National Library of Energy BETA

Sample records for butylene isobutane isobutylene

  1. TABLE56.CHP:Corel VENTURA

    Annual Energy Outlook [U.S. Energy Information Administration (EIA)]

    ... 2,153 0 2,153 1,884 1,514 370 Normal ButaneButylene ... 0 0 0 527 415 112 IsobutaneIsobutylene...

  2. Product Supplied for Total Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    EthaneEthylene PropanePropylene Normal ButaneButylene IsobutaneIsobutylene Other Liquids HydrogenOxygenatesRenewablesOther Hydrocarbons Unfinished Oils Motor Gasoline Blend. ...

  3. EIA-800

    U.S. Energy Information Administration (EIA) Indexed Site

    ... Residual Fuel Oil 511 Asphalt and Road Oil 931 * Includes propane, propylene, ethane, ethylene, normal butane, butylene, isobutane, isobutylene, and pentanes plus. Quantities ...

  4. Version No.:2010.01 PART 2. SUBMISSION/RESUBMISSION INFORMATION

    U.S. Energy Information Administration (EIA) Indexed Site

    Residual Fuel Oil 511 Other Petroleum Products 666 *Includes propane, propylene, ethane, ethylene, normal butane, butylene, isobutane, and isobutylene, and pentanes plus Algeria ...

  5. EIA-802

    U.S. Energy Information Administration (EIA) Indexed Site

    CODE 466 PADD 4 * Includes propane, propylene, ethane, ethylene, normal butane, butylene, isobutane, isobutylene, and pentanes plus. PADD 3 PADD 2 Item Description Product Code ...

  6. EIA-817

    U.S. Energy Information Administration (EIA) Indexed Site

    Fuel 205 Other Renewable Fuels 207 Liquefied Petroleum and Refinery Gases: EthaneEthylene 108 PropanePropylene 246 Normal ButaneButylene 244 IsobutaneIsobutylene 245 ...

  7. Refinery Net Production of Total Finished Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    Product: Total Finished Petroleum Products Liquefied Refinery Gases Ethane/Ethylene Ethane Ethylene Propane/Propylene Propane Propylene Normal Butane/Butylene Normal Butane Butylene Isobutane/Isobutylene Isobutane Isobutylene Finished Motor Gasoline Reformulated Gasoline Reformulated Blended w/ Fuel Ethanol Reformulated Other Conventional Gasoline Conventional Blended w/ Fuel Ethanol Conventional Blended w/ Fuel Ethanol, Ed55 and Lower Conventional Blended w/ Fuel Ethanol, Greater than Ed55

  8. Refinery & Blender Net Production of Total Finished Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    & Blender Net Production Product: Total Finished Petroleum Products Liquefied Refinery Gases Ethane/Ethylene Ethane Ethylene Propane/Propylene Propane Propylene Normal Butane/Butylene Normal Butane Butylene Isobutane/Isobutylene Isobutane Isobutylene Finished Motor Gasoline Reformulated Gasoline Reformulated Blended w/ Fuel Ethanol Reformulated Other Gasoline Conventional Gasoline Conventional Blended w/ Fuel Ethanol Conventional Blended w/ Fuel Ethanol, Ed55 and Lower Conventional Blended

  9. Total Crude Oil and Petroleum Products Exports

    U.S. Energy Information Administration (EIA) Indexed Site

    Exports Product: Total Crude Oil and Petroleum Products Crude Oil Natural Gas Plant Liquids and Liquefied Refinery Gases Pentanes Plus Liquefied Petroleum Gases Ethane/Ethylene Propane/Propylene Normal Butane/Butylene Isobutane/Isobutylene Other Liquids Hydrogen/Oxygenates/Renewables/Other Hydrocarbons Oxygenates (excl. Fuel Ethanol) Methyl Tertiary Butyl Ether (MTBE) Other Oxygenates Renewable Fuels (incl. Fuel Ethanol) Fuel Ethanol Biomass-Based Diesel Unfinished Oils Naphthas and Lighter

  10. Total Crude Oil and Petroleum Products Imports by Area of Entry

    U.S. Energy Information Administration (EIA) Indexed Site

    by Area of Entry Product: Total Crude Oil and Petroleum Products Crude Oil Natural Gas Plant Liquids and Liquefied Refinery Gases Pentanes Plus Liquefied Petroleum Gases Ethane Ethylene Propane Propylene Normal Butane Butylene Isobutane Isobutylene Other Liquids Hydrogen/Oxygenates/Renewables/Other Hydrocarbons Oxygenates (excl. Fuel Ethanol) Methyl Tertiary Butyl Ether (MTBE) Other Oxygenates Renewable Fuels (incl. Fuel Ethanol) Fuel Ethanol Biomass-Based Diesel Fuel Other Renewable Diesel Fuel

