Flow rate of butane

Catalytic Reactions. Catalytic oxidation of butane was carried out in a flow reactor at 713 K after the catalysts were pretreated in an N2 flow at 773 K for 2 h. The feed gas consisted of 1.5% butane, 17% O2, and N2 (balance) (7). The products were analyzed with an on-line gas chromatograph. W/F (W = catalyst weight/g, F = flow rate of butane/ mol-h l) was changed in the range of 1.1 x 10 - 11 x 10 mol g-h by controlling the total flow rate. 

Catalytic Oxidation of Butane. The dependences of the conversion of butane on W/F for (VO)2P207 and Si02/(V0)2P207 are given in Figure 5, where W is the catalyst weight and F is the flow rate of butane. The conversion increased with the increase in W/F. The catalytic activity and the selectivity of oxidation of butane are summarized in Table 2. 

Active crystal face of vanadyl pyrophosphate for selective n-butane oxidation catalyst preparation, 157-158 catalyst weight vs. butane oxidation, 162,163/ catalytic activity, 162,1 (At catalytic reaction procedure, 158 experimental description, 157 flow rate of butane vs. butane oxidation, 162,163/ fractured SiOj-CVO PjO scanning electron micrographs, 160,161/ fractured scanning electron... 

Flow rate of butane in the liquid product from stage 3, /.3X32 = 25 kmol/h... 

Example 6.4. An orifice meter is installed in a 4 in. Sch40 pipeline to measure the mass flow rate of butane up to 10000 kg h . Consider that butane is an incompressible fluid with a density of 600 kg m and a viscosity of 0.230 cP. The orifice diameter is exactly half of the pipe diameter ... 

Figure 9. H2 ( ) / n-butane ( ) separaticm with the ccxnposite zeolite-alumina membrane (fluxes in the permeate as a function of the tenq>erature). A mixture of hydrogen, n-btitane and nitrogen (12 14 74) was fed in the tube (Fig. 2) with a flow rate of 4.8 1/h. Sweep gas (N2), countercurrent mode, flow rate 4.3 1/h.

As the butane liquid level in the condenser increased, the area of the exchanger exposed to the condensing vapors would decrease. Let s assume that the tower s reboiler duty was constant. The vapor flow rate to the condenser would then be constant. To condense the same flow rate of vapor, with a shrinking exchanger surface area, the pressure of condensation must increase. The tower pressure would also go up, as the condenser pressure rose. 

Fig. 3 Chromatogram of a red wine using Shodex S-801/S and S-802/S columns at 75°C with a mobile phase of water at a flow-rate of 1 ml/min and using a refraction index detector. Peaks A = compounds with the highest molecular mass and with an acid character 1 = glucose 2 = fructose 3 = glycerol 4 = butan-2,3-diol (= 0.8 g/L added to the initial wine) 5 = ethanol. (Reprinted from Ref. 30 with the kind permission of Elsevier Science—NL, Sara Burgerhartstraat 25, 1055 KV Amsterdam, The Netherlands.)...

The dehydrogenation of iso-butane was carried out in a recirculating batch reactor.12 Reaction products were analyzed by gas chromatography using flame ionization. The vanadium and vanadium carbide powder materials were purchased from Aldrich Chemical Co. Their bulk compositions were confirmed by the X-ray diffraction measurements. Prior to the dehydrogenation reactions, these powder materials were heated for 1 h at 900 K in pure H2 at a flow rate of 200 cm3 per minute. 

We consider a distillation column for the separation of a mixture containing 80% (molar) normal-butane (n-butane) and 20% iso-butane, fed at a flow rate of 360... 

Three different zeolites (USY-zeolite, H-ZSM-5 and H-mordenite) were investigated in a computer controlled experimental equipment under supercritical conditions using the disproportionation of ethylbenzene as test reaction and butane or pentane as an inert gas. Experiments were carried out at a pressure of 50 bar, a flow rate of 450 ml/min (at standard temperature and pressure), a range of temperatures (573 - 673 K) and 0.8 as molar fraction of ethylbenzene (EB) in the feed. The results showed that an extraction of coke deposited on the catalysts strongly depends on the physico-chemical properties of the catalysts. Coke deposited on Lewis centres can be more easily dissolved by supercritical fluid than that on Brnsted centres. 

Example 4.1 Lost work in throttling processes w-Butane gas with a flow rate of 25 mol/s is throttled from 15 bar and 450 K to 1 bar in a steady-state flow process. Determine the final temperature and the lost work. Assume that the surroundings are at 298.15 K. 

Butane (C4H10) at 360°C and 3.00 atm absolute flows into a reactor at a rate of 1100 kg/h. Calculate the volumetric flow rate of this stream using conversion from standard conditions. 

The flow of air to a gas-fired boiler furnace is regulated by a minicomputer controller. The fuel gases used in the furnace are mixtures of methane (A), ethane (B), propane (C), n-butane (D), and isobutane (E). At periodic intervals the temperature, pressure, and volumetric flow rate of the fuel gas are measured, and voltage signals proportional to the values of these variables are transmitted to the computer. Whenever a new feed gas is used, a sample of the gas is analyzed and the mole fractions of each of the five components are determined and read into the computer. The desired percent excess air is then specified, and the computer calculates the required volumetric flow rate of air and transmits the appropriate signal to a flow control valve in the air line. 

