Method for selective oxidation of carbon monoxide in hydrogen- containing stream

FIELD: selective oxidation of carbon monoxide in hydrogen-containing stream.

SUBSTANCE: invention relates to method for selective oxidation of carbon monoxide to carbon dioxide in raw material containing hydrogen and carbon monoxide in presence of catalyst comprising platinum and iron. Catalyst may be treated with acid. Certain amount of free oxygen is blended with mixture containing hydrogen and carbon monoxide to provide second gaseous mixture having elevated ratio of oxygen/carbon monoxide. Second gaseous mixture is brought into contact with catalyst, containing substrate impregnated with platinum and iron. Carbon monoxide in the second gaseous mixture is almost fully converted to carbon dioxide, i.e. amount of carbon monoxide in product stream introduced into combustion cell is enough small and doesn't impact on catalyst operation characteristics.

EFFECT: production of hydrogen fuel for combustion cell with industrial advantages.

13 cl, 1 tbl, 4 ex

 

The scope of the invention

The invention relates to the catalytic oxidation of carbon monoxide. In accordance with other aspects, the invention relates to the selective oxidation of carbon monoxide in the presence of hydrogen. In accordance with another aspect of the invention relates to catalytic compositions effective for the oxidation of carbon monoxide. In accordance with another aspect of the invention relates to the removal of a maximum amount of carbon monoxide, preferably only carbon monoxide from a stream containing carbon monoxide and hydrogen, in particular to provide hydrogen feedstock for fuel cells.

Background of the invention

Selective oxidation of carbon monoxide enriched in hydrogen flows is of considerable technical interest for the purification of hydrogen produced in the reforming process used in the supply gas in the ammonia synthesis.

Recently, the process of selective oxidation, which is sometimes referred to as the preferred oxidation, attracts interest because of the possibility of using this technology to provide a suitable hydrogen fuel for fuel cells. Because carbon monoxide is oxidized to collect carbon dioxide, used in lasers di is xide carbon previously it was found that the catalyst, which is suitable for the oxidation of carbon monoxide for use in lasers carbon dioxide, can be adapted for use in providing a hydrogen containing carbon monoxide is intended for use as a feedstock for fuel cells.

A fuel cell is an electrochemical device that provides the possibility of transforming the chemical energy of fuels directly into electricity. The exhaust pipe of a fuel cell with a polyelectrolyte membrane (PEM) system for hydrogen-air at present is considered to be the best way to adapt this technology for most applications. Fuel cell with REM is most effective when used as fuel hydrogen gas. The use of the fuel processor to generate the enriched hydrogen raw material in the place of use eliminates the problems associated with storage and distribution of hydrogen fuel.

The fuel processor can turn fuels, such as alcohol, gasoline, liquefied petroleum gas or natural gas, enriched hydrogen stream. Using the method of reforming with steam you can get the stream, consisting mainly of hydrogen, diox is Yes carbon and carbon monoxide, but the product is usually saturated with water. During the processing of this flow in the reactor for the conversion of the content of carbon monoxide is reduced, thus providing a relatively greater amount of hydrogen through a well-known reaction of conversion of water gas. This reaction provides a product which contains from 0.2 to 2 vol.% carbon monoxide, which is sufficient to poisoning of the catalyst based on platinum REM anode. It is now established that in order to supply the hydrogen feedstock for fuel cells containing carbon monoxide on commercially suitable level, in addition to other possible ways of removal of carbon monoxide to the level required to prevent catalyst poisoning REM, can be used the same catalyst that is used for recombination of carbon monoxide and oxygen in lasers carbon dioxide. Working conditions for methods are essentially different. Compared to the conditions used for the recombination of carbon monoxide and oxygen in lasers carbon dioxide, the removal of carbon monoxide selective oxidation stream containing carbon monoxide and hydrogen, can be carried out using the same catalyst that is used in lasers carbon dioxide, p. the means of controlling increased flow of oxygen, supplied to the oxidation process, increasing the operating temperature of the oxidation process and avoid the reaction between oxygen and hydrogen.

