阅读说明：本技术 具有提高的耐硫性的锰掺杂的镍甲烷化催化剂 (Manganese-doped nickel methanation catalyst with improved sulfur tolerance ) 是由 A·盖斯保尔 于 2019-03-06 设计创作，主要内容包括：本发明涉及使用催化剂使含有一氧化碳和/或二氧化碳、氢气和大于1ppb的硫的反应物料流中的一氧化碳和/或二氧化碳甲烷化的方法,所述催化剂包含氧化铝、Ni活性物料以及Mn,其特征在于,催化剂中的Ni/Mn摩尔比在1.0至15.0,优选2.0至12.0的范围内。此外,本发明涉及使含有一氧化碳和/或二氧化碳、氢气和大于1ppb的硫的反应物料流中的一氧化碳和/或二氧化碳甲烷化的方法,其中将反应物料流引导通过具有催化剂的反应器,和所述催化剂包含Ni活性物料以及Mn和具有1.0至15.0,优选2.0至12.0范围内的催化剂中的Ni/Mn摩尔比,其特征在于,所述催化剂吸收反应物料流中含有的硫并且同时催化甲烷化反应。(The invention relates to a process for methanation of carbon monoxide and/or carbon dioxide in a reactant stream containing carbon monoxide and/or carbon dioxide, hydrogen and greater than 1ppb of sulphur using a catalyst comprising alumina, a Ni active material and Mn, characterised in that the Ni/Mn molar ratio in the catalyst is in the range 1.0 to 15.0, preferably 2.0 to 12.0. Furthermore, the invention relates to a process for methanation of carbon monoxide and/or carbon dioxide in a reactant stream containing carbon monoxide and/or carbon dioxide, hydrogen and more than 1ppb of sulfur, wherein the reactant stream is conducted through a reactor with a catalyst, and the catalyst comprises a Ni active mass and Mn and has a Ni/Mn molar ratio in the catalyst in the range from 1.0 to 15.0, preferably from 2.0 to 12.0, characterized in that the catalyst absorbs the sulfur contained in the reactant stream and simultaneously catalyzes the methanation reaction.)

1. Process for the methanation of carbon monoxide and/or carbon dioxide in a reactant stream containing carbon monoxide and/or carbon dioxide, hydrogen and greater than 1ppb of sulphur using a catalyst comprising alumina, a Ni active material and Mn, characterised in that the Ni/Mn molar ratio in the catalyst is in the range 1.0 to 15.0, preferably 2.0 to 12.0.

2. The method of claim 1, wherein the catalyst is prepared by co-precipitation.

3. A process according to claim 1 or 2, characterized in that the molar ratio Ni/Mn in the catalyst is in the range of 2.0 to 6.0 or 3.5 to 5.5.

4. A process according to any one of the preceding claims, characterized in that the Al/Ni molar ratio of the catalyst is in the range of 0.1 to 0.9, preferably 0.3 to 0.7.

5. The method of claim 1, wherein the catalyst is prepared by impregnating alumina with a solution comprising Ni.

6. The method according to claim 5, wherein the solution comprising Ni further contains Mn.

7. Process according to any of claims 5 or 6, characterized in that the molar ratio Ni/Mn in the catalyst is in the range of 6.0 to 10.0, particularly preferably 7.5 to 9.5.

8. A process according to any one of claims 5 to 7, characterized in that the Al/Ni molar ratio in the catalyst is in the range of 2 to 9, preferably 2.3 to 5.

9. The method according to any of the preceding claims, characterized in that the reactant stream contains more than 1ppb, preferably more than 4ppb, particularly preferably more than 10ppb of sulphur.

10. The process according to any of the preceding claims, characterized in that the reactant stream contains from 1ppb to 100ppm, preferably from 4ppb to 50ppm, of sulfur.

11. A method according to any of the preceding claims, characterised in that the Ni active material has crystallites with a diameter below 20nm, preferably below 10 nm.

12. The process according to any of the preceding claims, characterized in that the catalyst has an absorption capacity at 35 ℃ of more than 200 μmol/g, preferably from 200 to 300 μmol/g.

