Inlet temperature cell reactor

The view-cell reactor is made of titanium and has two sapphire windows, a gas inlet valve and an outlet valve, as shown in Figure 3. The view cell is interfaced with a pressure transducer, a thermocouple, and a pressure relief valve. The pressure and temperature are computer-monitored during the reaction. 0.6 ml of 50 wt% H2O2/H2O (10.41 mmoles), 0.20ml of pyridine (2.47 mmoles), or some other base, was dissolved in 5 ml of acetonitrile or methanol, and was added to the reactor. 2.2 ml of supercritical CO2 was charged after lOOmg of propylene (2.38 mmoles) had been added to the reactor. The reactor was heated with a band heater at 40 - 70°C for 3, 6, 12, and 24 hr reaction periods. Following a batch conversion experiment, the amounts of products formed were determined by GC and GC/MS. 

Autothermal reforming reactor (ATR) is maintained under adiabatic conditions. There is no heat transfer from or to the reactor section during the reaction. The effect of S/C and O/C ratios on the net electric efficiency of the system with fuel cell has been calculated. The results are illustrated for different inlet temperatures (700° and 400°C) in Figures 7 and 8. A decrease of the S/C ratio decreases the efficiency. On the other hand, an... 

The solution as mobile phase (imidazole lOOmmol/L in the Tricine buffer 50 mmol/L, pH 9.4) was flowed at 0.1 mL/min using HPLC pump to the flow cell reactor via inlet connecting tube, and drained via a outlet tube. H2O2 specimen (20 juL) was injected with a loop injector (7125, JASCO). The reaction temperature for CL was room temperature. Light from the flow-through chip was detected after the dark frame reduction with the CCD-CL monitor. 

An example of an experiment with a 2 factorial design is the analysis of the CO concentration after a water gas shift (WGS) reactor in a fuel cell system operating with reformate. In the example, the factors were selected as the inlet temperature of the shift reactor and the flow rate of quench water fed between the high- and low-temperature shift stages. The response of these values to the CO concentration as the target parameter was analyzed. In order to simplify the discussion, the values at the lower and upper levels were standardized as —1 and +1, respectively. The response functions were derived using the standardized values for each factor. 

Springmarm et ol. [152] simulated a 10-kWei autothermal reformer for gasoline with a one-dimensional, dynamic model. The reformer was a metallic monolith coated with precious metal catalyst. The reformer consisted of two parts both of 70-mm diameter, a small electrically heated monolith only 5-mm long (400 cells per square inch or about 1300-pm channel size) and a second, about 100-mm long monolith (1600 cells per square inch or about 630-pm channel size). Both monoliths were coated with the same catalyst Kinetic data were determined prior to the simulations [56] and heat losses were estimated for the reactors, which is a critical issue. The reformer was operated at a S/C ratio of 2 and an O/C ratio of 0.75. The pressure was 4bar and the feed inlet temperature 500 °C. 

Fig. 21.3 Oil heated methanol refrarnCT for 5 kW HTPEM fuel cell system. Temperature in the reactor center plane. Oil inlet temperature 533 K. Methanol water mixture inlet temperature 473 K...

Reactors used in the lab-scale facility shown in Figure 1 were glass made and had several sizes to place the different monoliths. Commercial 15x15 x 30 cm monoliths were cut to smaller ones, of around 2.0 x 2.0 x 20 cm. Number of cells used in these "small monoliths were 3 x 3, 4 x 4 or 5 x 5, depending on cell density. To avoid bypass in the catalytic reactor, the free space between the monolith and the reactor wall was always carefully filled with carburundum (SiC). For some tests, monoliths were crushed, sieved to several sizes below 1 mm, and then used as particles. Temperature was measured with two thermocouples located just at the inlet and exit of the monolith. Tenqjcrature differences between these two points were < 2 C. Gas san ting and analysis methods in this small facility were already reported [6,7]. 

All activity measurements were conducted in an in-situ infrared reactor cell placed in the sample compartment of a DIGILAB 15C Fourier Transform Infrared (FTIR) Spectrometer. The reactor, described in detail elsewhere [11], consisted of two aluminum flanges with CaF2 IR transparent windows, a gas inlet and outlet, and two foil fast response thermocouples which were placed in direct contat with the catalyst. The reactor temperature was maintained constant by external heaters controlled by a temperature programmed controller. A Teflon coated recycle pump permitted to maintain near isothermal conditions and improve the mixing in the reactor. The reactor and associated lines were tested for activity at the highest temperature used, and it was found to have negligible activity. 

As shown in Figure 4.C.2, Aspen HYSYS simulation file is opened first. In VBA, Dim statement is used for declaration of variables, whereas Set statement is used for creating new objects. Then, values of feed flow rate, length and diameter of each reactor, and temperatures of inlet streams of both separators are transferred from cells C3 to Cll in Excel worksheet named DV to Aspen HYSYS , to Aspen HYSYS. To reduce computational time, remember to deactivate HYSYS solver before this transfer, and then activate it after transferring values of all decision variables to proceed with the calculations... 

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