Given: #1a: Use the following reactor product flow rates out of the SRR for the energy balance: CH4: 175kmol/h, H2O: 3156kmol/h, CO: 1205kmol/h, H2: 4493kmol/h, CO2: 219kmol/h. #3: Use a water vapor flow rate of 21 kmol/h out of the third condenser (before the MUG compressor). The overall liquid water removal rate is 56,500 kg/h. Rate of heat transfer into the steam reformer reactor=-418175707kJ/hr. Flow rate of natural gas=5561549.8kmol/hr. Rate of steam generation by cooling down the burner effluent=-42033.85414kg/hr. Rate of steam generation by cooling the SRR reactor effluent=-46578.26174kg/hr. The temperatures of operation (in C) and the rates of heat removal (in kg/hr) for each of the three condensers designed to remove water from the SRR product stream are: T1=145, T2=125, T3=105, Q1=-92928060.13, Q2=-77177541, Q3=-51427023 #4: Use the composition above but after the third condenser (with only 21kmol/h of H2O) as your feed to this problem. #5a: Please use the following composition for the purge stream (total flow rate = 2900 kmol/h): CH4: 6.0%, CO2: 2.8%, CO: 11.2%, H2: 79.9%.

5.) You will be performing calculations to determine the amount of energy savings by energy integration. For these problems, assume you can purchase energy at a rate of $3 per million BTU (approximately the cost of burning natural gas). a.) How much money can be saved (in $MM/year) by combusting the MSR loop purge stream in the SRR by offsetting some of the methane used? Assume that the purge stream enters the burners at a temperature of 35 C, but the air enters as it is written in the process flow diagram (5% excess air at 300 C). b.) What is the financial equivalent to energy produced by methane combustion to that recovered by the production of steam in #2 (in $MM/year) by the cooling down of the SRR products and the combustion effluent? In other words, what is the effective savings of generating steam?