13. The process according to any of the preceding claims, characterized in that the catalyst is contacted with the reactant stream at a temperature higher than 150 ℃, preferably higher than 200 ℃.

14. Process for methanation of carbon monoxide and/or carbon dioxide in a reactant stream containing carbon monoxide and/or carbon dioxide, hydrogen and more than 1ppb of sulfur, wherein the reactant stream is led through a reactor with a catalyst, and the catalyst comprises a Ni active mass and Mn and has a Ni/Mn molar ratio in the catalyst in the range of from 1.0 to 15.0, preferably from 2.0 to 12.0, characterized in that the catalyst absorbs the sulfur contained in the reactant stream and simultaneously catalyzes the methanation reaction.

15. The process according to claim 14, characterized in that the catalyst absorbs 90%, preferably all, of the sulphur contained in the reactant stream.

16. Use of a catalyst comprising alumina, a Ni active material and Mn for the methanation of carbon monoxide and/or carbon dioxide with gaseous hydrogen in the presence of greater than 1ppb of sulphur, characterised in that the Ni/Mn molar ratio in the catalyst is in the range 1.0 to 15.0, preferably 2.0 to 12.0, particularly preferably 3.5 to 5.5 or 7.5 to 9.5.

Background

The supply of energy by means of so-called renewable sources photovoltaic and wind energy suffers from fluctuations in the production of electricity due to weather and daylight. In order to ensure the safety of the supply, a way must be found to absorb fluctuations in the electricity production due to weather and daylight hours. One potential method for storing energy chemically is the power-gas method, in which excess current is used to crack water into hydrogen and oxygen by electrolysis. Hydrogen, in which energy is stored after electrolysis of water, can only be stored or transported to the user itself at high cost. According to the electricity-gas method, hydrogen is therefore converted in a further step into methane and water in a methanation reaction with carbon dioxide which acts in the atmosphere as a climate-damaging greenhouse gas. Methane can be easily stored in large existing infrastructures with storage capacities in the range of months, can be transported over long distances with little loss, and can be reconverted back to electricity when energy is needed. The methanation reactions associated with high energy release and usually carried out catalytically are the cornerstone of the process. Two direct problems arise from the high exothermicity of the reaction (-165 kJ/mol). On the one hand, at high temperatures, the thermodynamic equilibrium limits the maximum methane yield achievable. In order to feed methane to the natural gas network in germany, a purity of 95% is required. This requires high catalyst activity so that higher methane yields can be achieved at reaction pressures used in the industry and at low temperatures.

Reacting CO on a nickel-based catalyst₂And the hydrogenation of CO to methane, in order to ensure constant product gas quality, a consistently high activity and selectivity of the catalyst is required as far as possible. However, the activity and selectivity of catalysts in industrial applications decrease over time due to various deactivation mechanisms.

In addition to thermal and mechanical deactivation processes, chemical processes due to sulfur in the gas stream play an important role in particular.

As is known from practice and literature, very low proportions<Hydrogen sulfide in the order of 100ppbHas resulted in poisoning of the nickel catalyst with a concomitant loss of activity. In this case, H₂S reacts with nickel such that the poisoning front of the nickel sulfide migrates through the catalyst bed. The nickel sulfide may be formed by at least two Ni_xS_yTo describe: ni₃S₂(Nickel sulfide ore) and Ni₃S₄(stellite ore, polydemite).

Depending on the CO used₂Or a source of CO, which contains a corresponding amount of impurities. In the purification of CO from plants for biogas production₂(which contains H on the order of 200 to 1000ppm₂S), it is currently prepurified by expensive adsorption means to first remove sulfur impurities such as H₂S is reduced to a minimum.

In large industrial SNG plants based on coal gasification (SNG ═ synthetic natural gas), methanation reactions are also of critical importance. Will pass through the gasification of coal and subsequent conversion reaction (CO + H)₂O→CO₂+H₂) The hydrogen obtained is purified (for example by wet washing with cold methanol) and contains<Low sulphur loads of the order of 100 ppb. However, even this low sulfur loading may negatively impact the life of the subsequent synthesis reactor.

