Mathematics subject Essay Example for Free

Mathematics subject Essay Write a simple sentence and then write the negation. Imagine situations where each statement is true or false. How does the truth value (true or false) of the negation statement compare with the truth value of the original statement? Simple sentence: Mathematics is an easy subject. Negation: Mathematics is not an easy subject. There are many situations in one’s life that is true or false. A proposition is a statement that is declarative in form and is either true or false. The truth value of a statement is unclear in real life due to some conditions and the reasoning of each and every people. Another is that the truth value of a statement may also depend on time and space. An example would be the statement â€Å"It is raining very hard. † The truth value of the statement is either true or false depending on the time and the location of the person mentioning the statement. A situation where each statement is true or false is that when there is a discussion between the existences of something like god. Each and every statement in this situation will be either true or false. The statement â€Å"God exists† can be true or false because no one really knows if god really exists. In the example, â€Å"Mathematics is an easy subject. † The truth value of the statement is either true or false. Also the negation of the sentence has a truth value of either true or false. If the truth value of the first statement is determined to be true, then the truth value of the negation will be false. On the other hand, if the truth value of the first statement is false then the truth value of the negation will be true.

Small Scale GTL (STG Plus) Plant

Small Scale GTL (STG Plus) Plant Course: Natural Gas Processing Technology (ENCH 609, Winter 2017) PROJECT TITLE GTL: Syngas to Gasoline (STG Plus) Professor: Dr. Nashaat Nassar List of figures and tables: Fig 1. Schematic sketch of the STG+ system (from Primus Green Energy TM) .. (6) Fig 2. Sensitivity Analysis for case 62.5 MMSCFD (14) Table 1. Economic Indicators for project evaluation (Detail calculation in Appendix).. (15) Appendix: Fig 1. Operating GTL plants on the world map [The Oil Gas Year, 2015] . (21) Fig 2. Simulation flow chart developed for the project (from Aspen plus V 7.2 Microsoft Visio 2010) (22) Table 1: Used compounds and Values of yields for reactor 4 in the model . (19-20) Table 2: Economic Evaluation for case 1: 10 MMSCFD ..(23) Table 3: Economic Evaluation for Case 2: 62.45 MMSCFD (24) Table 4: Mass balance of streams 1-22 for Case 1: 10 MMSCFD .(25-26) Table 5: Mass balance of streams 1-22 for Case 2: 62.45 MMSCFD .. (27-28) Abstract: The worlds energy demand is growing exponentially and to meet this demand, bringing new supply sources to the market is extremely critical. Natural gas resources are plentiful, geographically diverse and currently also the cleanest burning fossil fuel. Gas to Liquids (GTL) is a chemical process that transforms natural gas or other gaseous hydrocarbons into high quality liquid products that would otherwise be produced from crude oil [Shell Global]. GTL creates an additional opportunity to monetize a countrys resource of natural gas by turning them into high quality liquid fuels. GTL products are colorless and odorless hydrocarbons with very low level of impurities. The purpose of this project is to simulate a small scale GTL (STG Plus) plant that converts 10 MMSCFD of rich-methane natural gas into 672 BBL/day of gasoline. The first step of the STG Plus process is called steam reforming and it consists of the reaction between the methane in the natural gas with abundant water. The second step of the process is the reaction between the hydrogen, and the carbon monoxide producing methanol. The methanol thus formed will be converted to dimethyl ether (DME) and finally, the DME will be dehydrated, producing gasoline. The project will also highlight the difference between two major GTL technologies: Fischer Tropsch and STG Plus. An economic evaluation was conducted to check the viability of this process and at 10 MMSCFD conversion of methane; the project proves to be economically profitable, with an NPV value of $14.66M at 10% discount rate. It was also determined that if the production of gasoline increases to over 4,100BBL/day, the profitability of this project will increase significantly. 