  11. Total number of slots consumed in long_excl.q (exclusive nodes) will be

    Broader source: All U.S. Department of Energy (DOE) Office Webpages (Extended Search)

    Product: Total Crude Oil and Petroleum Products Crude Oil Natural Gas Plant Liquids and Liquefied Refinery Gases Pentanes Plus Liquefied Petroleum Gases Ethane/Ethylene Propane/Propylene Normal Butane/Butylene Isobutane/Isobutylene Other Liquids Hydrogen/Oxygenates/Renewables/Other Hydrocarbons Oxygenates (excl. Fuel Ethanol) Methyl Tertiary Butyl Ether (MTBE) Other Oxygenates Renewable Fuels (incl. Fuel Ethanol) Fuel Ethanol Biomass-Based Diesel Unfinished Oils Naphthas and Lighter Kerosene and

  12. table07.chp:Corel VENTURA

    Gasoline and Diesel Fuel Update (EIA)

    558 - 893 -73 1,935 -111 0 3,387 38 0 Natural Gas Liquids and LRGs ....... 283 89 116 - 9 -210 - 123 24 558 Pentanes Plus .................................. 37 - 1 - 17 7 - 25 15 9 Liquefied Petroleum Gases .............. 246 89 115 - -8 -217 - 98 10 550 Ethane/Ethylene ........................... 94 0 (s) - -71 -4 - 0 0 26 Propane/Propylene ....................... 100 116 86 - 31 -155 - 0 3 485 Normal Butane/Butylene .............. 37 -27 16 - 18 -48 - 74 6 12 Isobutane/Isobutylene

  13. Crude Oil plus Lease Condensate Proved Reserves, as of Dec. 31

    Gasoline and Diesel Fuel Update (EIA)

    Districts Pipeline between PAD Districts Product: Crude Oil and Petroleum Products Crude Oil Petroleum Products Pentanes Plus Liquefied Petroleum Gases Ethane/Ethylene Propane/Propylene Isobutane/Isobutylene Normal Butane/Butylene Motor Gasoline Blend. Comp. (MGBC) MGBC - Reformulated MGBC - Reformulated RBOB MGBC - RBOB for Blending w/ Alcohol* MGBC - Conventional MGBC - CBOB MGBC - Conventional GTAB MGBC - Conventional Other Renewable Fuels Renewable Diesel Fuel Finished Motor Gasoline

  14. Isobutane ignition delay time measurements at high pressure and detailed chemical kinetic simulations

    SciTech Connect (OSTI)

    Healy, D.; Curran, H.J.; Donato, N.S.; Aul, C.J.; Petersen, E.L.; Zinner, C.M.; Bourque, G.

    2010-08-15

    Rapid compression machine and shock-tube ignition experiments were performed for real fuel/air isobutane mixtures at equivalence ratios of 0.3, 0.5, 1, and 2. The wide range of experimental conditions included temperatures from 590 to 1567 K at pressures of approximately 1, 10, 20, and 30 atm. These data represent the most comprehensive set of experiments currently available for isobutane oxidation and further accentuate the complementary attributes of the two techniques toward high-pressure oxidation experiments over a wide range of temperatures. The experimental results were used to validate a detailed chemical kinetic model composed of 1328 reactions involving 230 species. This mechanism has been successfully used to simulate previously published ignition delay times as well. A thorough sensitivity analysis was performed to gain further insight to the chemical processes occurring at various conditions. Additionally, useful ignition delay time correlations were developed for temperatures greater than 1025 K. Comparisons are also made with available isobutane data from the literature, as well as with 100% n-butane and 50-50% n-butane-isobutane mixtures in air that were presented by the authors in recent studies. In general, the kinetic model shows excellent agreement with the data over the wide range of conditions of the present study. (author)

  15. Dynamics of Exchange at Gas-Zeolite Interfaces 1: Pure Component n-Butane and Isobutane

    SciTech Connect (OSTI)

    CHANDROSS,MICHAEL E.; WEBB III,EDMUND B.; GREST,GARY S.; MARTIN,MARCUS G.; THOMPSON,AIDAN P.; ROTH,M.W.