Catalysts with improved sulfur tolerance can reduce the cost of pre-purification or increase the life of the synthesis reactor, with positive effects on the economics of the overall plant.

US 4132672 a discloses an improved process for converting hydrogen and carbon monoxide to a methane-rich gas, wherein a supported nickel catalyst is used, which is promoted by the addition of a small percentage of iridium metal (typically 0.1 to 1.0 wt%). The promoted catalyst is very active in methanation and has good resistance to poisoning by sulfur compounds.

Because of CO and CO₂The methanation proceeds in a strongly exothermic manner, so in view of the reaction equilibrium, catalysts with increased resistance to sulfur at low temperatures are desired, but this is very challenging due to the exotherm of NiS formation. At a higher temperature (>600 ℃ C.), sulfur on nickelThe binding of the agent is reversible, but the position of the reaction equilibrium in the product gas towards a high share of methane is disadvantageous.

Disclosure of Invention

The object of the present invention is to provide a process for the efficient methanation of carbon monoxide and/or carbon dioxide with high selectivity and activity and improved stability in sulfur-containing reactant streams.

This object is achieved by a process for methanation of carbon monoxide and/or carbon dioxide in a reactant stream comprising carbon monoxide and/or carbon dioxide, hydrogen and more than 1ppb of sulfur using a catalyst comprising alumina, a Ni active material and Mn, characterized in that the Ni/Mn molar ratio in the catalyst is in the range from 1.0 to 15.0, preferably from 2.0 to 12.0, particularly preferably from 3.0 to 10.0, or particularly preferably from 3.5 to 5.5 or from 7.5 to 9.5.

It has been surprisingly found that Mn-containing Ni catalysts have high sulfur resistance as well as high sulfur capacity. The catalyst used in the process of the invention, in addition to its improved ability to catalyze the methanation reaction in the presence of sulfur ("sulfur tolerance"), at the same time exhibits the ability to absorb or reversibly bind sulfur ("sulfur capacity").

Furthermore, the invention relates to a process for methanizing carbon monoxide and/or carbon dioxide in a reactant stream containing carbon monoxide and/or carbon dioxide, hydrogen and more than 1ppb of sulfur, wherein the reactant stream is conducted through a reactor with a catalyst, wherein the catalyst comprises a Ni active mass and Mn and has a Ni/Mn molar ratio in the catalyst in the range from 1.0 to 15.0, preferably from 2.0 to 12.0, particularly preferably in the range from 3.0 to 10.0 or particularly preferably in the range from 3.5 to 5.5 or from 7.5 to 9.5, characterized in that the catalyst absorbs and simultaneously catalyzes the methanation reaction.

In addition, the invention relates to the use of a catalyst comprising alumina, a Ni active material and Mn for the methanation of carbon monoxide and/or carbon dioxide with gaseous hydrogen in the presence of more than 1ppb of sulfur, characterized in that the Ni/Mn molar ratio in the catalyst is in the range of 1.0 to 15.0, preferably 2.0 to 12.0, particularly preferably 3.0 to 10.0, or especially preferably 3.5 to 5.5 or 7.5 to 9.5.

Preferably, the catalyst absorbs more than 70%, more preferably more than 80% of the sulphur contained in the reactant stream during the process according to the invention, i.e. the product stream contains 70 or 80% less sulphur than the reactant stream during the process. It is particularly preferred that the catalyst completely absorbs the sulfur in the reactant stream during the process according to the invention, so that the product stream contains no more sulfur at all.

The catalyst according to the invention is particularly suitable for methanation of carbon monoxide and/or carbon dioxide by means of hydrogen in the presence of more than 1ppb of sulfur, preferably more than 4ppb, particularly preferably more than 10 ppb. 1ppb of sulfur corresponds here to a parts per billion volume fraction (10 parts per billion) of sulfur-containing molecules^-9) Where it is approximately assumed that each sulfur-containing molecule has only one sulfur atom. In particular, in the process according to the invention, the sulfur content is from 1ppb to 300ppm, preferably from 4ppb to 10ppm, of sulfur. 1ppm of sulfur corresponds here to a part per million by volume fraction (10 ppm) of sulfur-containing molecules^-6) Where it is approximately assumed that each sulfur-containing molecule has only one sulfur atom.

