1825,2 l/DM3module·h, coke formation 18%.

Example 16 (sample Ni7Al12containing catalytic coating La, CE and MgO)

Conduct carbon dioxide methane conversion as in example 11 except that the porous ceramic module prepared according to example 6.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who are 60 and 42,44%, respectively, the composition of the synthesis gas H2/CO - 1,06, performance SinTe the-gas - 2997,77 l/DM3module·h, coke formation of 5.7%.

Example 17 (sample Ni7Al12containing catalytic coating La, CE and MgO granular)

Conduct carbon dioxide methane conversion as in example 11 except that the porous ceramic module prepared according to example 6 and granulated.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that make up 42,95 and 19,97%, respectively, the composition of the synthesis gas H2/CO - 1,61, the productivity of the synthesis gas 1789,17 l/DM3module·h, coke formation 38%.

Example 18 (sample Ni7Al12containing catalytic coating La, CE and Al2About3)

Conduct carbon dioxide conversion of methane, as in example 11 except that the porous ceramic module prepared according to example 7.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who is 72 and 27,54%, respectively, the composition of the synthesis gas H2/CO - 1,96, the productivity of the synthesis gas 2795,66 l/DM3module·h, coke formation 49%.

Example 19 (sample Ni7Al12containing catalytic coating ZrO2, Y2O3and MgO)

Prov is completed with carbon dioxide methane conversion as in example 11 except that that porous ceramic module prepared according to example 8.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who is 90 and at 13.84%, respectively, the composition of the synthesis gas H2/CO - 4,88, the productivity of the synthesis gas 2788,71 l/DM3module·h, coke formation of 79.5%.

Example 20 (sample Ni7Al12containing catalytic coating of Pt and MgO)

Conduct carbon dioxide methane conversion as in example 11 except that the porous ceramic module prepared according to example 9.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who is 58 and 41,33%, respectively, the composition of the synthesis gas H2/CO - 1,05, the productivity of the synthesis gas 2908,29 l/DM3module·h, coke formation 5%.

Example 21 (sample Ni7Al12containing catalytic coating W2O5and MgO)

Conduct carbon dioxide methane conversion as in example 11 except that the porous ceramic module prepared according to example 10.

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that make up CH4and CO2 58,5 and 41,68%, respectively, the composition of the synthesis gas H2/CO - 1,05, the productivity of the synthesis gas 2933,36 l/DM3module·h, coke formation 5%.

Example 22

Conduct carbon dioxide methane conversion as in example 16 at a temperature of 450°C. Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that make up 10,31 and 7.5%, respectively, the productivity of the synthesis gas 522,28 l/DM3module·h, the composition of the synthesis gas H2/CO - 1,03, coke formation is 3%.

Example 23

Conduct carbon dioxide methane conversion as in example 16 at a temperature of 700°C. Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who is 67 and 36,18%, respectively, the productivity of the synthesis gas 2963,31 l/DM3module·h, the composition of the synthesis gas H2/CO - 1,39, coke formation is 28%.

Example 24

Conduct carbon dioxide methane conversion as in example 16 at the space velocity of the reaction mixture through the module 500 l/DM3·h

Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who is 58 and 27,31%, respectively, the composition of the Blues the ez-gas N 2/CO - 1,59, the productivity of the synthesis gas 404,65 l/DM3module·h, coke formation is 37,21%.

Example 25

Conduct carbon dioxide methane conversion as in example 16 at the space velocity of the reaction mixture 5000 l/DM3·H. Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2who are 50 and 36,38%, respectively, the composition of the synthesis gas H2/CO - 1,03, the productivity of the synthesis gas 4221,43 l/DM3module·h, coke formation is 3%.

Example 26

Conduct carbon dioxide conversion of methane analogously to example 16, except that the ratio of methane and carbon dioxide gas in the source gas mixture is 1.5. Determine the concentration of the components of the gas mixture at the reactor exit and calculate the conversion of CH4and CO2that amount of 31.4% and 90% respectively, the composition of the synthesis gas H2/CO - 1,92, the productivity of the synthesis gas 1716,02 l/DM3module·h, coke formation is 48%.

Example 27

Conduct carbon dioxide conversion of methane analogously to example 16, except that the ratio of methane and carbon dioxide gas in the source gas mixture is 0.5. Determine the concentration of the components of the gas mixture at the outlet of the reactor and schityvat conversion of CH 4and CO2that make up 48.5 and 22.8% respectively, the composition of the synthesis gas H2/CO - 1,06, the productivity of the synthesis gas 1881,80 l/DM3module·h, coke formation is 6%.