1.0. Introduction 1.1. GTL Technology and the World Gasoline to Liquid (GTL) is a technology that converts natural gas or other gaseous hydrocarbons into high quality liquid products like gasoline or diesel fuel, otherwise produced from crude oil []. GTL products are colorless and odorless hydrocarbons with very low level of impurities. Refineries can also use GTL to convert some of their gaseous hydrocarbon waste products into valuable fuel oil which can be used to generate income. The worlds first commercial GTL plant was opened by Shell in Bintulu, Malaysia in 1993. In 2011, the largest GTL plant, Pearl GTL was opened in Qatar [Shell Global]. Figure 1 in the Appendix shows all operating GTL plants and their corresponding locations on the world map. 1.2. GTL Origin In 1920s, when Germany found itself short of petroleum but with ample reserves of coal, GTL and Coal-to-Liquids (CTL) technologies were pioneered using a process known as Fischer-Tropsch (F-T) synthesis (Heng et al. 2004). Methanol-to-gasoline (MTG), Mobils synthetic gasoline process, based on the transformation of methanol to hydrocarbons using zeolite catalysts, was the first major synfuel process development in half a century since the development of the Fischer-Tropsch process (Frerich J. Keil, 1998). 1.3. Gas-to-Liquid (GTL) technology Gas to Liquids (GTL) is a refinery process that converts gas or other gaseous hydrocarbons into products with longer carbon chains. Gasoline and diesel fuel are classic examples. Gases with a high concentration of methane are transformed into liquid synthetic fuels following two methods: direct transformation using processes without the presence of catalysts that convert methane to methanol or by using syngas as a midway product, such as in the Fischer Tropsch, Syngas to Gasoline Plus and Mobil processes. This project will focus on designing a small scale Syngas to Gasoline (STG) plus plant that uses methane rich natural gas as feed and converts it to high quality gasoline and other products. 2.0. Syngas-to-Gasoline plus (STG+) process STG+ process was derived from the MTG (Methanol-to-Gasoline) process, which was developed by Mobil in the 1970s. This technology directly converts natural gas-derived syngas into drop-in gasoline and jet fuel through a catalytic thermo-chemical single-loop process that minimizes complexity, improves product quality and yield. The plus in STG+ stands for the alternate end products yielded by the process. The STG+ technology is currently operating by Primus Green Energy company in Hillsborough, New Jersey at pre-commercial scale with a production of 100,000 gallons (approximately) of distinct quality gasoline per year from natural gas with surpassed performance of the STG+ system and catalyst and 720 hours of continuous operation. The STG+ process consists of the following operating steps in one continuous process loop. It comprises of Syngas generation by steam reforming method, four fixed bed reactors in series and a two phase separator. Figure 1: Schematic sketch of the STG+ system (from Primus Green Energy TM) 2.1. Syngas Generation by Steam reforming method The first step in the STG+ process is to convert the natural gas feed into syngas or synthesis gas which is an intermediate gas feed for many different petrochemical processes. This processing basically removes contaminants, such as mercaptans, sulfides, mercury and any others that can compromise the various catalysts performance that are used in the STG+ reactors before it is fed to the syngas generation unit. Either partial oxidation or steam reforming processes are used for syngas production. Steam reforming process is widely used to generate syngas for feedstock in different petrochemical processes. A mixture of hydrogen, carbon monoxide, carbon dioxide, and unconverted methane and steam are formed when methane reacts with steam in the presence of a catalyst such as Nickel or Rhodium at high temperature (800-1000 C), high pressure (20-40 bars) and steam-to-carbon ratio varying between 1.8 and 4 in the steam reforming process which is highly endothermic in nature (Mbodji et al., 2012). The possible reactions are: The steam methane reforming reaction (SMR) CH4 + H2O à ¢Ã¢â‚¬ ¡Ã¢â‚¬Å¾ CO + 3H2 [ΆH = +206 kJ mol-1] (strongly endothermic).. (1) The water-gas shift (WGS) CO + H2O à ¢Ã¢â‚¬ ¡Ã¢â‚¬Å¾ CO2 + H2 [ΆH = -41 kJ mol-1] (moderately exothermic) . (2) The product from the reformer depends on the operating pressure temperature, composition of the feed gas, and the proportion of steam fed to the reactor. The thermodynamics and kinetics of the reaction within the reformer decides the amount of carbon monoxide in the final product from the steam reformer (Larminie Dicks, 2000). 2.2. Reactor 1 (Methanol Synthesis) Centrifugal compressors are used to compress the syngas from reforming unit which enters the reactor 1 containing copper zinc as catalyst and the following reaction occurs. 2H2 + CO à ¢Ã¢â‚¬ ¡Ã¢â‚¬Å¾ CH3OH [ΆH = -92 kJ mol-1] .. (3) Due to the exothermic nature of the reactions, low temperatures favor conversion to methanol and pre-heating of the reactant gas and heating of the boiler feed water are done by this excess heat. The position of the equilibrium depends on the pressure and temperature. The methanol formation is favored by increase in pressure. 