Methanation of carbon dioxide can be represented by the following reaction equation:

4H₂+CO₂→CH₄+2H₂O

methanation of carbon monoxide can be represented by the following reaction equation:

3H₂+CO→CH₄+H₂O

methanation is generally carried out at temperatures of from 180 ℃ to 600 ℃. During the process of carrying out methanation, the reactant gases containing carbon dioxide or carbon monoxide or a mixture of the two are brought into contact at a temperature of from above 180 ℃ to 600 ℃.

The catalyst contains alumina, a Ni active material and Mn, and the Ni/Mn ratio may (especially in the case of catalysts prepared by co-precipitation) be in the range 2.0 to 6.0, particularly preferably 3.5 to 5.5 or particularly preferably 4.0 to 5.0. Alternatively, the Ni/Mn ratio (especially in the case of catalysts prepared by impregnation) is in the range of 6.0 to 10.0, preferably 7.5 to 9.5, and particularly preferably 8.0 to 9.0.

The alumina need not be stoichiometric Al₂O₃But may also in this case be a non-stoichiometric alumina, preferably gamma-Al₂O₃。

The promoter Mn may be completely or partially contained in the Ni active material. The catalyst may contain a further promoter in addition to Mn, but it may also contain only promoter Mn. The oxidation states of Al, Ni, and promoters may vary depending on the treatment of the catalyst. Al, Ni and promoters are typically present as metal cations (e.g., Al)³⁺、Ni²⁺、Mn²⁺、Mn⁴⁺) Are present. After calcination (e.g., in air), a high or maximum oxidation state may be achieved. If the catalyst is reduced at temperatures above room temperature, for example under reaction conditions with hydrogen, Al, Ni and the promoter may adopt a low oxidation state or partially or completely appear in the oxidation state 0. The charge balance of the metal cation is via the oxygen anion (O)^2-) And (5) realizing.

The catalyst according to the invention is other than alumina (AlO)_xWhere x.ltoreq.1.5), Ni and Mn (and the oxyanions necessary for charge balancing), may contain further components, but may also consist only of aluminum oxide, Ni and Mn. The Ni active material may contain another promoter in addition to Mn, but it may also contain only promoter Mn. Preferably, the Ni active material does not contain an element selected from the group consisting of: b, Ta, In, Cu, Ce, Cr, Bi, Fe, P, Sb, Sn, Si, Ti, Zr, Co, Rh, Ru, Ag, Ir, Pd and Pt. Preferably, the Ni active material does not contain precious metals.

For the catalyst prepared by impregnation, the Al/Ni atomic (i.e. molar) ratio is preferably greater than 2, particularly preferably greater than 2.7, and in particular, the Al/Ni molar ratio is from 2 to 9, more preferably from 2.3 to 5.

For the catalyst prepared by coprecipitation, the Al/Ni molar ratio is preferably from 0.1 to 0.9, more preferably from 0.3 to 0.7, and particularly preferably close to 0.45.

The catalyst according to the invention can advantageously have crystallites in the Ni active mass with a diameter below 20nm, preferably below 10 nm. The Ni active material may also consist entirely or essentially of crystallites having a diameter below 20nm, preferably below 10 nm. The Ni active material is preferably present in the metallic state.

CO at 35 ℃ of the catalyst₂The absorption capacity can be greater than 150. mu. mol/g and is preferably in the range from 150 to 350. mu. mol/g, particularly preferably from 180 to 260. mu. mol/g.

BET surface area (S) of the catalyst according to the invention_BET) May be greater than 100m2/g, preferably greater than 200m2/g, or in the range of 100 to 200m2/g, preferably in the range of 150 to 180m 2/g.