The invention

There is a need for a method which is effective for the catalytic oxidation of carbon monoxide free oxygen. Another purpose of this invention is the provision of a method of converting carbon monoxide (CO) carbon dioxide CO2in the presence of hydrogen. It is also desirable to provide a method of obtaining hydrogen fuel for a fuel cell, in which the carbon monoxide (CO) into carbon dioxide (CO2in the presence of hydrogen in the scale, which is commercially appropriate.

In accordance with this invention proposes a method of selective oxidation of carbon monoxide to carbon dioxide in a gaseous mixture containing hydrogen and carbon monoxide. In this way a certain amount of free oxygen is mixed with the gaseous mixture containing hydrogen and carbon monoxide, with the receipt of the second gaseous mixture having a high molar ratio of oxygen to carbon monoxide. The second gaseous mixture is subjected to contact with a catalyst containing platinum and iron impregnated in the material of the carrier. The monoxide of carbon is and the second gaseous mixture as a consequence essentially completely converted into carbon dioxide. Used in this description, the expression "essentially complete conversion of carbon monoxide to carbon dioxide" or similar expression means that the amount of carbon monoxide present in the material stream entering the fuel cell is quite small, because they will not be significant impact on the functioning of the catalyst REM.

Detailed description of the invention

In accordance with this invention a method of oxidation of carbon monoxide in the stream of incoming material, which also contains hydrogen, can be implemented in such a way that preferably selectively oxidized WITH, and not the hydrogen, thus providing the means to deliver a stream of high-purity hydrogen for fuel cell in which the oxidation of carbon monoxide in the hydrogen fuel can be combined into one to generate the enriched hydrogen raw material in the place of use.

Arriving in the oxidation process gas can be formed by any suitable method, such as mixing before contacting with the catalyst of hydrogen that contains contaminating impurity carbon monoxide with air containing oxygen, anywhere.

The method of oxidation of the raw materials containing carbon monoxide and hydrogen gas, it is possible to carry out paragraph and any pressure during any period when any average hourly rate of gas supply and any volume ratio of O2to which are appropriate for the selective oxidation of CO in the presence of hydrogen in the temperature range from about 0 to about 300°C, preferably in the range of from about 25 to about 250°and most preferably in the range of from about 50 to about 200°C.

The pressure during the oxidation process is typically in the range from about 68,9 to about 6890 kPa (from about 10 to about 1000 pounds/inch2), preferably from about 96,4 to about 1378 kPa (from about 14 to about 200 pounds/inch2).

The ratio of the number of moles of O2in the incoming gas to the number of moles of CO in the incoming gas will typically be in the range of from about 0.5 to 8.0 mol O2/mol, preferably from 0.5 to 4.0 mol O2/mol, most preferably from 0.5 to 1.5 mol O2/mole.

Hourly average gas flow rate (CC incoming gas CC of catalyst per hour) may be in the range of from about 100 to about 200,000, preferably from about 5,000 to about 50,000.

The amount of hydrogen will typically be in the range of about 50-90 vol.%, and the number of input will typically be in the range of from about 0.1 to about 5 vol.%.

The preparation of the catalyst usable in the present invention, it is possible OS which may serve as a basis method, disclosed in U.S. patent No. 5017357 and U.S. patent No. 4943550, in the above patents discloses the ways in which the catalyst is used for the recombination of carbon monoxide and oxygen for lasers carbon dioxide.

As the material of the carrier for the composition of a substance used as a catalyst in the method of this invention may be used any of well-known materials for the media containing the metal oxide. Preferred at present are essentially pure alumina (aluminum oxide) titanium dioxide and/or aluminasilica spinel. More preferably the material of the carrier may contain at least 95 wt.% Al2About3or magnesium aluminate. These materials are commercially readily available.

The specific surface of the material carrier, which can be determined by BET method/N2(ASTM D3037), is typically in the range from about 10 to about 350 m2/, Media can be spherical, cylindrical, triangular, rectangular, annular, or it may have an irregular shape. The material of the spherical carrier typically has a diameter in the range from about 0.2 to about 20 mm, preferably from about 1 to about 5 mm.