2.3. Reactor 2 (Dimethyl Ether (DME) Synthesis) After the crude methanol from reactor 1 is preheated, vaporized and then superheated between 300-320oC in a series of heat exchangers, it is then sent to the dimethyl ether (DME) reactor containing a dehydration catalyst (alumina) where methanol is partially dehydrated to an equilibrium mixture of DME, water and methanol which is a reversible and exothermic reaction. 2CH3OH à ¢Ã¢â‚¬ ¡Ã¢â‚¬Å¾ CH3OCH3 + H2O . (4) 2.4. Reactor 3 (Gasoline Synthesis) In reactor 3, in presence of catalyst the product gas from reactor 2 converts to hydrocarbons including paraffins (alkanes), aromatics, naphthene (cycloalkanes) and olefins (alkenes), mostly from C6 to C10. 2.5. Reactor 4 (Gasoline Treatment)    To have high octane number for synthetic gasoline and desirable volumetric properties, the product from reactor 3 is treated in reactor 4 to reduce the durene (tetra methylbenzene), Iso durene and tri methylbenzene components which have high freezing points. 2.6. Separator Finally, in the reactor 4 two or three phase separation is done to obtain synthetic gasoline comprised of paraffins, aromatics and naphthene, non-condensed gas and water. The non-condensed gas is recycled back to the feed stream for reactor 1 and water is recycled back to the Steam Reformer (Syngas Generation Unit). 3.0. Why STG+? The previous group responsible for GTL used the conventional GTL technology called Fisher Tropsh (FT) in their simulation process. Fischer-Tropsch (FT), which is a technology developed in early 1920s, converts gas into liquid hydrocarbons mainly diesel through a very complex process. While there have been significant improvements on the efficiency and technology of the Fisher-Tropsch process, the industry is in an urgent need of new technologies capable of converting as much gas as possible into liquid fuels in a cheaper and more efficiently manner. As consequence, we decided to apply for our project the novel process called STG+ developed by Primus Energy. The main product of STG+ is gasoline as opposed to diesel. Since the most demanded liquid fuel in Canada, especially in Alberta, is gas, we decided not use FT or any new technology producing diesel. STG+ has numerous advantages over the conventional GTL techniques such as: lower operating and capital costs, higher production, bett er product quality and faster delivery times. The rival technology of STG+ is ExxonMobils MTG process. However, ExxonMobils MTG process has a greater environmental impact and it is not very cost-effective. STG+ process was designed to correct some inefficiencies in the ExxonMobil process . The main correction is the integration of the reactors in a single-loop that increases the production and yields a higher quality of the gasoline with a less environmental impact A key example is integration of the reactors in the STG+ process. 4.0. Project Design/Simulation 4.1. Flowchart Description The lists of components that are considered in the simulation for the STG+ process and the yields in mass base for the fourth reactor (Keil, 2012) are shown in the Appendix (Table 1). The flowchart developed for the STG+ process is shown in the fig. 2 of Appendix. A brief explanation of the flowchart will be done now. First, our feedstock is basically the natural gas. For simplification purposes, our feed of natural gas is basically methane. Another feedstock that this process will have is fresh water. The water will be heated in a heat exchanger (HE-01) and will be mixed with the methane to enter the first reactor (R-01). In this reactor, carbon monoxide, carbon dioxide and hydrogen will be produced, as explained above. The fractional conversion in the first reaction is 83.4% of the methane, the limiting reactant. The conversion in the second reaction is 6% of the carbon monoxide (Choudhary et al, 1992). The exit stream of the reactor R-01 is cooled in a heat exchanger (HE-02), enters a compressor (CP-01) to increase the pressure for the second reaction process and, finally, enters another heat exchanger (HE-03) to adjust the temperature for the ideal temperature in reactor R-02. The operating conditions of this reactor are 69 bar and 380ƚ °C (Wood et al, 2012). In it, basically, the syngas will be consumed to form methanol. The fractional conversion of this reaction is 63.7% of carbon monoxide (Lebarbier et al, 2012). The exit stream of reactor R-02 will pass through a heat exchanger (HE-04) to adjust the temperature of the mixture to enter reactor R-03. The methanol will form dimethyl ether (DME) and water. The operating conditions of this reactor are 12 bar and 325 °C (Wood et al, 2012). The fractional conversion of the methanol for this process is 76% (Kasaie