Methanation Kinetics

Bis(pyrazol-l-yl)methane, kinetic and thermodynamic lithiation, 56, 185 l,l-Bis(pyrazol-4-yl)prop-2-yne, 56, 34 Bis(trifluoromethylsulfonyl)imide, N-fluoro-, fluorination by, 59, 4 Bis(trifluoromethyl)tellurium,... 

Another approach to preparing model catalysts is the preparation of inverse supported catalysts . In this approach, the catalytically active metal (usually single crystal) is used as a substrate upon which an oxide is deposited, presumably leaving patches of exposed metal. This approach has been used to study reduction of ceria, and methanation kinetics on Rh as promoted by deposited ceria, and chemisorption of various molecules. As stated above, it is generally assumed that thick enough ceria layers will continuously cover the metal substrate, placing a limit on the thickness of the ceria islands that can be achieved for an inverse supported catalyst. The different procedures used for the inverse and metal particle on bulk oxide model catalysts is expected to produce differences in thermal stability, morphology and surface structure which may have consequences for the reactivity of the model catalyst. 

For reforming of methane, kinetics allow methane to decompose into carbon instead of reacting with steam even if thermodynamics predict no carbon formation. However, with proper reformer design, industrial operation at HgO/CH =... 

Experimental results of the reverse isotope effect observed upon replacement of Hj by D2 provide an interesting illustration of the difference in methane kinetics compared to that of the hydrocarbon chain growth reaction (see Scheme 16.2). 

Beebe T P, Goodman D W, Kay B D and Yates J T Jr 1987 Kinetics of the activated dissociation adsorption of methane on low index planes of nickel single crystal surfaces J. Chem. Phys. 87 2305... 

Anhydrous, monomeric formaldehyde is not available commercially. The pure, dry gas is relatively stable at 80—100°C but slowly polymerizes at lower temperatures. Traces of polar impurities such as acids, alkahes, and water greatly accelerate the polymerization. When Hquid formaldehyde is warmed to room temperature in a sealed ampul, it polymerizes rapidly with evolution of heat (63 kj /mol or 15.05 kcal/mol). Uncatalyzed decomposition is very slow below 300°C extrapolation of kinetic data (32) to 400°C indicates that the rate of decomposition is ca 0.44%/min at 101 kPa (1 atm). The main products ate CO and H2. Metals such as platinum (33), copper (34), and chromia and alumina (35) also catalyze the formation of methanol, methyl formate, formic acid, carbon dioxide, and methane. Trace levels of formaldehyde found in urban atmospheres are readily photo-oxidized to carbon dioxide the half-life ranges from 35—50 minutes (36). 

Fuel. Natural gas is used as a primary fuel and source of heat energy throughout the iadustrialized countries for a broad range of residential, commercial, and iadustrial appHcations. The methane and other hydrocarbons react readily with oxygen to release heat by forming carbon dioxide and water through a series of kinetic steps that results ia the overall reaction,... 

Flame or Partial Combustion Processes. In the combustion or flame processes, the necessary energy is imparted to the feedstock by the partial combustion of the hydrocarbon feed (one-stage process), or by the combustion of residual gas, or any other suitable fuel, and subsequent injection of the cracking stock into the hot combustion gases (two-stage process). A detailed discussion of the kinetics for the pyrolysis of methane for the production of acetylene by partial oxidation, and some conclusions as to reaction mechanism have been given (12). 

Only 20—40% of the HNO is converted ia the reactor to nitroparaffins. The remaining HNO produces mainly nitrogen oxides (and mainly NO) and acts primarily as an oxidising agent. Conversions of HNO to nitroparaffins are up to about 20% when methane is nitrated. Conversions are, however, often ia the 36—40% range for nitrations of propane and / -butane. These differences ia HNO conversions are explained by the types of C—H bonds ia the paraffins. Only primary C—H bonds exist ia methane and ethane. In propane and / -butane, both primary and secondary C—H bonds exist. Secondary C—H bonds are considerably weaker than primary C—H bonds. The kinetics of reaction 6 (a desired reaction for production of nitroparaffins) are hence considerably higher for both propane and / -butane as compared to methane and ethane. Experimental results also iadicate for propane nitration that more 2-nitropropane [79-46-9] is produced than 1-nitropropane [108-03-2]. Obviously the hydroxyl radical attacks the secondary bonds preferentially even though there are more primary bonds than secondary bonds. 

An anaerobic digester is a no-recycle complete mix reactor. Thus, its performance is independent of organic loading but is controlled by hydraulic retention time (HRT). Based on kinetic theoiy and values of the pseudo constants for methane bac teria, a minimum HRT of 3 to 4 days is required. To provide a safety factor and compensate for load variation as indicated earlier, HRT is kept in the range 10 to 30 days. Thickening of feed sludge is used to reduce the tank volume required... 

Englezos, P., Kalogerakis, N., Dholababhai, P.D. and Bishnoi, P.R., 1987a. Kinetics of fonuation of methane and ethane gas hydrates. Chemical Engineering Science, 42(11), 2647-2658. 