The carrier can also be an inert porous ceramic material, having any of the above forms, p and can be coated with aluminum oxide and/or aluminasilica spinel.

Impregnation of the material of the carrier platinum and iron can be accomplished in any suitable way. Usually platinum compounds and iron compounds are dissolved in a suitable solvent, preferably in water, obtaining a solution of the appropriate concentration, usually containing from about 0.005-about 5.0 g of platinum on cm3solution and from about 0.005-about 5.0 g of iron per cm3solution. Suitable connections both platinum and iron are, inter alia, nitrates, carboxylates and acetylacetonates, while preferred are the acetylacetonates. In accordance with this invention as solvents for platinum or iron can be used organic solvents, such as methanol, ethanol, acetone, ethyl acetate, toluene or similar solvents. In practice, the preferred acetone.

The material of the carrier may be impregnated in a solution containing platinum compounds and/or compounds of iron, or it may be sprayed with a solution for impregnation of the carrier. The ratio of the impregnating solution to the material of the carrier is usually such that the final composition of the catalyst contains from 0.05 to about 10 wt.% platinum, preferably from about 0.1 to about 5 wt.% platinum and from about 0.05 to about 20 wt.% iron, preferably from about 0.1 to about 4 wt.% iron. In this volume from which retene also includes the use of any weight percentage of platinum and iron, when they act as copromotor oxidation WITH oxygen. At present, it is preferable to spray the solution containing the compound of the two metals on a carrier, but the metal compounds can be added separately in any order.

After impregnation material impregnated carrier is heated to a temperature sufficient to remove the solvent used in the impregnation. Can be used in a flow of inert gas fed through the surface of the material medium. For this purpose usually sufficient temperature in the range up to about 250°applied for approximately one hour.

The dried catalyst is treated by heating in an oxidizing atmosphere, preferably in an atmosphere containing free oxygen (such as air), typically at a temperature in the range from about 80 to about 700°With in a period of time ranging from about 0.5 hours to about 10 hours. The heat treatment is preferably carried out with a stepwise increase in temperature. The conventional heat treatment is carried out at 150°C for 1 hour, at 200°With - in 2 hours and at 400° - within 3 hours. Any combination of heating at a temperature for a time sufficient for annealing material impregnated carrier with the aim of obtaining at least one of platinum oxide, n is necessarily mixed with metallic platinum, and at least one of iron oxide, meets the requirements of this invention.

After oxidation calcined, impregnated with platinum/iron carrier is subjected to a reduction reaction, which can be accomplished in any suitable way, preferably at a temperature in the range from about 20 to about 650°S, more preferably from about 200 to about 500°C. Can be used any reduction gas such as a gas containing hydrogen, CO, gaseous hydrocarbons such as methane, mixtures of the aforementioned substances and similar substances. Preferably uses a gas containing free hydrogen, more preferably a gas stream essentially pure hydrogen. Stage of recovery can be performed within an appropriate period of time from about 1 minute to about 20 hours, preferably from about 1 hour to about 5 hours.

Restored impregnated platinum/iron carrier can be further processed by contacting with any suitable organic or inorganic acid having a pH of less than about 7. Preferably used an aqueous solution of nitric acid or carboxylic acid (preferably acetic acid). Previously restored impregnated platinum/iron carrier preferably soaked (permeate) in about 0.1-16 mol/l NGO 3usually at a temperature of from about 10 to about 80°during the period of time from about 0.01 to about 1 hour, but enough to get an initial wetting.

After acid treatment of the impregnated material of the carrier is heated to a temperature sufficient to remove the solvent used for the acid treatment. Can be used in a flow of inert gas supplied to the material of the carrier. For this purpose usually sufficient temperature in the range up to about 250°used for about an hour.