et al, 2010). The stream that comes out of reactor R-03 passes through a heat exchanger (HE-05) to reduce its temperature and then enters a liquid-vapor flash vessel (FV-01). The dimethyl ether along with the non-polar components will come out in the gas stream, while the water will come out in the bottom or liquid stream, which can be sent to the effluent treatment plant. The gas stream will pass through a compressor (CP-02) and then through a heat exchanger (HE-06) to adjust the temperature and pressure for the fourth reaction process in reactor R-04. Basically, in this reactor, the dimethyl ether will be dehydrated in order to break down its molecule into -C2H4- radicals, which will be combined to form bigger molecules, as explained above. Since the reaction process is complex and the number of reactions is big, the stoichiometry of the process will be very complicated. Therefore, this paper only shows the yield in mass basis of each component formed in reactor R-04 (yield per unit mass of tota l feed of components that are not listed as inerts) (Aspentech Support Technology, 2001). Since only the dimethyl ether (DME) is a reactant in reactor R-04, all of the other compounds that enter reactor R-04 are considered inerts. The exit stream of reactor R-04 will pass through a compressor (CP-03) and through a heat exchanger (HE-07) to adjust the pressure and temperature for the last flash vessel (FV-02). This flash vessel is a liquid-liquid-vapor separator that will separate on the top the gas and lightest products. The middle liquid stream will be the gasoline formed (main stream) and the bottom liquid stream will be the water that was formed in the reactor R-04 and must be removed. The gas stream can be sold to an industry that processes gas phase hydrocarbons, while the water removed can be sent to the effluent treatment plant. 4.2. Thermodynamic Model and Simulation Considerations The simulation of the STG+ process was developed in the software Aspen Plus ® version 7.2. In our simulation, we chose the GRAYSON model, because it was developed for systems consisting of hydrocarbons, such as carbon dioxide and hydrogen sulfide. This method should return good results for temperatures in the range of 60 °F to 800 °F and pressures up to 3000 psia (Aspentech Support Technology, 2001). Since our process contains hydrogen and all the temperatures of the streams are within this temperature range, we can use the GRAYSON model (Aspentech Support Technology, 2001). The first three reactors (R-01, R-02 and R-03) were modeled in Aspen Plus as RSTOIC reactors since only fractional conversions and stoichiometry were considered for them. The last reactor (R-04) was modeled as an RYIELD reactor. In this model, the input data that is required consists of the outlet temperature and pressure of the reactor, as well as the yield values for the components that are products of the reaction process. 4.3. Assumptions adopted in the simulation Natural gas feed consists only of methane; We used only flash drums to perform the separation of the components after the reactions. The gasoline yields only consist of paraffins, olefins, aromatics and cyclic hydrocarbons from C2 to C11. Fractional conversions and stoichiometry are only considered for the first three reactors and no kinetic parameters for the reaction processes and catalyst deactivation are considered due to lack of data. Even though the STG+ process is well known for the loop which defines the efficiency of the process, due to lack of data on fractional conversions for C2-C11 compounds, we restricted our simulation till gasoline production and planned to sell our product (Gasoline and Natural Gas) to the other parties who are in charge of any post treatment required. Since we are not including the durene/Isodurene in our output, the Gasoline treatment reactor is not considered. 5.0. Economic Evaluation In order to evaluate the economics of the project, a cash flow analysis is made based on the following considerations: Our business model consider buying treated natural gas to be used as both feedstock and fuel gas (we dont pay royalties because we are not producing it), paying for electricity consumption; and revenues come from gasoline and natural gas sales. Two years for construction and 20 years of operations. 