Natural Gas Dehydration Based On Agricultural By Products

Separation and Dehydration is another stage of oil and gas production wells. Gas must be separated from heavier hydrocarbons like oil and natural gas liquids. Dehydrators remove the water from the harvested gas. These processes occur at well sites, compressor stations, gas processing plants, and oil storage sites. Air can be contaminated from high amounts of vented methane and volatile organic compounds from dehydrators and separators. Wastewater storage tanks can leak and contaminate soil. Wastewater storage can leak and contaminate surface and

A solid substance can serve as a stationary phase on which the constituents to be separated can be adsorbed. In practice, gas-solid chromatography (GSC) or adsorption chromatography is important for the analysis of air gases. The use of liquid as stationary phase is preponderant

This project aims to create valuable products from natural gas extracted from shale formations. The shale gas feed entering the process contains mostly hydrocarbons that can be transformed into a variety of value added chemicals, but it also contains impurities that must be removed. Carbon dioxide is useful in the chemical reactions utilized to convert hydrocarbons into hydrogen gas (in order to create ammonia), but at 8 mole percent, the concentration of CO2 in our feed will dilute the shale gas and may cause corrosion. Hydrogen sulfide is not only hazardous to health and corrosive to pipelines, but also destroys metal catalysts used in the processes downstream. These impurities can be removed using a variety of separations techniques. Once removed, however, sulfur should not be considered a waste product. It can be collected and used in ammonium sulfate fertilizer. Depending of the desired quality of gas,

Carbon Dioxide Capture and Storage, which involves capturing, transporting and storing the main greenhouse gas, is a process that could help in the fight against climate change. This paper evaluates gas storage options in detail and discusses the issues and potential of each. The technology proves to have large potential for development in the close future. The most effective carbon capture method is inconclusive as it is dependent on the type of fuel being used and whether it is a pre-existing plant. Of the existing methods of storage, enhanced oil recovery is the most common and economically viable option due to the large volume of CO2 the empty oil reservoirs can secure. The future of what can be done with captured carbon

The inclusion of NOP demonstrated a reduction in methane emissions production and/ or methane yield in beef cattle (Romero-Pérez et al., 2014; Romero-Pérez et al., 2015b), dairy cattle (Haisan et al., 2014; ; Reynolds et al., 2014; Hristov et al., 2015; Haisan et al., 2016; Lopes et al., 2016), and sheep (Martínez-Fernández et al., 2014). When NOP was administered to sheep at 100 mg/ d (approximately 110 mg/ kg of DM) and dosed into the rumen immediately prior to feeding, there was no effect on methane production (g/d), however, there was a 24% reduction in methane yield when expressed as g/kg of DMI (Martínez-Fernández et al., 2014). Additionally, when NOP was supplemented at 2,500 mg/ d (approximately 125-130 mg/ kg of DM), Reynolds et

Recently, Park et al. published an elaborated review on the use of zeolites, mesoporous catalysts and metal oxide catalysts for catalytic vapor cracking. Zeolites, due to their acidity and shape selective catalysis, are reported to be the most effective catalysts for the production of deoxygenated liquid fuel consisting of gasoline range aromatic hydrocarbons. The product composition of the upgraded bio-oils varied with Si/Al ratio and the pore structure of the zeolites. Low organic product yields and rapid deactivation of the catalysts are the drawbacks associated with zeolite catalysis. Recently, Carlson et al. demonstrated that high catalyst to feed ratios and high heating rates attenuate the catalyst deactivation despite improving organic product yields. Poor organic product yields (due to secondary cracking reactions) and the deactivation of HZSM-5 catalysts can be attributed to their high Brönsted acidity.

Based on the calculation data of Concentration-Absorbance plot (Appendix 1), the equation between concentration (mg/ml) and absorbance (AU) is: AU= 1.0057C, R2=0.9924. The concentration change of solutions for continuous 10 min are in Appendix 2. The concentration of solution decreased sharply at first 20 min and then reach the equilibrium after 40 min. According to the adsorption data and equilibrium equation, the beads adsorption abilities can be calculated as following: he saturated adsorptions of beads from Ratio 1 to Ratio 7 are: 24.2020 mg/g, 20.2313 mg/g, 18.0074 mg/g, 15.1917 mg/g, 11.3437 mg/g, 28.0750 mg/g and 20.0573 mg/g. the highest adsorption level of ceramic beads is Ratio 6 (28.0750 mg/g absorption level with the ratio RH: Clay: flour= 5: 4: 0)), the lowest level of beads shows at Ratio 5 (11.3437 mg/g absorption level with the ratio RH: Clay: flour= 1: 8: 1). The saturation level is changed with the change of beads compositions ratios. Figure 3.1 marks the absorption saturation of 7 ratios of beads under the same burning condition.