The dried, treated with acid catalyst is subjected to a heat treatment in an oxidizing atmosphere, preferably in an atmosphere containing free oxygen (such as air), typically at a temperature in the range from about 80 to about 700°With in a period of time ranging from about 0.5 hours to about 10 hours. The heat treatment is preferably carried out with a stepwise increase in temperature. The conventional heat treatment is carried out at 150°C for 1 hour, at 200°With - in 2 hours and at 400° - within 3 hours. Any combination of heating at a temperature for a time sufficient for annealing material impregnated carrier with the aim of obtaining at least one oxide of platinum, optionally mixed with metallic platinum, and at least on the aqueous iron oxide, meets the requirements of this invention.

Before use in the method of oxidation of carbon monoxide oxidized, treated with acid, the catalyst is platinum/iron on the carrier can be activated stage of recovery, which can be accomplished in any suitable way, preferably at a temperature of from about 20 to about 650°S, more preferably from about 200 to about 500°With the passage of time from about 0.5 hours to about 20 hours, preferably from about 1 hour to about 5 hours, to improve the activity of the catalytic composition for low-temperature catalysis of CO oxidation by oxygen in the presence of hydrogen. Can be used any reduction gas: hydrogen, CO, waxes and like substances and their mixtures.

The following examples are given to further illustrate the invention and should not be viewed as examples of limiting the scope of invention.

Example I

The catalyst precursor was obtained by weighing about 500 g of the spheres of aluminum oxide with a diameter of 1/8 inch (0,32 cm) (activated alumina Alcoa S-100) in two porcelain bowls are medium in size and progulivali at 800°C for 16 hours in the purged air muffle furnace. In a large porcelain bowl was placed 400 grams of dry calcined alumina and using conventional plastic the flask for manual spray spray impregnating solution, obtained by dissolving 8,07 g acetylacetonate platinum (II) platinum (II) 2,4 pentanedionate) and 10,13 g of iron acetylacetonate (III) at about 650 cm3of acetone. The media often mixed to ensure uniform distribution of the solution. When about 1/4 of impregnating solution was supported on a carrier, the catalyst placed in the exhaust furnace and was heated at 175°during the time from 45 minutes to an hour, this was accompanied by the removal of acetone and partial decomposition of acetylacetonates of metals. The processes of wetting, mixing and heating were repeated more than three times. When the impregnating solution was used, the catalyst was divided into equal portions, each weighing approximately 202 grams, and was placed in the purged air muffle furnace, heated at 150°C for 1 hour, at 200°C for 2 hours and at 400°C for 3 hours. In the specified heat treatment was received as a catalyst precursor 202 two-gram portions of the oxidized 1.0 wt.% platinum/0.4 wt.% iron aluminum oxide.

Example II

202 g portion of the catalyst precursor was transferred into a quartz reactor with a diameter of 2 inches (5.08 cm), which was then installed in a vertical tube furnace. The catalyst was activated recovery for three hours at 300°and atmospheric pressure using n is directed downward flow of hydrogen gas, flowing at a rate of about 200 cm3/min. the Catalyst and the reactor was cooled in a stream of hydrogen, was then purged with nitrogen, the result has been activated catalyst. The catalyst is a catalyst A.

Example III

Another 202 g portion of the catalyst precursor was transferred into a quartz reactor with a diameter of 2 inches (5.08 cm) and installed in a vertical tube furnace. The catalyst was restored within three hours at 300°and atmospheric pressure using the downward flow of the hydrogen gas flowing at a rate of about 200 cm3/min. the Catalyst and the reactor was cooled in a stream of hydrogen, was then purged with nitrogen. Newly restored, the catalyst was poured into a large bowl and soaked in a fume hood for approximately 60 cm3concentrated nitric acid. The acid impregnation was carried out by dropwise with stirring. To minimize oxidation under the action of atmospheric oxygen impregnation was carried out as quickly as possible. The acid-treated catalyst was dried and progulivali in the purged air muffle furnace, heated at 150°C for 1 hour, at 200°C for 2 hours and at 400°C for 3 hours. The catalyst was transferred into a quartz reactor with a diameter of 2 inches, which then set the vertical tubular furnace. The catalyst was activated recovery for three hours at 300°and atmospheric pressure using the downward flow of the hydrogen gas flowing at a rate of about 200 cm3/min. the Catalyst and the reactor was cooled in a stream of hydrogen, was then purged with nitrogen, the result has been activated the acid-treated catalyst. The catalyst is a catalyst Century

