Methane construction materials

The pyrolytic reforming reactor was a packed bed in a quartz tube reactor. Quartz was selected to reduce the effect of the reactor construction material on the hydrocarbon decomposition rate. ° The reactor was packed with 5.0 0.1 g of AC (Darco KB-B) or CB (BP2000) carbon-based catalyst. The reactor was heated electrically and operated at 850—950 °C, and the reactants had a residence time of 20—50 s, depending on the fuel. The reactor was tested with propane, natural gas, and gasoline as the fuels. Experiments showed that a flow of 80% hydrogen, with the remainder being methane, was produced for over 180 min of continuous operation.The carbon produced was fine particles that could be blown out... 

Rhodium was chosen as construction material for the reactor, which served as active catalyst species at the same time. Rhodium has a high thermal conductivity of 120 W/(m K). Twenty three foils carrying 28 channels each of which was sealed by electron beam and laser welding. The stack of foils formed a honeycomb which was pressure resistant up to 30 bar. The maximum operating temperature of the reactor was 1200°C. The feed was preheated to 300° C and then fed to the reactor. The experiments were carried out between ambient pressure and 25 bar at 0/C ratio 1.0. After ignition of the reaction between 550 and 700°C, 1000°C reaction temperature was then achieved within 1 min, and mainly carbon monoxide and hydrogen were formed. Only 62% conversion of methane but 98% conversion of oxygen was achieved at 1190°C. The performance of the reactor deteriorated when the system pressure was increased. By-product and even soot formation then occurred downstream the reactor. 

A S5mgas of H2/CO=3 at 30 bar would result in an adiabatic temperature increase to 923°C with an inlet temperature of 300 C [219]. However, the high temperatures will require expensive construction materials for reactors and heat exchangers followed by a series of reactors for final methanation. Moreover, at typical conditions, there is thermodynamic potential for carbon formation at high temperatures. 

Find et al. developed a nickel-based catalyst for methane steam reforming in microchannels [218]. AluchromY steel, which is a Fecralloy (see Section 10.2.1), was used as the construction material for the microstructured plates. The catalyst was based upon a nickel spinel support (NiAl204) for stabilisation. The active nickel... 

In the mid 1970s, Ugi and co-workers developed a scheme based on treating reactions by means of matrices - reaction (R-) matrices [16, 17]. The representation of chemical structures by bond and electron (BE-) matrices was presented in Section 2.4. BE-matrices can be constructed not only for single molecules but also for ensembles of them, such as the starting materials of a reaction, e.g., formaldehyde (methanal) and hydrocyanic add as shown with the B E-matrix, B, in Figure 3-12. Figure 3-12 also shows the BE-matrix, E, of the reaction product, the cyanohydrin of formaldehyde. 

Considerable challenges still remain in the development of new carbonylation processes for acetic acid manufacture. For example, all of the current processes use iodide compounds, leading to corrosive HI and the need for expensive materials for plant construction. An iodide-free system could potentially impart considerable benefit. Other long term goals include the selective direct conversion of syn-gas or oxidative carbonylation of methane to acetic acid. Organometallic chemists are certain to play a crucial role if these targets are to be achieved. 

Carbon tetrachloride represents an example of the change to petroleum raw materials in this field. The traditional source of this widely used product has been the chlorination of carbon disulfide, either directly or through the use of sulfur dichloride. Military requirements in World War II caused an increase in demand, and in addition to expansion of the older operations, a new process (28) was introduced in 1943 it involved direct chlorination of methane at 400° to 500° C. and essentially atmospheric pressure. This apparently straight-forward substitution of halogen for hydrogen in the simplest paraffin hydrocarbon was still a difficult technical accomplishment, requiring special reactor construction to avoid explosive conditions. There is also the fact that disposal of by-product hydrochloric acid is necessary here, though this does not enter the carbon disulfide picture. That these problems have been settled successfully is indicated by the report (82) that the chlorination of methane is the predominant process in use in the United States today, and it is estimated that more than 100,000,000 pounds of carbon tetrachloride were so produced last year. 