Pavlinec and Lazar [39] reported that organic hydroperoxide and piperidine(PD) could be used as an initiator for MMA polymerization. In our laboratory, we also found that TBH-NMMP, TBH-NEMP [20], TBH-PD(piperidine) [31], TBH-NEP(N-ethylpiperdine) [31], TBH-TMDAPM (N,N -tertramethyl-diamin-odiphenyl-methane), and TBH-TMEDA(MN.NW -tera-methylethylenediamine) [15] systems could initiate MMA to polymerize. The kinetic equation of MMA polymerization initiated with CHP-DMT system has been investigated in our laboratory and the rate equation of polymerization is shown as follows ... 

This paper surveys the field of methanation from fundamentals through commercial application. Thermodynamic data are used to predict the effects of temperature, pressure, number of equilibrium reaction stages, and feed composition on methane yield. Mechanisms and proposed kinetic equations are reviewed. These equations cannot prove any one mechanism however, they give insight on relative catalyst activity and rate-controlling steps. Derivation of kinetic equations from the temperature profile in an adiabatic flow system is illustrated. Various catalysts and their preparation are discussed. Nickel seems best nickel catalysts apparently have active sites with AF 3 kcal which accounts for observed poisoning by sulfur and steam. Carbon laydown is thermodynamically possible in a methanator, but it can be avoided kinetically by proper catalyst selection. Proposed commercial methanation systems are reviewed. 

This paper presents a review of the chemistry of the methanation process, the mechanisms of the key reactions, the kinetics of the reactions over various catalysts, and the application of this background to commercial processes. 

Kinetics. Extensive studies of the kinetics of methane synthesis were reported by White and co-workers (10,11, 12, 13, 14, 15). They studied the reaction between CO and hydrogen over a reduced nickel catalyst on kieselguhr at 1 atm and 300°-350°C (10). They correlated the rate of methane formation by the equation ... 

The kinetic expression was derived by Akers and White (10) who assumed that the rate-controlling factor in methane formation was the reaction between the adsorbed reactants to form adsorbed products. However, the observed temperature-dependence of the rate was small, which indicates a low activation energy, and diffusion was probably rate-controlling for the catalyst used. 

It was shown in laboratory studies that methanation activity increases with increasing nickel content of the catalyst but decreases with increasing catalyst particle size. Increasing the steam-to-gas ratio of the feed gas results in increased carbon monoxide shift conversion but does not affect the rate of methanation. Trace impurities in the process gas such as H2S and HCl poison the catalyst. The poisoning mechanism differs because the sulfur remains on the catalyst while the chloride does not. Hydrocarbons at low concentrations do not affect methanation activity significantly, and they reform into methane at higher levels, hydrocarbons inhibit methanation and can result in carbon deposition. A pore diffusion kinetic system was adopted which correlates the laboratory data and defines the rate of reaction. 

This is a report on the basic work done in the laboratory to develop the catalysts for the methanation of synthetic gas from coal, and it also reports on the development of an applicable kinetic system. This report does not include any of the subsequent pilot plant test work. 

As particle size decreases, hydrogen leakage decreases and hot spot temperature in the bed is higher. Thus the smaller particle size has greater activity (see Table VI). A kinetic system which defines the reaction in terms of CO and C02 methanation and CO shift conversion was used to determine the activity (see last column of Table VI). 

For the C02, the literature kinetics gave more reasonable correlation than the simple kinetics though the difference is not great. However, Ref. 15 (16) involves methanation of > 50% C02 in H2 under conditions where Equation 3 would break down, and Ref. 17 (18) involves only the initial hydrogenation (less than the first 1 or 2% ) of the C02 present. Furthermore, there is a possibility that the reverse shift would produce enough CO to poison the C02 methanation in these experiments which would make it difficult to obtain agreement between various runs. 

It is concluded that a fully satisfactory system for calculating simultaneous reactions of CO and COo with H2 and H20 will require a schedule of the effect of CO on C02 methanation as a function of temperature. This effect will probably be different with different particle sizes. From a commercial standpoint, the particle size range may be too small to require much difference in the treatment of the data, but in the laboratory very small particle size may lower the CO methanation rate. A simple kinetics system such as that derived from Equation 3 may be satisfactory for all the reactions. It is unlikely that reliable data will be collected soon for the shift reaction (since it is of a somewhat secondary nature and difficult to study by itself), and therefore a more complicated treatment is not justified. 

For CO methanation, one of the simple literature kinetic systems (2, 3) should be as reliable or better than the one used in this study. With C02 methanation, it is less certain that a simple system is indicated. It is probably of more urgency to elucidate the quantiative effect of CO on C02 methanation than to find a complex kinetic expression for the C02-H2 reaction itself. 

The main disadvantage of this technique is that it relies on very accurate temperature measurement, particularly near the top of the temperature profile, so that the position of the 5°F point can be established and the tangent accurately constructed. Also, the end of the bed is predicted only from kinetic considerations when, in fact, other factors may be more important. In practice, however, although this introduces some scatter into successive measurements—as does variation in the duty required of the methanator—the technique has proved very satisfactory. 

Dr. Woodward May I just make one comment to emphasize and to repeat what was said earlier Thermodynamics and kinetics. Yes, under the inlet conditions of several SNG processes, and also of methanation in ammonia and hydrogen processes, thermodynamically they are inside the carbon-forming region. At the exit they tend not to be. In practice, carbon is not formed. One could, therefore, conclude very simply that kinetics outweighs thermodynamics. 

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