Example IV

When conducting experiments on the conversion used the following equipment. There were two separate mass flow controller Brooks 5850 E, one for the initial mixture containing CO, and the other for air flow. Containing the mixture was kept under high pressure in a 30-liter aluminum cylinder. Containing a mixture usually had a CO content of 1%, the rest to balance hydrogen. The air was applied from a system of air supply. Streams containing a mixture of air and United inlet is equipped with a jacketed glass tube, while the outer shirt was intended for circulation of the cooling medium. The glass tube was cooled in a bath of electrolyte circulation and temperature controlled, which could adjust the temperature to the desired temperature selected in the range from 5 to about 100°C. the Catalyst was loaded inside a glass tube.

The catalyst produces and, as indicated in examples I-III. The treated catalyst in the amount of 2.0 g were loaded into a glass tube with granular crushed quartz, filled in the empty space. Each catalyst was pre-treated for one hour with a stream of hydrogen flowing through the catalyst layer at a rate of 100 cm3/min, when heated to 97°C. the Experiments were carried out under the conditions shown in the table below. All experiments were performed at ambient pressure, GHSV (average hourly rate of gas supply) 10000 cm3incoming gas on cm3of catalyst per hour, used raw materials, which represented 1% of CO in hydrogen. Data were removed every 15 minutes, and the results obtained after 30 minutes, was recorded as the test result.

1td align="center"> 62,3
Table 1
Pt/Fe, Pt/Fe (treated with acid) in the presence of hydrogen
CatalystThe reaction temperature°The target molar ratio OF:The actual molar ratio O:SOThe conversion of O2,%The degree of CO conversion,%Neproreagirovavshimi CO(vol.%)The selectivity for CO2,%
And800,8100,159,30,427075,0
And8021,699,994,90,051961,1
And802,51,999,899,90,000651,6
And802,752,199,6100,00,0000to 47.2
And8032,399,4100,00,000043,3
In8010,8100,059,50,429076,6
In8021,5100,097,00,031462,7
In802,51.9100,0100,00,000051,7
In802,752,1100,0100,00,000047,0
In8032,399,9100,00,0000to 43.1
And2510,890,385,00,1570119,2
And251,51,287,696,50,0359br93.1
And2521,684,798,00,020274,4
And2532,380,5the 98.90,011452,9
And2543,1to 78.399,00,009341,1
In2510,894,688,70,1200120,7
In251,51,291,5the 98.90,011691,4
In251,751,488,3of 99.10,008982,3
In2521,585,599,30,007275,1
In252,51,982,699.60,0045
In2532,377,199,40,005755,6

Data show that as the Pt/Fe, and Pt/Fe (treated with acid) were effective as a catalyst in the conversion of CO in the CO2. Data conversion of oxygen show that the acid-treated catalyst had a higher activity than the catalyst, which was not treated with acid.

Received higher activity was present under all conditions, including very high average hourly rate of gas supply. At 80°and GHSV of 10,000 treated with acid catalyst provided a slightly higher degree of CO conversion, resulting remained fewer unreacted CO and had higher selectivity for CO2. At 25°and GHSV of 10,000 treated with acid catalyst provided a higher degree of CO conversion than the untreated catalyst that has led to a much smaller amount of unreacted CO and high selectivity for CO2.

Within the scope of this description and the appended claims may be made reasonable changes, modifications and alterations are intended for different conditions and applications.

1. Process for the selective oxidation of mono is xida carbon in carbon dioxide in the gaseous mixture, containing hydrogen and carbon monoxide, including

(A) mixing a quantity of free oxygen with the specified gaseous mixture containing hydrogen and carbon monoxide, with molar ratio of oxygen to carbon monoxide in the range of about 0.5-8.0 mol O2/mol of CO and the formation of the second gaseous mixture;

(B) contacting a second gaseous mixture at a temperature in the range of about 0°C-300°With the acid-treated catalyst containing platinum and iron impregnated in the material of the carrier, resulting in essentially complete conversion of carbon monoxide in the second gaseous mixture to carbon dioxide.

