Production mass water calculations

When the electric current was 1.1 mA, i.e., 10.2 pmolThr of oxygen flux, the formation rates of acrylaldehyde, carbon monoxide and carbon dioxide were 0.33, 1.9 and 4.53 (xmol/hr, respectively, and the oxygen consumption rate of 9.02 pmol/hr was calculated by assuming water as another oxidation product. Mass balance calculated between oxygen evolution and consumption of propene oxidation was about 90%. 

On the basis of mass balance calculations through the first 3 years of acid additions (17), only 33% of the added acid resulted in a decrease in lake alkalinity. A second 33% was neutralized by in-lake (IAG) processes, of which sulfate reduction accounted for slightly more than half and cation production for slightly less than half. Approximately 33% of the total sulfate load (wet and dry deposition, and acid additions) was lost via outflow. Therefore, about half of the added acid remained in the water column two thirds of it was unreacted and one third was neutralized by base cations. 

Mass-balance calculations for the first 3 years of acid additions indicate that the principal IAG processes are sulfate reduction and cation production. Specifically, one-third of the total sulfate input (added acid and deposition) was neutralized by in-lake processes. Increased sulfate reduction consumed slightly more than one-sixth and production of cations neutralized somewhat less than one-sixth of the acid added. Of the remaining sulfate, one-third was lost by outflow, and one-third decreased lake alkalinity. Laboratory determinations suggest that sediment-exchange processes occurring in only the top 2 cm of surficial sediments can account for the observed increase in water-column cations. Acidification of the near-surface sediments (with partial loss of exchangeable cations) will slow recovery because of the need to exchange the sediment-bound H+ and neutralize it by other processes. Reactor-based models that include the primary IAG processes predict that... 

Practice Problem 10.7 The industrial process for the production of sodium metal and chlorine gas involves electrolysis of molten (melted) sodium chloride (in the absence of water). Calculate the mass of sodium that can be prepared by electrolysis of 207 kg of sodium chloride. The balanced equation is... 

An aqueous solution of sodium hydroxide contains 20.0% NaOH by mass. It is desired to produce an 8.0% NaOH solution by diluting a stream of the 20% solution with a stream of pure water. Calculate the ratios (liters H20/kg feed solution) and (kg product solution/kg feed solution). 

Mass-balance studies are widely considered to be the most reliable means of making quanta-tive determinations of elemental transfer rates in natural systems. Garrels (1967) and Garrels and Mackenzie (1967) pioneered the use of mass-balance calculations for mineral weathering in their classic study of Sierra Nevada springwaters. These waters were chosen because a careful set of water analyses and associated primary igneous rock minerals and the soil mineral alteration products were known. Since the actual compositions of the minerals were not known, Garrels and Mackenzie used the theoretical formulas for the minerals. 

We can now calculate the surface acidity equilibrium constants (equations 20 and 21). There are five species, =FeOH, =FeOH, =FeO", H , OH", that are interrelated by the two acidity mass law constants (equations 20 and 21), by the ion product of water Kw = [H l [OH"]) and two mass balance equations ... 

Thus, the following links of nitrogen biogeochemical cycle were accounted for mass balance calculations in Northern-East Asia and the whole East Asian domain input — deposition, fertilizers, biological N fixation, import of food and products, riverine fluxes and output — crop uptake, denitrification, volatilization, runoff, sedimentation and sea water exchange. All calculations were condncted for 1994-1997 and the mean values were used. 

The estimated product mass balances for these two runs are shown in Table I. These values assume 10% coke formation, which was determined in other experiments by weight gain of the catalyst. The 3-26-87 data are quite close to the calculated values, but the 4-2-87 data are significantly high in oxygen, which can be explained by the high water value for that day. 

Three different methods were used to quantify the RF energy dissipated in the product thermal energy balance based on the product mass and temperature measurements electrical losses in the matching device (insertion losses) and inductance losses calculated from the flow rate and temperature rise of the cooling water. 

Generally the moderation in powder area is limited. For each unit, one makes a choice of the criticality control mode (1) mass in process equipment (interlinks and administrative measures) or (2) shape and size in storage areas (hardware). The double contingency principle will be applied. Calculations will be done using fixed conservative values for densities of products, a water reflector, and as acceptance criteria a K-eff. below 0.95 or the safety factors given in Table 4. 

Select a basis for the calculation—the basis is an amount or flowrate of a particular stream or component in a stream. Other quantities are determined in terms of the basis. E.g. in Example 7.1 the flowrates of product and water were obtained on a basis of 10kgs of feed. It is usually most convenient to choose an amount of feed to the process as a basis. Molar units are preferable if chemical reactions occur, otherwise the units in the problem statement (mass or molar) are probably best. 

D19. We wish to use n-hexane as an entrainer to separate a feed that is 80.0 wt % ethanol and 20 wt % water into ethanol and water. The system shown in Figure 8-18 will be used. The feed is 10,000.0 kg/h and is a saturated liquid. The ethanol product is 99.999 wt % ethanol, 0.001 wt % hexane, and a trace of water. The water product is 99.998% water, 0.002 wt % ethanol and a trace of hexane. Do external mass balances and calculate the flow rates of make-up solvent (n-hexane), ethanol product, and water product. (Assume that trace = 0.)... 

Table 5.15 Comparison of product mass flow rates, reformer efficiency T r, fuel processor efRciency T fp and auxiliary power unit efRciency T apu of steam reforming values are determined for various, feed inlet temperatures Tjn and S/C (SCR) and O/C ratios (expressed as O2/C ratio OCR) as calculated by Specchia etal. [371]. is the fraction of the fuel which is fed to the steam reformer 1- Pr is fed to the burner yp is the dry hydrogen molar fraction of the reformate Wq shows the water balance of the systems, which is positive when the Wq exceeds unity. 

When we know the balanced chemical equation for a reaction, we can determine the mole and mass relationships between the reactants and products. Then we use molar masses to calculate the quantities of substances used or produced in a particular reaction. We do much the same thing at home when we use a recipe to make a cake or add the right quantity of water to make soup. In the manufacturing of chemical compounds, side reactions decrease the percent of product obtained. From the actual amount of product, we can determine the percent yield for a reaction. Knowing how to determine the quantitative results of a chemical reaction is essential to chemists, engineers, pharmacists, respiratory therapists, and other scientists and health professionals. 

The combustion of the alkane CH4 with oxygen produces carbon dioxide and water. Calculate the total mass of reactants and products for the following equation when... 

Before energy balance is calculated, we need to make mass balance. Figure 9.1 shows the material balance for ethanol and glycerol fermentation. Put simply, mass into the system is equal to mass out of die system. The mass of carbon dioxide is calculated by adding mass of dry cell, mass of glycerol, mass of edianol and mass of water at product stream and then subtracting die sum from die feed stream. As a result, die mass of carbon dioxide is defined. The heat of the reaction is calculated by the following equation ... 

Water is to be cooled in a small packed column from 330 to 285 K by means of air flowing countercurrently. The rate of flow of liquid is 1400 cm3/m2 s and the flow rate of the air, which enters at a temperature of 295 K and a humidity of 60%, is 3.0 m3/m2 s. Calculate the required height of tower if the whole of the resistance to heat and mass transfer may be considered as being in the gas phase and the product of the mass transfer coefficient and the transfer surface per unit volume of column is 2 s-1. 

---