Plot conversion (up to 90%) and reaction rate as a function of catalyst weight for an entering molar flow rate of pure butan-2-01 of 10 mol/min and an entering pressure Pq = lOatm.VP jx = 23 kg. 

The in sim characterization of catalysts was earned out in an apparatus which included a quadiupole mass-spectrometer and a gas chromatograph for TPO and H2 chemisorption measurements. In situ coking was performed by injecting a mixture of He and n-hexane vapor over the reduced catalysts at 500 C, In TPO experiments, ihe coked sample was heated at a rate of 8 C/min in a stream of 2 voL% O2 + 98% He. The amount of CO2 produced was recorded. The chemisorption of H2 was carried out in the same appanitus by a flow method after reduction or caking. The flow rate of carrier gas (Ar) was maintained at 25 ml/min and the volume of H2 injected was 0.062 ml/pulse. Since the partial piessiire of H2 was very low in this system, the hydrogenation of coke was never observed. Isobaric H2 chemisorption measurements with fresh catalysts were carried out in a static adsorption apparatus. Dehydrogenation of n-butane was carried out in a flow micro-rcactor in H2 atmosphere at LHSV = 3 h-l and H2/HC=1. Reaction products were... 

The flow rate is 5804 kg mol/day. If the overhead and bottoms streams from the butane splitter have the following compositions, what are the flow rates of the overhead and bottoms streams in kg mol/day ... 

Three thousand cubic meters per day of a gas mixture containing methane and n-butane at 21 C enters an absorber tower. The partial pressures at these conditions are 103 kPa for methane and 586 kPa for -butane. In the absorber, 80% of the butane is removed and the remaining gas leaves the tower at 38°C and a total pressure of 550 kPa. What is the volumetric flow rate of gas at the exit How many moles per day of butane are removed from the gas in this process Assume ideal behavior. 

The flow rate of the overhead or bottoms product determines roughly which components go mostly in the overhead and which ones in the bottoms. This also defines the key components where the separation takes place. In this example, an overhead rate of 50 kmol/h would include most of the methane, ethane, propane, isobutane, and n-butane. The bottoms product would include most of the hexane, n-pentane, and isopentane. The n-butane is, therefore, considered the light key component and the isopentane, the heavy key component. The product compositions at a reflux ratio of 1.0 are given in Table 7.3. 

An intermediate product such as the upper side draw, which is mostly propane, may contain impurities from components both lighter and heavier than the main component. The upper side draw is at the same time the bottom product of the top column section and the top product of the second section. The fractionation in the upper section determines to what extent ethane is stripped off from the propane product, and the fractionation in the second section determines to what extent butane is removed from the propane product. Again, in this situation since the number of stages in each section and the reflux ratio are all fixed, the fractionation is fixed. The propane recovery and purity depend mostly on its flow rate and on the flow rates of the adjacent products above and below it. If the propane product contains too much ethane, its flow rate should be cut back and the overhead rate increased. If the propane product contains too much butane, its flow rate should be cut back and the lower side draw rate increased. Table 9.14 summarizes the purities of components in different products at different flow rates. The recoveries can also be calculated from Table 9.14. The dependence of the other products compositions on their rates may be analyzed in a similar manner. 

In the above equations, flow rates of solvent (n-butane), initiator Ii (tert-butyl peroxypivalate) and initiator h (rm-butyl 3,5,5 trimethyl-peroxyhexaonate) are represented by Fs, Fi,i and Fi,2 respectively. 

The catalytic oxidation of benzene (0.5 % in air) and n-butane (1.5 % in air) was carried out in flow reactor operated at atmospheric pressure. The tests were done on a constant catalyst volume basis (2 cm ) in a quartz reactor of internal diameter 1.0 cm. The reactions were performed in the temperature range of 300-550 C at the flow rate of 50-200 cmVmin. The analysis of the substrates and products was performed by gas chromatography. 

One example of extractive distillation is the use of furfural to permit the separation of butadiene from a mixture containing butane and butenes. Furfural, which is a highly polar solvent, lowers the activity of butadiene more than it does for butenes or butane, and the butadiene is concentrated in the furfural-rich stream from the bottom of the column. Butadiene is distilled from the furfural, which is returned to the top of the extractive distillation column. This column would operate with a reflux containing butane and butenes, but the total liquid rate in the top section of the column would be the reflux rate plus the flow rate of furfural. 

Magnitude of Response vs. That for HC Oxidation and Stoichiometry. The response of the NO-NH3 interaction in the presence of excess oxygen and that of the highly reactive 1-butene oxidation were compared at 390°C at flow rates of 1.0 and 2.3 ft3/hr. On a C vs. N basis, the C/N relative response was 1.27 at 1.0 ft3/hr and 0.90 at 2.2 ft3/hr. Response for HC s less reactive than butenes (e.g. butanes) was much less. The interaction of NO and NH3 in the presence of oxygen apparently releases about the same heat and is more rapid than 1-butene oxidation. Reactions 6 and 7 both qualify in heat effect and ratio of NH3/NO utilized. It seems probable that both reactions are involved. For our purposes, it was not necessary to make the distinction. 

The aldol condensation reaction of n-butanal was carried out over 3 ml of the 4 wt% Na/Si02 at 7 barg, 350 C, a n-butanal liquid feed of 0.05 ml min and a H2 flow rate of 42 ml min. This reaction achieved considerably higher conversions than the reaction of butanone over the same catalyst and a high selectivity to a single product (Table 4). 

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