2. The method according to claim 1, wherein a material of the carrier is chosen from the group consisting of aluminum oxide, magnesium aluminate, and mixtures thereof.

3. The method according to claim 2, in which the material of the carrier is aluminum oxide.

4. The method according to claim 1, in which the acid-treated catalyst produced by the method, including

(1) impregnation of the material of the carrier with a solution containing a platinum compound and a solution containing a compound of iron, resulting impregnated with a mixture comprising a material impregnated media containing platinum impregnating compound containing iron impregnating compound, and a solvent;

(2) heating the impregnated mixture at a temperature and for a time sufficient for at least partial removal of the solvent, the resulting dried catalyst mixture;

(3) optional repeating steps (1) and (2)at least one time;

(4) heating the dried catalyst mixture in the presence of a gas containing oxygen, under oxidative conditions with the production of oxidized catalytic mixture;

(5) heating the oxidized catalytic mixture in the presence of a reducing atmosphere in the reducing conditions of obtaining the recovered catalyst mixture;

(6) contacting the recovered catalyst mixture with an acid to obtain the acid-treated catalyst mixture and

(7) contacting the acid-treated catalyst mixture atmosphere containing free oxygen at a temperature and for a time sufficient to ensure oxidized, treated with acid catalytic mixture.

5. The method according to claim 4, in which the oxidized catalytic mixture in contact with an atmosphere containing hydrogen at a temperature and for a time sufficient to provide for the recovered oxidized catalytic mixture.

6. The method according to claim 5, in which the material of the carrier is chosen from the group consisting of ethoxide aluminum, the magnesium aluminate and mixtures thereof.

7. The method according to claim 6, in which the material of the carrier is aluminum oxide.

8. The method according to claim 5, in which the temperature at which heat the impregnated mixture is in the range of about 125-225°and the time during which heat the impregnated mixture is in the range of about 0.5 to 1.5 hours

9. The method according to claim 8, in which the temperature at which the dried catalyst mixture in contact with an atmosphere containing free oxygen is in the range of about 100-600°and the time during which heat the impregnated mixture is in the range of about 0.5 to 1.5 hours

10. The method according to claim 4, in which the acid used for the acid treatment, is nitric acid.

11. The method according to claim 5, in which the temperature at which the oxidized catalytic mixture in contact with the atmosphere containing hydrogen, is in the range of about 200-400°and the time during which the oxidized catalytic mixture in contact with the atmosphere containing hydrogen, is in the range of about 2-4 hours

12. Process for the selective oxidation of carbon monoxide to carbon dioxide in a gaseous mixture containing hydrogen and carbon monoxide, including:

(A) mixing a quantity of free oxygen with the specified gaseous mixture containing hydrogen and carbon monoxide, are provided with the eat molar ratio of oxygen to carbon monoxide in the range of about 0.5-8.0 mol O 2/mol of CO and the formation of the second gaseous mixture;

(C) contacting the second gaseous mixture at a temperature in the range of about 0-300°With a catalyst containing platinum and iron impregnated in the material of the carrier, resulting in essentially complete conversion of carbon monoxide in the second gaseous mixture of carbon dioxide, where the catalyst was prepared by a method including:

(1) impregnation of the material of the carrier with a solution containing a platinum compound and a solution containing a compound of iron, resulting impregnated with a mixture comprising a material impregnated media containing platinum impregnating compound containing iron impregnating compound, and a solvent;

(2) heating the impregnated mixture at a temperature and for a time sufficient for at least partial removal of the solvent, the resulting dried catalyst mixture;

(3) optional repeating steps (1) and (2)at least one time;

(4) heating the dried catalyst mixture in the presence of a gas containing oxygen, under oxidative conditions with the production of oxidized catalytic mixture;

(5) heating the oxidized catalytic mixture in the presence of a reducing atmosphere to restore the nutrient conditions of obtaining the recovered catalyst mixture;

(6) contacting the recovered catalyst mixture with an acid to obtain the acid-treated catalyst mixture and

(7) contacting the acid-treated catalyst mixture atmosphere containing free oxygen at a temperature and for a time sufficient to ensure oxidized, treated with acid catalytic mixture.