Specific Metal surface area (S) of the catalyst according to the invention_met) Preferably greater than 10m2/g, preferably greater than 20m2/g and preferably in the range of 20m2/g to 70m 2/g. Specific metal surface area (S) for catalysts prepared by coprecipitation_met) Preferably in the range from 30 to 70m2/g, particularly preferably from 40 to 60m 2/g. Specific metal surface area (S) for catalysts prepared by impregnation_met) At 20 to 80m²In the range of/g, preferably from 25 to 70m²G or 30 to 60m²/g。

The catalyst used in the process according to the invention is preferably present in the reactor and forms a catalyst bed therein. The reactant gases are flowed through the reactor and are thus contacted with the catalyst. The reactor is heated at the same time, thus achieving the necessary reaction temperature of the catalyst.

Due to the increased sulfur capacity of the catalyst, in addition to its catalytic function, simultaneously functions as a sulfur trap ("trap" function). The catalyst in the catalyst bed near the reactor inlet absorbs sulfur and thus protects the downstream catalyst from sulfur poisoning. At the same time, the sulfur-loaded catalyst at least partially retains its activity in the methanation reaction. The catalyst used in the process according to the invention is advantageous in terms of an increased sulfur absorption capacity, so that in addition to functioning as a methanation catalyst, a function as a sulfur trap is achieved. The function as a methanation catalyst is thus enhanced due to the improved function as a sulphur trap. Ideally, the sulfur contained in the reactant gas is completely absorbed in the front region of the catalyst bed, so that in the rear region of the catalyst bed the reactant gas no longer contains sulfur and therefore no deactivation by sulfur takes place there.

The catalyst used in the process according to the invention can be prepared by coprecipitation. In preparing a catalyst by coprecipitation, a precipitation reagent is incorporated into at least one solution containing Al, Ni and Mn in dissolved form to obtain a precipitate.

The preparation of the catalyst by coprecipitation includes, for example, the following steps:

a) coprecipitated from a solution containing Al, Ni and Mn in dissolved form, to obtain a precipitate,

b) separating the precipitate from step a),

c) drying the separated precipitate from step b), and

d) calcining the dried precipitate from step c).

It is preferred here that the solution from step a) is an aqueous solution and that Al, Ni and Mn are present in the aqueous solution in dissolved form as ionic compounds.

Alternatively, the catalyst according to the invention can also be prepared by impregnation. The catalyst according to the invention is for example realised by simultaneous impregnation of nickel and manganese on a suitable alumina support.

The effect of improved sulfur tolerance and sulfur capacity of the precipitated (co-precipitated) and impregnated catalysts was observed. In general, impregnated catalysts cannot be prepared with as high a Ni content as precipitated catalysts, since the nickel uptake is limited during impregnation due to the pore volume of the alumina.

It has surprisingly been found that in the case of impregnated catalysts, the sulfur capacity, based on the amount of Ni used, is even somewhat greater than in the case of coprecipitated catalysts. This can be seen in fig. 2, where the amount of sulfur absorbed is normalized to the weight of the catalyst. Similar mass gains were obtained as in the case of catalyst a, despite the lesser metal loading of catalyst C.

Drawings

FIG. 1: the activity of catalysts a to C during the catalytic test reaction (test 1) decreased.

FIG. 2: the mass increase due to sulfur uptake of catalysts a to C during the catalytic test reaction was normalized to the weight of the catalyst (test 1).

FIG. 3: the activity during the catalytic test reaction was reduced compared to the sulfur uptake (test 1, assuming the formation of nickel sulfide).

FIG. 4: the activity of catalysts a and B decreased during the catalytic test reaction (test 2).

Method of producing a composite material

Elemental analysis

The determination of the composition of the calcined catalyst was carried out by means of inductively coupled plasma (ICP-OES) by optical emission spectroscopy. 50mg of the catalyst was dissolved in 50ml of 1 molar phosphoric acid (VWR, A.R.) at 60 ℃. To dissolve the pyrolusite formed, 50mg of Na was added to the solution₂SO₃(Sigma Aldrich, a.r.). After cooling, the solution was diluted at 1/10 and Na was incorporated at the same concentration₂SO₃And filtered through a 0.1 μm filter (Pall). Bring the calibration solution to 1, 10 and 50mg l^-1(Merck). The determination of the metal concentration was carried out with the aid of an Agilent 700 ICP-OES.

