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- A mixture of methane and air is capable of being ignited only if the mole percent of methane is between 5% and 15%. A mixture containing 6.00 mole% methane in air flowing at a rate of 1300.0 kg/h is to be diluted with pure air to reduce the methane concentration to the lower flammability limit. Calculate the required flow rate of air in mol/h and the percent by mass of oxygen in the product gas. (Note: Air may be taken to consist of 21.0 mole% O2 and 79.0 mole% N and hence to have an average molecular weight of 29.0). Required dilution air: 4/1ouy Mass percent O2 in product: i1. A boiler burns fuel oil with the following analysis by mass : 80% C 18% H2 2%S 30% excess air is supplied to the process. Calculate the stoichiometric ratio by mass and the % Carbon Dioxide present in the dry products. (15.62/1 14.9% CO2) 2. A boiler burns coal with the following analysis by mass : 75% C 15% H2 7%S remainder ash Calculate the % Carbon Dioxide present in the dry products if 20% excess air is supplied. (16.5% CO2) 3. Calculate the % of each dry product when coal is burned stoichiometrically in air. The analysis of the coal is: 80% C 10% H2 5% S and 5% ash. (76.7%N, 22.5% CO2 0.8% SO2)A gasification plant of MSW produces syngas of the following Component Composition (dry volume %) CO 30 H2 40 CO2 30 Determine the weight percentage of syngas component. (MW: CO =28; H2 = 2; CO2 = 44) (Hints: It is easier to start with 100 moles syngas and volume ratio is equal to molar ratio)
- A steady-state process to recover crystalline potassium chromate (K,CrOz) from an aqueous solution of this salt is required. Four thousand kilograms per hour of a solution that is one-third K,CrO, by mass is joined by a recycle stream containing 36.4% K2CrO7, and the combined stream is fed into an evaporator. The concentrated stream leaving the evaporator contains 49.4% K,CrO; this stream is fed into a crystallizer in which it is cooled (causing crystals of K,CrO, to come out of solution) and then filtered. The filter cake consists of K,CrO, crystals and a solution that contains 36.4% K,CrO, by mass; the crystals account for 95% of the total mass of the filter cake. The solution that passes through the filter, also 36.4% K,CrO,, is the recycle stream. 1- Draw the flowchart of the system and put all known information. 2- Calculate the rate of evaporation, the rate of production of crystalline K,CrO7, the feed rates that the evaporator and the crystallizer must be designed to handle, and…Methane (CH4) is burned with air (79% N2 and 21% O2 by volume) at atmospheric pressure. The molar analysis of the flue gas yields CO, %3D 10.00%, O2 = 2.41%, C0= 0.52%, and N2 = 87.07%. Balance the combustion %3D equation and determine the mass air-fuel ratio, the of stoichiomet- percentage ric air, and the of excess air. percentageDetermine the volume (L) of hydrogen needed (based on room temperature 25 °C and l atm) to hydrotreat 1 liter crude oil with 1.8 wt % S to a sulfur content of 0.2 wt%. The oil has a specific gravity of 0.8 (compared to water). The stoichiometry follows the following reaction: Oil-S + 2H2¬→O¡I-H2 + H2S
- In a process producing KNO3 salt, 1000 kg/h of a feed solution containing 10 wt% KNO3 is fed to an evaporator, which evaporates some water at 422 K to produce a 50 wt% KNO3 solution. This is then fed to a crystallizer at 311 K, where crystals containing 98 wt% KNO3 are removed. The saturated solution containing 37.5 wt% KNO3 is recycled to the evaporator. Calculate the amount of the recycle stream R in kg/h and the product stream of crystals P in kg/h.3. Given: Soda and lime are added to a glass batch in the form of soda ash (Na,CO,) and limestone (CaCO). During heating, these two ingredients decompose to give off carbon dioxide (CO₂), the resulting products being soda and lime. Find: Compute the weight of soda ash and limestone that must be added to 110 lb of quartz (SiO₂) to yield a glass of composition 72 wt% SiO₂, 16 wt% Na₂O, and 12 wt% Cao. Solution:0 A too kmal/h stream that is 97 msle % Carbon tetrachlorice Ccc4) and 3 % Carbon disullide ccs) is to be recovered Prom the bottom of a distillation column. The feed to the column is 16 mole % CS, and 84 % Cc4, and 2 % of the cc4 enterirg the column is contained in the overhead stream leaving H top of 'the column- O a flow charf of the pocess and do the degree-of- Drae and label freedom analysis- Clculate the mass and mle fracklons of Ccl4 in the overhend stranm, and determine He malar Piow rates of cc4 & CS, in the overhend and feel streams
- Solid calcium (CaF2) reacts with sulfuric acid to form solid calcium sulfate and gaseous hydrogen fluoride. The HF is then dissolved in water to form hydrofluoric acid. A source of calcium fluoride is fluorite ore containing 96 wt% CaF2 and 4% SiO2. In a typical hydrofluoric acid manufacturing process, fluorite ore is reacted with 93 wt% aqueous sulfuric acid, supplied 15% in excess of the stoichiometric amount. Ninety-five percent of the ore dissolves in the acid. Some of the HF formed reacts with the dissolved silica in the reaction 6 HF + SIO2 (aq) – H2SİF6 (9) + 2 H2O (1) The hydrogen fluoride exiting from the reactor is subsequently dissolved in enough water to produce 60 wt% hydrofluoric acid. Calculate the quantity of fluorite ore needed to produce a metric ton of acid. Express your answer into three significant figures.A mixture of methane and air is capable of being ignited only if the mole percent of methane is between 5% and 15%. A mixture containing 9.0 mole% methane in air flowing at a rate of 7:00 x 102 kg/h is to be diluted with pure air to reduce the methane concentration to the lower flammability limit. Calculate the required flow rate of air in mol/h and the percent by mass of oxygen in the product gas. (Note: Air may be taken to consist of 21 mole% O2 and 79% N2 and to have an average molecular weight of 29.0.)1. A wet gas from a field in Iran is processed through two stages of separation; first stage separator operates at 220 psia and 71°F, while the stock tank operates at atmospheric pressure and 69°F. The separator gas condensate ratio is 41,000 scf/STB and the stock tank gas condensate ratio is 450 scf/STB. The molecular weights of the separator gas and stock tank gas are 25.0 and 35.0 lb/lb-mol, respectively. The stock tank condensate gravity is 0.85 and its molecular weight is 125 lb/lb-mol. Let us calculate the specific gravity of the reservoir gas in a step-wise manner, by considering quantities for one STB of condensate. Note that 1.0 bbl is 5.614 ft. Separator gas MWsg = 25 lb/lb-mol 41,000 scf/STB Reservoir gas 1st stage separator 220 psia and 71°F Stock tank gas MWsg = 35 lb/lb-mol 450 scf/STB 2nd stage separator (Stock tank) 14.7 psia and 69°F MW=125 lb/lb-mol SGstc = 0.85 Stock tank condensate a. to one STB. Calculate the mole number [lb-mole] of the stock tank condensate that…