To develop an appropriate biogas purification technology for small-scale anaerobic digesters various commercially available large-scale purification methods are verified. The pros and cons of each available technology are discussed to utilize it in small biogas plant.

The traditional mass-transfer equipment has been known to have several disadvantages such as flooding, weeping, entrainment, channeling, etc. Further, the above mentioned operational problems were in addition to the technical scale up problems that were faced while the installation of such equipment. The preparation prior to industrial set-up generally required designing, appropriate small scale testing, pilot plant testing and finally industrial scale test, before the system went into operation. Such elaborate preparations required large amount of capital as well as physical space as the separation equipment, is most generally extremely large and occupies huge area. The introduction of membrane separators was a major breakthrough as the membrane separation techniques do away with all such problems. The membrane separators generally have a very high selectivity for a particular component (which is aimed to be separated) in the absorption process, as well as they are compact and modular, which essentially means that the scale-up is not an issue with the membrane separators. Their other advantages include very high surface to volume ratio, which can also be calculated (whereas in columns, such as distillation or packed column, contact surface area is unknown and cannot be estimated), and are flexible in operation as they separate gas liquid flows which can be independently controlled as well as

A S Alosaimy is experimented to Concentration of desiccant solution regenerated by solar energy. Experimental results show that solution with 30% concentration can be regenerated up to 50% using solar energy. It was found that as the regeneration temperature was increased, moisture absorbing capacity of air was increased. As the regeneration temperature was increased, the dehumidification rate in the absorber was increased. The moisture removal rate was increased with the increasing in regeneration. As the inlet temperature of desiccant was increased, the dehumidification was reduced in the absorber, indicated the reduction in moisture removal capacity [2].

A S Alosaimy is experimented to Concentration of desiccant solution regenerated by solar energy. Experimental results show that solution with 30% concentration can be regenerated up to 50% using solar energy. It was found that as the regeneration temperature was increased, moisture absorbing capacity of air was increased. As the regeneration temperature was increased, the dehumidification rate in the absorber was increased. The moisture removal rate was increased with the increasing in regeneration. As the inlet temperature of desiccant was increased, the dehumidification was reduced in the absorber, indicated the reduction in moisture removal capacity.

The PDMS, PTMSP, zeolite and composite membranes have been reported to have separation factors of 4.4–10.8, 9–26, 7–59, 12–106, respectively. However, in some cases, the separation factor gets way higher than expected, such as a separation factor of 218 during the separation of ethanol (98.2% permeate) over water-ethanol solution (20% by weight ethanol), using a silicate zeolite membrane (Nomura et al., 2002). In general, separation factors are ranked in the following order: PDMS < PTMSP < composite membranes < zeolite

There are several methods available for color removal from waters and wastewaters such as membrane separation, aerobic and anaerobic degradation using various microorganisms, chemical oxidation, coagulation and flocculation, and reverse osmosis. Some of these techniques have been shown to be effective however they have some limitations such as excess amount of chemical usage, accumulation of concentrated sludge that has serious disposal problems and lack of effective color reduction. The adsorption technique, which is based on the transfer of pollutants from the solution to the solid phase, is known as one of the efficient and general wastewater treatment method

Using of residues from agro-industrial sources in bio processes has aroused the interest of the scientific community lately. Ecological issues and concerns aimed to reducing pollution have boosted the search for “clean Technologies” to be used in the production of commodities of importance to chemical, energy and food industries. This idea makes use of alternative materials, requires less energy, and minimizes pollutants in industrial effluents, as well as being more economically useful due to its reduced costs (Martins et al., 2011) (1).

Solid sorbents are small porous particles which can selectively adsorb or complex with gaseous chemical species (in this case, CO2), thereby removing the species from a gas mixture. Molecules of CO2 may be held loosely by weak intermolecular forces termed ?physiosorption? or strongly via covalent bonding, termed ?chemisorption.? Generally, physiosorption occurs when the heat of adsorption is greater than approximately -40 kJ/mol of CO2 (i.e. -20 to -40 kJ/mol), while chemisorption occurs with the heats of adsorption less than -60 kJ/mole (Yang, 2003). These are rules of thumb, however, and exceptions do exist. For instance, the heat of physiosorption of CO2 in some zeolites has been reported to be as low as -210 kJ/mol CO2 (Shen, et al., 2000), with heats of chemisorption known to extend from as low as -62 kJ/mol to over -420 kJ/mol. The heat