Analysis of the above examples shows that the best results are achieved when carrying out the conversion of a mixture of methane and carbon dioxide gas at a temperature of 600°on porous ceramic catalytic module composition Ni7Al12containing catalytic coating La, CE and MgO, at a feed rate of the mixture of methane and carbon dioxide is taken in the ratio of 0.75 through module 3000 l/DM3·h, according to which the performance of the synthesis gas is 2997,77 l/DM3module·h, conversion of CH4and CO260 and 42,44%, respectively, the composition of the synthesis gas H2/CO - 1,06, coke formation is not more than 6%.

Thus, the proposed method will significantly reduce the size, reduce the amount of catalyst and lead to a substantial simplification of MRH in General. This implementation process is carried out at substantially lower temperatures (200-400°lower in comparison with the indicators of these processes realized in traditional flow-through reactor selectivity in the formation of synthesis gas, approaching 99%.), that, in its the turn will reduce energy costs and ensure efficient processing of CH4and CO2in valuable raw materials, alternative oil.

1. Porous ceramic catalytic module, which is a product of thermal synthesis compacted by vibrocompression fine exothermic mixture of Nickel and aluminum containing in wt.%: Nickel 55,93-96,31, aluminum 3,69-44,07.

2. Porous ceramic catalytic module according to claim 1, characterized in that it contains titanium carbide in an amount of 20 wt.% in relation to the weight of the module.

3. Porous ceramic catalytic module according to claim 1, characterized in that it contains a catalytic coating comprising La and MgO or CE and MgO, or La, Ce and MgO, or ZrO2, Y2O3and MgO, or Pt and MgO, or W2O5and MgO in an amount of 0.002 to 6 wt.% in relation to the weight of the module.

4. The method for production of synthesis gas by reforming a mixture of methane and carbon dioxide at elevated temperature and pressure, wherein the conversion is conducted at a temperature of 450-700°and a pressure of 1-10 ATM in the filtration mode on porous ceramic catalytic module according to any one of claims 1 to 3 at a feed rate of the mixture of methane and carbon dioxide through the module, equal 500-5000 l/DM3·h

5. The method according to claim 4, characterized in that the ratio of methane to carbon dioxide in the initial mixture with the hat from 0.5 to 1.5.



 

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3 cl, 3 tbl

FIELD: chemical industry; other industries; methods of production of the composite gradient-porous material.

SUBSTANCE: the invention is pertaining to the field of inorganic chemistry and the technology of production of the porous materials. On the surface of the substrate apply the uniform layer of the dry powder the metal oxide selected from the group of oxides of titanium, zirconium, aluminum or silicon, execute formation of the gel out of the selected oxide by humidification of the surface of the layer by the electrolyte solution having the coagulating properties in the given system, and conduct drying, then, at least, once repeat the operations of application of the powder, formation of the gel and its drying. After that on the dried layer of the gel again uniformly apply the layer the selected powder, humidify it with the electrolyte solution having the peptizating properties in the given system, and conduct the drying, repeat, at least, once, the operations of application of the powder, humidification of the layer by the solution with peptizating properties and drying, then conduct the annealing. The invention ensures production of the high-quality gradient-porous structures characterized by the high efficiency at simplification of the process of their production.

EFFECT: the invention ensures production of the high-quality gradient-porous structures characterized by the high efficiency at simplification of the process of their production.

4 cl, 2 tbl

FIELD: diaphragm technology; production of the composite oxygen- conducting diaphragms.

SUBSTANCE: the invention is pertaining to the diaphragm technology and may be used for separation of the gases. The composite oxygen-conducting diaphragm contains the solid ceramic layer with the ionic and-or electronic conductivity and at least one layer of the gas-permeable structure made out of the alloy containing the elements of the VIII and VI groups of Mendeleev's Periodic table of elements plus aluminum. The diaphragm consists of two layers of the gas-permeable structure and the solid ceramic layer arranged between them. The presented invention ensures the decrease of the difference of the linear expansion coefficients of the protective gas-permeable layer and the ceramic layer and prevention of the diffusion of the applied alloy into the ceramic layer.

EFFECT: the invention ensures the decreased difference of the linear expansion coefficients of the protective gas-permeable layer and the ceramic layer and prevention of the diffusion of the applied alloy into the ceramic layer.

6 cl, 3 dwg, 11 ex

FIELD: technology for producing semi-penetrable membranes for molecular filtration of gas flows and for division of reaction spaces in chemical reactors.

SUBSTANCE: method for producing gas-penetrable membrane includes two-sided electro-chemical etching of monocrystalline plate made of composition AIIIBV of n conductivity type or of semiconductor AIV with width of forbidden zone E≥1,0 electron volts and alloying level 1017-1020 1/cm3. Modes of aforementioned etching are set, providing for generation of simultaneously porous layers, while etching process is performed until moment of spontaneous stopping of electro-chemical process and generation of solid separating layer of stationary thickness on given part of plate area, determined using sharp bend on the curve of temporal dependence of anode current.