340 days of production per year. Analysis in constant American dollars of January 2017, exchange rate of 1.30 CAD to USD. Annual non-fuel operating and maintenance cost equal to 3.6% (Haro P. et al ,2013) of total capital expenditures. Corporate income tax rate equal to 28%. Electricity consumption, fuel gas required, flow rates (feed and products) from the simulation model. Current prices for gasoline, natural gas and electricity in Alberta, taken from Alberta Energy websites. Capital Cost Allowance (CCA) with a half year rule is considered for tax calculation purpose according to Alberta legislation. Discount rate 10%. Capital expenditure (CAPEX) for syngas generation is estimated using figures for a known plant (Yang Ogden, 2005) and the following equation to take into account the different capacities. . (5) Where, Cx = capital cost for a plant of size x (Sx), Cb = capital cost of the known plant of size b (Sb). CAPEX related to the STG+ process itself is estimated based on the ratio given by Primus Green Energy (company proprietary of the STG+ technology) that syngas generation typically represents 60% of total capital cost for commercial-scale plant and the STG+ process itself represents the other 40%. Two scales are considered: 10 MMSCFD of natural gas in the feed for comparison purpose with the previous years group and 62.5 MMSCFD of natural gas in the feed to evaluate the influence of the scale on the economic indicators. The economic indicators of the project are summarized in the following table: Feed Gas Flow rates (MMSCFD) 10 62.5 Net Present Value NPV @10% (million $) 14.66 371.86 Internal Rate of Return IRR 12.12% 22.87% Profit to Investment Ratio PIR 0.14 0.97 Breakeven price for Gasoline (CAD/L) 0.91 0.62 Table 1: Economic Indicators for project evaluation (Detail calculation in Appendix) Finally, a sensitivity analysis is made to see the influence of different variables: natural gas price, electricity price, gasoline price and capital cost on the NPV of the project. For these, all variables are changed +10% and -10% and the NPV are calculated. Results shown in the fig. 2 correspond to the case with 62.5 MMSCFD in the feed. However, it is the same trend in both cases: Figure 2: Sensitivity Analysis for case 62.5 MMSCFD It can be concluded that the project is economically feasible and the variable that impact the most the economics of the project is the gasoline price. 6.0. Recommendations We recommend considering the fractional conversions for C2-C11 compounds in reactor 1 to have a better picture of STG+ with its close loop process. A thorough composition analysis for gasoline in the fourth reactor gives more realistic results. There is much scope to extend our work by adding gasoline treatment and distillation column (instead of flash drum for more efficient separation) with proper chemical reactions and stoichiometric fractional conversions and kinetics to improve the market value of our product. There is possibility for considering more components in the feed gas till C5-C6. In our model, due to lack of data, we focused on chemical reactions and stoichiometric fractional conversions. There is scope for more efficient designing by working on catalyst cycle life. 7.0. Conclusion The 21st century is witnessing the establishment of a new global business based on natural gas processing. As a consequence, the gas-to-liquids (GTL) industry is becoming increasingly important as it is getting more difficult to find and extract new oil reserves as well as the presence of more environmental restraints. This is why we decided to apply the new STG+ process technology in our project to demonstrate its efficiency in the conversion of methane to gasoline. As previously stated, we decided to differ from the previous group process, mainly because its technology is old and their product is diesel as opposed to STG+ process which is a novel technology and its product being gasoline, which is more demanded in Canada. We chose to do the simulation of a small scale GTL plant that processes 10 MMSCFD of methane, producing 672 bbld, which resulted in an economically viable process. The economic indicators showed that, by increasing the production of gasoline, the profit would incr ease significantly (proven with the case 0f 62.5 MMSCFD). In conclusion, STG+ might be indeed successful and profitable in Alberta if there is a reliable source of natural gas and good market conditions. 8.0. References Alberta energy website.http://www.energy.alberta.ca/NaturalGas/1316.asp. Accessed on March 16th, 2017. Alberta energy website.http://www.energy.alberta.ca/Electricity/679.asp. Accessed on March 16th, 2017. Aspentech Support Technology, Inc.; Aspen Physical Property System 11.1; Cambridge, MA, September 2001. Choudhary V. R., Rajput A. M., Prabhakar B; Low temperature oxidative conversion of methane to syngas over NiO-CaO catalyst; Chemical Engineering Division; National Chemical Laboratory, India, May 1992. Haro P, Trippe F, Stahl R, Henrich E. Bio-syngas to gasoline and olefins via DME: A comprehensive Techno-economic assessment; Apple Energy; 2013; volume 108; page no.: 54-65. Heng H.C., Idrus. S; The future of gas to liquids as a gas monetization option; Journal of Natural Gas Chemistry 13, 2004; pages 63-70. http://www.albertagasprices.com/index.aspx?fuel=C . Accessed on March 16th, 2017. Kasaie M., Sohrabi M.; Kinetic Study on Methanol Dehydration to Dimethyl Ether Applying Clinoptilolite Zeolite as the Reaction Catalyst; Chemical Engineering Department, Amirkabir University of Technology, Tehran, Iran, January 2010. Keil, Frerich J.; Methanol-to-hydrocarbons: process technology; Department of Chemical Engineering, Technical University of Hamburg-Harburg, Hamburg, Germany, July 1998; page 49. Larminie, James, Dicks, Andrew; Fuel Cell Systems Explained; West Sussex, U.K.: John Wiley Sons; 2000. Lebarbier V. M., Dagle R. A., Kovarik L., Adarme J. A. L., King D. L., Palo D. R.; Synthesis of methanol and dimethyl ether from syngas over Pd/ZnO/Al2O3 catalysts; Richland, USA, June 2012. Mbodji M., Commenge J.M., Falk L., Di Marco, Rossignol F., Prost L., Valentin S., Joly R., Del-Gallo P. Steam methane reforming reaction process intensification by using a milli structured reactor: Experimental setup and model validation for global kinetic reaction rate estimation, Chemical Engineering Journal, vol. 207-208, pages 871-884. Primus Green Energy website (http://primusge.wpengine.com/press-room/white-papers/), Accessed in March 2017. Shell Global Website (http://www.shell.com/energy-and-innovation/natural-gas/gas-to-liquids.htm), Accessed March 05, 2017. Wood, David A., Nwaoha C., Towler, Brian F; Gas-to-liquids (GTL): A review of an industry offering several routes for monetizing natural gas; Journal of Natural Gas Science and Engineering, Volume 9, November 2012. Yang, Christopher; Ogden, Joan M. (2005).Analyzing Natural Gas Based Hydrogen Infrastructure Optimizing Transitions from Distributed to Centralized H2 Production; Institute of Transportation Studies; UC Davis. 9.0. Appendix Component in Aspen Plus ® Component name Formula Mass yield METHANE Methane CH4 - METHANOL Methanol CH4O - CO Carbon monoxide CO - CO2 Carbon dioxide CO2 - H2O Water H2O - ETHER Dimethyl ether C2H6O - H2 Hydrogen H2 - OCTANE n-Octane C8H18 3.582 HEXANE n-Hexane C6H14 2.702 HEPTANE n-Heptane C7H16 3.142 NONANE n-Nonane C9H20 4.022 DECANE n-Decane C10H22 4.462 N-C11 n-Undecane C11H24 24.602 N-C5 n-Pentane C5H12 36.078 OXYGEN Oxygen O2 47.549 ETHANE Ethane C2H6 4.901 PROPANE Propane C3H8 45.691 N-BUTANE n-Butane C4H10 69.321 ISOC4 Isobutane C4H10 101.615 ISOC5 2-Methyl-butane C5H12 75.269 ISOC6 2-Methyl-pentane C6H14 34.921 ISOC7 2,2-Dimethylpentane C7H16 3.137 ISOC8 2,2-Dimethylhexane C8H18 1.690 ISOC9 2-Methyloctane C9H20 0.491 ISOC10 2-Methylnonane C10H22 37.092 AROMC6 Benzene C6H6 4.024 AROMC7 o-Xylene C8H1

Irelands Michael Collins And Emon De Valera :: essays research papers

Ireland's Michael Collins and Emon De Valera   Ã‚  Ã‚  Ã‚  Ã‚  There are many conditions under which Ireland was divided into two nations. Two main men were the main leaders of this split, Emon de Valera and Michael Collins. Sinn Fein also played a large role. Their differing visions for an Ireland free of British rule was the root motivation for the split.   Ã‚  Ã‚  Ã‚  Ã‚  Born in New York City in 1882, Emon de Valera was described as a 'tall, spectacled, schoolmasterly, of Jewish cast' as Tim Healy said. Edward Norman, the author of A History of Modern Ireland, added that de Valera was an 'austere theoretician' (Norman, 265). Michael Collins was born in 1890 at Clonakilty, Co. Cork. Edward Norman said his personality was to be to the contrary of de Valera's; he said Collins was not an intellectual and was a man of violent impulses. He took that statement further when he said the Collins would go as far to tumble his colleagues on the floor and bite their ears in playful attention. Now that de Valera's and Collins' personalities have been established, we can now analyze the events and actual conditions under which Ireland was under that led ultimately to her freedom.   Ã‚  Ã‚  Ã‚  Ã‚  All across Ireland people were repulsed by the executions which they considered to be needlessly brutal. What they lacked was new leadership to focus the restless energy of the Irish into effective political action, but it was not long in coming. At Christmas 1916 all rebel prisoners who had been interned without trial, those that the British had considered insignificant, were released as a goodwill gesture to the United States which had been very angry by British conduct regarding the rebels. This proved to be a costly mistake. Among those released was a cadre of IRB men who had spent their time in prison educating and organizing themselves into what came out to be a formidable political and military force. The leader of these efforts in prison was Michael Collins, who was still a little known Volunteer at the time.   Ã‚  Ã‚  Ã‚  Ã‚  Despite martial law, Collins contacted the members of his secret organization throughout Ireland and set in motion a clever plan to obtain political power. Using Sinn Fein as cover, the IRB began to run its members as candidates for parliament. Their successes throughout 1917 against Redmond's Irish Parliamentary Party candidates shifted power to Sinn Fein and caused a turmoil of public support for the republican movement throughout Catholic Ireland. After Collins release in June, 1917,Eamon de Valera, the oldest of the surviving 1916 rebels, joined Collins. De Valera was lucky for he had been

