In the pursuit of sustainable sources of energy that do less harm to the environment, numerous technologies have been developed to reduce carbon emissions in the atmosphere. The implementation of carbon capture and storage systems (CCS) has played a crucial role in reducing CO2 emissions, but depleting storage reserves and ever-increasing costs of sequestrating captured CO2 has prompted the idea of utilizing CO2 as soon as it is produced (i.e. carbon capture and utilization, or CCU) and storing any remaining amounts. This project analyzes the cost of implementing a delafossite CuFeO2 backed CCU system for the average US coal-burning power plant with respect to current amounts of CO2 captured. Beyond comparing annual maintenance costs of CCU and CCS systems, the project extends previous work done on direct CO2 conversion to liquid hydrocarbons by providing a protocol for determining how the presence of NO affects the products formed during pure CO2 hydrogenation. Overall, the goal is to gauge the applicability of CCU systems to power plants with a sub 10-year lifespan left, whilst observing the potential revenue that can be potentially generated from CCU implementation. Under current energy costs ($0.12 per kWh), a delafossite CuFeO2 supported CCU system would generate over $729 thousand in profit for an average sized supercritical pulverized coal power (SCPC) plants selling diesel fuel created from CO2 hydrogenation. This amount far exceeds the cost of storing captured CO2 and suggests that CCU systems can be profitable for SCPC power plants that intend to burn coal until 2025.

TiO2 has been studied in the degradation of ethanol for indoor application. A dynamic flowing non-loop system was utilized. The reactor was a quartz tube filled with the TiO2 catalyst with glass wool on the ends. The analytical equipment used were Vernier's ethanol and CO2 sensors with a two-point calibration performed on the ethanol sensor. The purpose of the calibration was to create a known standard to establish accurate readings. The experimental procedure followed the scheme of bypassing the reactor, flowing into the reactor without the UV lights on for a small period, turning the UV lights on for five minutes, and then going back to the bypass. A CFD simulation using ANSYS Fluent was done to determine the optimal inlet and outlet positions of the biochamber that housed the sensors. The objective of the simulation was to determine which inlet and outlet locations provided the best fluid flow for sensor contact and mixing. Sensitivity analysis of varying parameters were tested to determine the optimal settings in producing accurate results to fulfill the simulation goals. It was determined that a vertical position biochamber with an inlet centered on the top face and the outlet on the bottom of a side face was ideal. The main experimental results showed that ethanol of both low and high concentrations were completely or almost fully degraded into carbon-products. The results showed that there was CO2 consumption and it was most likely due to a combination of sensor inaccuracy and accumulation onto the catalyst surface. However, the sensor inaccuracy would not account for the entirely of the CO2 consumption and previous studies have shown that carbon-products do form on the catalyst surface. Therefore, it can be asserted that CO2 has accumulated on the catalyst and the inclusion of water may have caused catalyst deactivation. Having the light on the photoreactor the whole time rather than waiting to turn on the light has shown to decrease the period of degradation but has no effect on the amount of degradation. Research from Nimlos, Muggli, etc., have determined that intermediate products such as acetaldehyde, acetic acid, formaldehyde, and formic acid form during ethanol degradation and this can be assumed to have occurred in this research as well. These intermediate products were not analyzed for this study, but has been included in the go-forward for future works. For indoor applications, TiO2 catalyst have already been implemented into consumer and commercialized air purifiers, but there is tremendous potential for HVAC systems. There are concerns with HVAC application as discussed, but if implemented correctly, it can be a useful tool for indoor air purification.

Due to depletion of oil resources, increasing fuel prices and environmental issues associated with burning of fossil fuels, extensive research has been performed in biofuel production and dramatic progress has been made. But still problems exist in economically production of biofuels. One major problem is recovery of biofuels from fermentation broth with the relatively low product titer achieved. A lot of in situ product recovery techniques including liquid-liquid extraction, membrane extraction, pervaporation, gas stripping and adsorption have been developed and adsorption is shown to be the most promising one compared to other methods. Yet adsorption is not perfect due to defect in adsorbents and operation method used. So laurate adsorption using polymer resins was first investigated by doing adsorption isotherm, kinetic, breakthrough curve experiment and column adsorption of laurate from culture. The results indicate that polymer resins have good capacity for laurate with the highest capacity of 430 g/kg achieved by IRA-402 and can successfully recover laurate from culture without causing problem to Synechocystis sp.. Another research of this paper focused on a novel adsorbent: magnetic particles by doing adsorption equilibrium, kinetic and toxicity experiment. Preliminary results showed excellent performance on both adsorption capacity and kinetics. But further experiment revealed that magnetic particles were toxicity and inhibited growth of all kinds of cell tested severely, toxicity probably comes from Co (III) in magnetic particles. This problem might be solved by either using biocompatible coatings or immobilization of cells, which needs more investigation.

In this work, the vapor transport and aerobic bio-attenuation of compounds from a multi-component petroleum vapor mixture were studied for six idealized lithologies in 1.8-m tall laboratory soil columns. Columns representing different geological settings were prepared using 20-40 mesh sand (medium-grained) and 16-minus mesh crushed granite (fine-grained). The contaminant vapor source was a liquid composed of twelve petroleum hydrocarbons common in weathered gasoline. It was placed in a chamber at the bottom of each column and the vapors diffused upward through the soil to the top where they were swept away with humidified gas. The experiment was conducted in three phases: i) nitrogen sweep gas; ii) air sweep gas; iii) vapor source concentrations decreased by ten times from the original concentrations and under air sweep gas. Oxygen, carbon dioxide and hydrocarbon concentrations were monitored over time. The data allowed determination of times to reach steady conditions, effluent mass emissions and concentration profiles. Times to reach near-steady conditions were consistent with theory and chemical-specific properties. First-order degradation rates were highest for straight-chain alkanes and aromatic hydrocarbons. Normalized effluent mass emissions were lower for lower source concentration and aerobic conditions. At the end of the study, soil core samples were taken every 6 in. Soil moisture content analyses showed that water had redistributed in the soil during the experiment. The soil at the bottom of the columns generally had higher moisture contents than initial values, and soil at the top had lower moisture contents. Profiles of the number of colony forming units of hydrocarbon-utilizing bacteria/g-soil indicated that the highest concentrations of degraders were located at the vertical intervals where maximum degradation activity was suggested by CO2 profiles. Finally, the near-steady conditions of each phase of the study were simulated using a three-dimensional transient numerical model. The model was fit to the Phase I data by adjusting soil properties, and then fit to Phase III data to obtain compound-specific first-order biodegradation rate constants ranging from 0.0 to 5.7x103 d-1.