Determination of specific surface area

Specific surface area (S) of catalyst_BET) By means of N₂BET analysis was performed on NOVA 4000e (Quantachrome). For this purpose, 100mg of the catalyst were degassed at 120 ℃ for 3 hours and subsequently at a p/p of 0.007 to 1₀Adsorption and desorption isotherms were recorded over the range. For the determination of the BET surface area, p/p of 0.007 to 0.28 is considered₀Data points within the range.

Hg pore volume

The pore distribution and pore volume of the catalyst particles were carried out in accordance with DIN 66133 using a mercury intrusion instrument Pascal 440 from Thermo Electron Corporation. In this case, the sample was previously evacuated at room temperature for 30 min. The sample was measured in the range of 600 to 900mg and the pressure was raised to 2000 bar.

Chemical adsorption

Chemisorption experiments were performed on Autosorb 1c (quantachrome). Before the measurement, 100mg of catalyst was added at 500 ℃ in N ₂10% of H in₂And activating for 6 hours. Heating slope of 2Kmin^-1。

Metal surface area (S)_MET) Is carried out according to DIN 66136-2 (version 2007-01) and with the aid of H₂The chemisorption was carried out at 35 ℃. For this purpose 20 adsorption points were recorded equidistantly from 40mmHg to 800 mmHg. The calibration time for adsorption was 2min and the calibration time for thermal equilibration was 10 min. For the determination of the metal surface area, the metal atom/H stoichiometry is assumed to be 1. For CO₂Chemisorption measurement, with otherwise unchanged parameters, the equilibrium time for adsorption was set to 10 min. CO was experimentally excluded under these conditions prior to recording chemisorption data₂Possible kinetic inhibition of chemisorption. Combining the surface area of the metal with CO₂The absorption capacity is extrapolated to a pressure of 0mmHg according to extrapolation.

Synthesis of

Catalysts a and B were prepared by co-precipitation with 50 wt% Ni, which resulted in a 0.75 molar ratio of Al to Ni for catalyst a and 0.47 molar ratio of Al/Ni for manganese containing catalyst B. To investigate the effect of manganese on catalyst behavior, manganese (II) nitrate was added to the salt solution of nickel nitrate and aluminum nitrate during catalyst synthesis. All chemicals used were of analytical purity. The water was purified by Millipore filtration system and purity was verified by conductivity measurements. The synthesis was carried out in a double-walled 3l capacity stirred vessel. A double jacket filled with water allows to maintain the temperature of the synthesis additive at 30 ℃ by means of a thermostat, two baffles ensuring improved mixing. For stirring, a precision glass stirrer (KPG) may be used at 150 rpm. For the synthesis, 1L of H was placed in a stirred vessel₂O and adjusted to pH 9 ± 0.1. At a rate of 2.5ml min^-1The metered addition of the mixture of dissolved nitrates is carried out. While controlled addition of a precipitating reagent to maintain the pH. As starting material, a one-mole solution of each nitrate (Ni (NO) was used₃)₂*6H₂O、Al(NO₃)₂*9H₂O and Mn (NO)₃)₂*4H₂O). For catalyst B, they were mixed at a molar ratio of Ni to Mn of 4.6 to 1 andmixing Al to Ni of 0.45 mol ratio to 120ml min^-1And then added dropwise to the reactor. As precipitation reagents, 0.5M NaOH and 0.5M Na were used₂CO₃An equal volume mixture of solutions, a titrator was used for its metered addition. The suspension was aged overnight in the mother liquor with constant stirring, after which the precipitate was filtered and washed with H₂O wash until the filtrate has a neutral pH. After drying in an oven overnight at 80 ℃, the dried precipitate (precursor) was dried for 5K min^-1Is heated to 450 c and calcined under synthesis air for 6 hours.