Fighting a War :: Personal Narrative Papers

Fighting a War I have never been to war. I hope I'll never go. There is nothing that I believe in enough to sacrifice my life. These are supposed to be days of idealism and youth, and I am blessed. I cannot care. I cannot fight. The only appealing little thing about violence is the potential for heroism, and I doubt I'll ever be a hero or save an innocent life from a burning building, stop a runaway train like so many bad movies. I can't see myself triumphing over this world. I can see myself climb out of the trench and nobly get mowed down by the bullets of a gattling gun. I let fly an arrow from my longbow. In the cockpit of a fighter plane, props twirling, I strafe Japanese ships and dodge innumerable Zeros. On a dusty hill I calculate the trajectory of an artillery shell and re-check my math. I slink through a dark jungle and blend in with the foliage, camouflaging my thoughts, a shadow amidst all the life. I can only see myself in war movies, not in actual wars. I have never been in an honest-to-god kill or be killed full on violent fight, much less a nationally sponsored war. Never defended my life or my honor, or someone else's; but I have taken and sadly given a beating. The closest I have ever been to war is a controlled skirmish with a friend, a fistfight for fun. No anger. One time, at his twenty-first birthday party, Frank and I gave up on docile lives and began to fight. Neither of us was born in Idaho. We never grew up together but we've both spent some time there. Our families moved, his east mine west, Hong Kong and Connecticut, so we're there for the summer and the winter. We know some of the same people, like the Peruvians and Adam Pracna and Jason Spicer, but we're three years too far apart. I'm younger, and we never hung out. We've got mutual friends and we've eaten at all the same places. Small town, not many places. We've both driven out the same canyons in a pickup with mud and girls, same girls? Who knows? There's a keg or two in the back kicking up dust up into it all and clouding up the sky, and we're throwing empty glass bottles shattering at trees and shadows and animals as we drive and sing.

Its my opinion :: social issues

It's my opinion I was told that the principal had used her executive power to chop up my article into bits that didn’t contain the harassing, offensive points that it originally owned. I was sad, very very sad. It’s tough for someone with a weak emotional structure to be rejected and told I’m harassing to younger people. So, the advisors went to the bargaining table, nothing changed. Therefore we revised, redid, and reedited the entire article and pumped out a version that had the heart and soul cut out of it, but we put it in the paper anyway. The version that came out in the last edition didn’t have the same edge that the original copy had. Now I have respect for people who have the courage to challenge the freedom of press (that’d be me). Bring it on. I’m not afraid of having my paper rejected. I take it as a compliment. If you want to try to challenge me, I will have the last word. I think of myself as an Epicurean. That means I don’t believe in emotions, but it also means I’m perverted. Anyway, someone without emotions has no conscience, without a conscience you are free of convictions. Being free of conviction means I cannot be offended. My anger is under my control, I choose not anger myself with the people who are angered with me. I divert my anger to people who cannot control themselves. That basically means that if your mad at me, and you try to make me angry it won’t work. For the last year of writing this column it has been more or less a joke. It was designed to make people chuckle a little. Now, this year I was told by the staff that the offender had no real point, just humor. So I decided for my first piece I would take a controversial subject, such as eroding senior privileges, and put my own point of view down and the point of view from many of the other seniors. I realize that I didn’t look at it from everyone’s point of view. That, I believe, was a mistake on my behalf. This is a subject that has seriously infuriated me and I took it out in a public piece. I believe there will be more people looking to my column, since I have written a controversial piece.