13. The method according to item 12, in which the process of preparation of the catalyst comprises the additional step:

(8) contacting the oxidized, treated with acid catalytic mixture atmosphere containing hydrogen at a temperature and for a time sufficient to ensure recovered, oxidized, treated with acid catalytic mixture.



 

Same patents:

The invention relates to a process for the catalytic purification of hydrogen-containing gas mixtures of carbon monoxide and can be used in various fields of chemical industry, for example in the production of ammonia, and hydrogen energy, in particular, as a fuel for fuel cells

The invention relates to the production of gaseous commodity carbon dioxide from flue gases

The invention relates to a catalyst, the method of its preparation and process for the catalytic purification method from the carbon monoxide-enriched hydrogen gas mixtures

The invention relates to the field of combustion and can be used to produce steam or hot water and carbon dioxide

The invention relates to the field of synthesis of materials, which are used as catalysts for organic synthesis, and in particular to an improved method for producing a titanium-silicate catalyst for processes of selective oxidation of organic compounds by hydrogen peroxide

The invention relates to a method for preparing a catalyst which comprises a noble metal and a metal, which is the promoter of catalysis, in combination with the compound of the alkali or alkaline-earth metal deposited on the outer surface of the carrier

The invention relates to catalysts for production of vinyl acetate by reaction of ethylene, oxygen and acetic acid

The invention relates to a method for producing a catalyst for production of vinyl acetate by reaction of ethylene, oxygen and acetic acid containing porous media, porous surfaces of which is coated with an effective amount of copper, palladium and gold

The invention relates to the field of production of phenol, as well as preparation of catalysts for this process

The invention relates to an improved process for the preparation of vinyl acetate by reaction of ethylene, oxygen and acetic acid, used as reagents, including contacting the above reactants with a catalyst containing a porous medium, the porous surfaces of which is deposited catalytically effective amounts of metallic palladium and gold, copper in the form of free metal or copper acetate, and the fourth metal selected from the group consisting of magnesium, calcium, barium and zirconium, in the form of its oxide or mixture of oxide and free metal, at a temperature of 150-220oC and pressure up to 20 ATM

The invention relates to catalysts and method of removal of nitrogen oxides from both dry and wet and sulfur-containing exhaust gas hydrocarbons2-C16in oxidizing conditions

The invention relates to a new method for selective receipt of acetic acid and used in the catalyst

The invention relates to the discovery, before this time is appreciated that in the preparation of vinyl acetate using supported on a carrier catalyst containing palladium, gold and copper in which copper is essentially mixed with palladium or gold or both of these metals, the copper content in the catalyst during the lifetime of the catalyst tends essentially to decline, it is necessary previously to replace or regenerate the catalyst, the durability of which can approach or exceed two years

FIELD: selective oxidation of carbon monoxide in hydrogen-containing stream.

SUBSTANCE: invention relates to method for selective oxidation of carbon monoxide to carbon dioxide in raw material containing hydrogen and carbon monoxide in presence of catalyst comprising platinum and iron. Catalyst may be treated with acid. Certain amount of free oxygen is blended with mixture containing hydrogen and carbon monoxide to provide second gaseous mixture having elevated ratio of oxygen/carbon monoxide. Second gaseous mixture is brought into contact with catalyst, containing substrate impregnated with platinum and iron. Carbon monoxide in the second gaseous mixture is almost fully converted to carbon dioxide, i.e. amount of carbon monoxide in product stream introduced into combustion cell is enough small and doesn't impact on catalyst operation characteristics.

EFFECT: production of hydrogen fuel for combustion cell with industrial advantages.

13 cl, 1 tbl, 4 ex

Up!