Catalyst C was prepared by triple impregnation, each with subsequent calcination. 3022.0g of Ni (NO) are placed in a 5L beaker₃)₂x 6H₂O (98%), 307.9g of Mn (NO)₃)₂x 4H₂O (98.5%). The volume of about 2900ml was made up with deionized water and stirred with a propeller stirrer until a clear solution was obtained. Then make up to the desired total volume of 3441ml with deionized water.

First impregnation: 1879.3g of gamma alumina 1/8 "extrudates (corresponding to 3.6L; bulk density: 522 g/L; loss on ignition: 4.22%) are placed in a closable vessel. 1349ml of the impregnation solution was added slowly and in small amounts, which corresponds to the maximum amount of solution at which no supernatant had formed. During which the container is closed again all the time and shaken/homogenized. After the entire solution was added, shaking was performed for another 2 minutes.

First calcining: the impregnated extrudate was transferred to a porcelain dish and heated to 120 ℃ at 2 ℃/min and dried in air at this temperature for 6 h. The impregnated extrudate was then heated to 240 ℃ at 2 ℃/min and calcined in air at this temperature for 4 h.

Second impregnation: the extrudate impregnated once is placed in a closable container. 1147.0ml of the impregnation solution were added slowly and in small amounts, which corresponds to the maximum amount of solution at which a supernatant had not yet formed. During which the container is closed again all the time and shaken/homogenized. After the entire solution was added, shaking was performed for another 2 minutes.

And (3) second calcination: the impregnated extrudate was transferred to a porcelain dish and heated to 120 ℃ at 2 ℃/min and dried in air at this temperature for 6 h. The impregnated extrudate was then heated to 240 ℃ at 2 ℃/min and calcined in air at this temperature for 4 h.

And (3) third impregnation: the extrudate impregnated twice is placed in a closable container. 944.3ml of the impregnation solution were added slowly and in small amounts, which corresponds to the maximum amount of solution at which a supernatant had not yet formed. During which the container is closed again all the time and shaken/homogenized. After the entire solution was added, shaking was performed for another 2 minutes.

And (3) third calcination: the impregnated extrudate was transferred to a porcelain dish and heated to 120 ℃ at 2 ℃/min and dried in air at this temperature for 6 h. The impregnated extrudate was then heated to 240 ℃ at 2 ℃/min and calcined in air at this temperature for 4 h.

Thermogravimetric analysis and catalytic test reactions

To investigate deactivation due to hydrogen sulfide, thermogravimetric analysis (TGA) was used. In this case, the catalyst to be investigated is introduced into a heated forced flow reactor (1.53ml) and a reactant gas (79.5% by volume of H) is supplied₂20.5% by volume of CO₂(ii) a Reactant H₂The S content was 43ppm, T270 ℃, p 6 bar gauge pressure and SV ("space velocity" about 160001/h). The flow behaviour through the bed is in this case similar to that of a tubular reactor. The change in mass during the catalytic process can be detected by intermittent contactless weighing (precision ═ 10 μ g) via magnetic levitation coupling. The catalytic activity was also evaluated by measuring the product gas composition. For this purpose, the product gas substreams are analyzed by mass spectrometers. The results are shown in "catalytic test reaction", "test 1" and "test 2". To ensure comparability of the individual catalysts studied between the study sequences, the test conditions were kept constant. Because the catalysts in the oxidized form are produced by synthesis, they must first be brought to H before the test begins₂Reducing in the stream to produce a catalytic household metal phase. In this case the reduction is allowed to proceed so long until the weight remains constant. In this case, the reported weight of the catalyst is based on that weight after reduction, since from NiO to Ni or MnO₂Conversion to MnReduced to less than the original weight:

test 1: catalyst A: 1.27g, catalyst B: 0.93g, catalyst C: 0.90 g. Shows normalized H₂Conversion (0 corresponds to 0% conversion, 1 corresponds to 100% conversion).

And (3) testing 2: catalyst A: 1.02g, catalyst B: 1.05g of catalyst

Examples