EFFECT: gas membrane, produced in accordance to method, has increased penetrability for molecules of light gases and increased selectivity characteristics at room temperature.

2 cl, 3 dwg, 3 ex

FIELD: chemical industry; methods of production of the olefins.

SUBSTANCE: the invention presents the method, in which from the source powders, fibers or fabrics consisting of carbides of elements of III-V groups of D.I.Mendeleev's periodic table, or aluminum oxides or silion oxides, or the materials representing glass or carbon fibers form the inorganic billet of the necessary form, in the macropores of the billet introduce the billet reinforcingpyrocarbon or impregnate it with phenol-formaldehyde resins with the subsequent carbonization. After that on the surface of the sintered or reinforced billet apply the gas-impermeable carbide layer of the adjustable depth (10-100 microns) by the gaseous phase depositions at the temperature of 800-1100°C, and then conduct halogenation of the carbide layer at the temperature of 400-1100°C. The method ensures production of the diaphragm suitable for separation of the gaseous mixtures.

EFFECT: the invention ensures production of the diaphragm suitable for separation of the gaseous mixtures.

2 cl, 1 tbl, 2 ex

FIELD: methods of sealing of built-up structures.

SUBSTANCE: the invention is pertaining to technologies of sealing of built-up structures. The invention offers a method of sealing, which makes it possible to form easily a sealing compaction, which has an exclusive reliability and a capability of repetition of a thermal cycle in the range of high temperatures of 800°C or higher. The offered built-up block contains: ceramics and a metal preferably used for a device intended for production of clear oxygen, the oxygen-rich air, etc.; a membranous reactor intended for the partial oxidation of a hydrocarbon gas; a solid-state oxidic fuel cell; a device of oxygen clearing; a heat exchanger or a similar device. The part of elements of the built-up unit is made out of an oxidic material and the tank is filled in with silver or a silver alloy. The offered invention ensures an increase of tightness of built-up frameworks. In particular, use of the units in the device intended for production of clear oxygen, the oxygen-rich air or in a similar device, in the membranous reactor for the partial oxidation of the hydrocarbon gas, in the solid-state oxidic fuel cell, in the oxygen clearing device, in the heat exchanger or in the similar device allows to speed-up significantly the production process.

EFFECT: the invention ensures an easy formation of a reliable tightness and significant speed-up of the production process.

25 cl, 19 dwg, 3 tbl, 7 ex

FIELD: purification of polluted liquids.

SUBSTANCE: the invention is dealt with purification of polluted liquids , in particular, with a ceramic filter for purification of polluted liquids. The ceramic filter contains at least one plate of the rectangular form made out of a porous oxide material with through channels, on the walls of which a membranous layer out of a source material is formed, and connectors between the channels. A maximum size of a channel cross-section, a plane thickness, a connection thickness and its width are in a definite dependence to each other. The mentioned filter is produced in the device for formation, which is supplied with a preheated receiving unit and a storage unit, a means for channels formation in the plate body by a method providing for a stirring of a ceramic material of different composition in parallel in the heated and not heated mixers, commixing of blends from the mixers, filling the device for formation with the produced mixture. A formed ceramic plate is directed into the preheated receiving unit, cut out a piece by a piece as the preheated receiving unit is filled and then directed to the storage unit. After extraction from the storage unit a plate is cut for measuring pieces and subjected to burning at the temperature of 1200-1550°C. The technical result is simplification of the method and the device at production of plates of big size with the thin walls of channels.

EFFECT: the invention ensures simplification of the method and the device at production of plates of big size with the thin walls of channels.

5 cl, 7 dwg, 53 tbl, 54 ex

FIELD: purification of polluted liquids.

SUBSTANCE: the invention is dealt with purification of polluted liquids , in particular, with a ceramic filter for purification of polluted liquids. The ceramic filter contains at least one plate of the rectangular form made out of a porous oxide material with through channels, on the walls of which a membranous layer out of a source material is formed, and connectors between the channels. A maximum size of a channel cross-section, a plane thickness, a connection thickness and its width are in a definite dependence to each other. The mentioned filter is produced in the device for formation, which is supplied with a preheated receiving unit and a storage unit, a means for channels formation in the plate body by a method providing for a stirring of a ceramic material of different composition in parallel in the heated and not heated mixers, commixing of blends from the mixers, filling the device for formation with the produced mixture. A formed ceramic plate is directed into the preheated receiving unit, cut out a piece by a piece as the preheated receiving unit is filled and then directed to the storage unit. After extraction from the storage unit a plate is cut for measuring pieces and subjected to burning at the temperature of 1200-1550°C. The technical result is simplification of the method and the device at production of plates of big size with the thin walls of channels.

EFFECT: the invention ensures simplification of the method and the device at production of plates of big size with the thin walls of channels.

5 cl, 7 dwg, 53 tbl, 54 ex

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