The materials of construction of the radiant coil are highly heat-resistant steel alloys, such as Sicromal containing 25% Cr, 20% Ni, and 2% Si. Triethyl phosphate [78-40-0] catalyst is injected into the acetic acid vapor. Ammonia [7664-41-7] is added to the gas mixture leaving the furnace to neutralize the catalyst and thus prevent ketene and water from recombining. The crude ketene obtained from this process contains water, acetic acid, acetic anhydride, and 7 vol % other gases (mainly carbon monoxide [630-08-0], carbon dioxide [124-38-9], ethylene [74-85-1], and methane [74-82-8]). The gas mixture is chilled to less than 100°C to remove water, unconverted acetic acid, and the acetic anhydride formed as a liquid phase (52,53). 

The quite loud explosions (either immediate or delayed) which occur when LNG (containing usually high proportions of heavier materials) is spilled onto water are non-combustive and harmless [1]. Superheating and shock-wave phenomena are involved [2]. There is a similar effect when LNG of normal composition (90% methane) is spilled on to some CsCg hydrocarbons or methanol, acetone or 2-buta-none [3]. A US National Fire Code covers site selection, design, construction and fire prevention aspects of LNG installations [4]. 

The reaction takes place under fuel-rich conditions to maintain a nonflammable feed mixture. Typical feed composition is 13% to 15% ammonia, 11% to 13% methane and 72% to 76% air on a volumetric basis. Control of feed composition is essential to guard against deflagrations as well as to maximize the yield. The yield from methane is approximately 60% of theoretical. Conversion, yields, and productivity of the HCN synthesis are influenced by the extent of feed gas preheat, purity of the feeds, reactor geometry, feed gas composition, contact time, catalyst composition and purity, converter gas pressure, quench time and materials of construction. 

As can be seen from the above equation, formation of HCN is in reality a hetero-bimolecular oxidative coupling reaction of methane with ammonia. The ammoxidation reactor construction is a simple fixed-bed multi-tube and the catalyst is usually a platinum or sometimes a Group V or VI metal oxide on a silica or alumina support. The HCN product is recovered by condensation and fractionation. With the reaction simplicity and yield, and widespread availability of starting materials, in-situ HCN generation is an ideal industry solution to HCN supply. (See Chapter 29 for more details.)... 

After separation of the catalyst by filtration, raw succinic anhydride is purified by distillation under reduced pressure, ie, 4—13 kPa (30—98 mm Hg), and flaked. The material of construction of the plant is stainless steel. Typical specific consumptions for the production of one metric ton of succinic anhydride are maleic anhydride at 10501 hydrogen, 300 m steam, 45001 cooling water, 100 electricity, 350 kW nitrogen, 100 m and methane,... 

Besides being a key starting material for the preparation of polyorthocarbonates, dichlorodiphenoxy methane is a versatile synthon for the construction of heterocyclic systems of medicinal interest (Ref. 36). Its condensation with cyanamide affords diphenyl cyanocarbonimidate in high yield (Ref. 35) as shown in scheme 38 ... 

The introduction of the catalyst presents one of the main problems in using MSRs for heterogeneously catalyzed reactions. There are some examples of reactors that are constructed directly from the catalytically active material. Kestenbaum et al. [145] used silver foils for the construction of a microchannel reactor for the partial oxidation of ethene to oxirane. A similar concept was proposed by Fichtner et al. [91,146], These authors used a microstructured rhodium catalyst for the partial oxidation of methane to syngas. This reaction can be considered as a coupling of the exothermic oxidation and the endothermic reforming of methane, which occur at different reaction rates. In such a case, the formation of a pronounced axial temperature profile can be avoided through the use of a material with high thermal conductivity. The reactor... 

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