First Day of School Essay

Life is full of surprises and difficulties. A college can make your life are changing after you walked into the campus at first day in college. I used to think about the class in college which is different from in high school. Those people who are older than me, they have told me that college would be new life for me. That college would show me what is the differently between college and high school. I was really wondering about it, I didn’t know anything since the first year and first day. Everything I knew before I went to college that was I had to studied more harder, and I won’t have many friends like I did in high school. The most things that I was interesting is about the course class, the education, the campuses. They took me to a new look, and they show me what is real college life. see more:my first day at school paragraph I wasn’t thinking the differently from high school to college is big deal, but I have a bit scared when I went into the campus, and I have seen many students that I didn’t know anyone of them. First class were surprise me because that was about 20 to 30 students only, but they aren’t friend to each other. I went to my class early so that I can get a good seat close to teacher, and I can meet my classmate. That was lucky because I just met a old friend from high school in the first class. Therefore, the class is not so scaring anymore and everything is seemed to be better than before. After the first class, I just knew another things, that is college students didn’t like to make friends like we did in high school. They came to class to record the lecture then they left the class after the lecture done without any talk. College’s course classes are really differently. First, the college classes are taking more time than the high school, they are taking about two hour for each day. All I could do in class that was hearing the lecture from professor. That was not really for all class, there was some professors let us doing group works. The professors tried to help students had more time to knew each other, and they worked better in their works. The lecture is  taking about two hour, it made the students fall in sleep easy. Now is one another thing, I did not realize that college’s student could wear whatever they want; it doesn’t matter with the uniform. Students can’t talk to each other during lecture that is reason students are not so friendly when they tried to ask the other about homework or any assignment. However, students can leave early before class end 15 minutes or 20 minutes early, In high school, students would get their assignments and homework from the professors in class, but that was not for college. Everything are in online and website, assignments, homework, projects, including lecture summaries. All the assignment and homework had dude day, it really could help students have more time to do their work, and they will management their time life more easy. In high school, teacher always gave us homework before we left class, and turn them in next day. I knew sometime we won’t have enough time, but that is more helpful to students because they would catch up and learned more about what they learned in class that day. All the course class, they have a schedule for lecture, tests, quiz and the final. The professors did that because they didn’t want the students miss any test or final. There is no time to make up any test if we are absent and miss those test. College is having many campuses, those are really cool and bigger than the high school campus. I knew it is unfair compare but that is truth, there is some class have around 100 students in one lecture. Some college campuses are really big with 3 or 4 floors up, each one have more than 50 rooms to be laboratory, class rooms, computer labs. Students can have free internet to research and doing their homework without going home. The library have all the kind of books, it is helping students find their book easy, and students can use the desktop in library to do their project. I think college is a new world, and new life, that is giving me more option, surprises and difficulties. College is changing my angle personal life, it gave me the knowledge and the differently between high school and college. I sum up my College life as an impactful one, but I think I could’ve done better to be someone I hope to be. I’ve learnt to change my own view after I saw everything college in front of my eyes, it is not that difficult like  the other people told me before. All the things, The course class, the education, the campuses are totally changing my to new life.

NCO on my Staff

My subordinates describe as bold, fearless and direct. They also know if they have problems they should exhaust all their resources before coming to me with that problem. Additionally, my subordinates know I would do anything to better them even if the action is not popular. Finally, my subordinates would describe me as a work hard play hard type of NCO. 4. How would you describe yourself as NCO? Would describe my self as a trying to become a great NCO.There is always room for improvement so I never agreed with the term a good NCO. Have my Moments, but I can get a little stubborn at times which may seem a little bit disobedient, but do believe you have to ruffle feathers if you are being a good NCO. 5. How would your supervisor describe me as a NCO? My supervisor would describe me as a NCO who embodies the leadership style idealized influence, and intellectual stimulation. I'm not one to bark orders or give task I haven't done or wouldn't do my self.My supervisor also feels I'm his g o to NCO on my Staff. Some people are fly swatters others are hammers then you have the Ax; I'm been told I am the Ax. 6. What are my strengths? Feel my strengths are my ability to think outside the box. Feel bring lots of creativity to the most trivial task. I feel if we don't mix things up and promote freethinking we move in the wrong direction, and fife will past us by waking up one day wondering what happen.Additionally, believe working under pressure no matter the task is strength. Some may see it as procrastination at times, but it gets the job done when things hit the fan. Or when something critical comes down at the last minute. 7. What is my Essence? My essence is my struggle, which defines me who I am. I honestly that if I didn't get two article 1 g's I would not be here Wright now.