    2000-07-13

    The authors present the results of molecular dynamics simulations of n-butane and isobutane in silicalite. They begin with a comparison of the bulk adsorption and diffusion properties for two different parameterizations of the interaction potential between the hydrocarbon species, both of which have been shown to reproduce experimental gas-liquid coexistence curves. They examine diffusion as a function of the loading of the zeolite, as well as the temperature dependence of the diffusion constant at loading and for infinite dilution. They continue with simulations in which interfaces are formed between single component gases and the zeolite. After reaching equilibrium, they examine the dynamics of exchange between the bulk gas and the zeolite. Finally, they calculate the permeability of the zeolite for n-butane and isobutane as a function of pressure. Their simulations are performed for a number of different gas temperatures and pressures, covering a wide range of state points.

  16. Synthesis of Isobutene and Isobutane from Synthesis Gas. A Literature Review Since 1992

    SciTech Connect (OSTI)

    Petkovic, Lucia M.; Ginosar, Daniel M.

    2012-04-01

    The isosynthesis reaction is commonly referred as the reaction that converts selectively synthesis gas to isobutene and isobutane. The main feature of this reaction is the production of branched hydrocarbons in higher proportion with respect to linear hydrocarbons than expected from thermodynamic equilibrium and with a molecular weight distribution favoring iso-C4 hydrocarbons. This article reviews and summarizes isosynthesis research results reported in the open scientific literature with emphasis on the articles published in the last two decades.

  17. Ignition properties of n-butane and iso-butane in a rapid compression machine

    SciTech Connect (OSTI)

    Gersen, S.; Darmeveil, J.H.; Mokhov, A.V.; Levinsky, H.B.

    2010-02-15

    Autoignition delay times of n-butane and iso-butane have been measured in a Rapid Compression Machine in the temperature range 660-1010 K, at pressures varying from 14 to 36 bar and at equivalence ratios {phi} = 1.0 and {phi} = 0.5. Both butane isomers exhibit a negative-temperature-coefficient (NTC) region and, at low temperatures, two-stage ignition. At temperatures below {proportional_to}900 K, the delay times for iso-butane are longer than those for the normal isomer, while above this temperature both butanes give essentially the same results. At temperatures above {proportional_to}720 K the delay times of the lean mixtures are twice those for stoichiometric compositions; at T < 720 K, the equivalence ratio is seen to have little influence on the ignition behavior. Increasing the pressure from 15 bar to 30 bar decreases the amplitude of the NTC region, and reduces the ignition delay time for both isomers by roughly a factor of 3. In the region in which two-stage ignition is observed, 680-825 K, the duration of the first ignition stage decreases sharply in the range 680-770 K, but is essentially flat above 770 K. Good quantitative agreement is found between the measurements and calculations for n-butane using a comprehensive model for butane ignition, including both delay times in the two-stage region, with substantial differences being observed for iso-butane, particularly in the NTC region. (author)

  18. Thermodynamic properties of a geothermal working fluid; 90% isobutane-10% isopentane: Final report

    SciTech Connect (OSTI)

    Gallagher, J.S.; Linsky, D.; Morrison, G.; Levelt Sengers, J.M.H.

    1987-04-01

    We present tables of thermodynamic properties, and dew and bubble properties, of a mixture of 90 mol % isobutane and 10 mol % isopentane, a working fluid in a binary geothermal power cycle. The tables are generated by a formulation of the Helmholtz free energy, in which the mixture properties are mapped onto the known properties of pure isobutane by means of the principle of generalized corresponding states. The data base for the Helmholtz free energy formulation is new. We report data obtained in three different apparatus: critical-line and isopentane vapor pressure data obtained in a visual cell; vapor-liquid equilibria data obtained in a mercury-operated variable-volume cell; and pressure-volume-temperature data for the 90 mol %-10 mol % mixture obtained in a semi-automated Burnett-isochoric apparatus. The principles of the methods, and estimates of the reliability, are discussed and all experimental data are compared with the surface. The results are tables of specific volume, enthalpy, entropy, specific heat and density and temperature derivatives of the pressure at 10 K temperature increments from 240 to 600 K along isobars from 0.01 to 20 MPa. Separate tables are prepared from the dew and bubble properties of the 90-10 mixture. Estimates of the effects of isomeric impurity of isobutane are given in graphical form.

  19. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    365 29 3,734 1,930 3,700 8 55 3,685 284 5,743 Crude Oil 47 - - - - 875 395 5 91 1,093 139 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 318 0 9 83 -19 - - -49 44 35 361 Pentanes Plus 35 0 - - - 0 - - 1 7 1 24 Liquefied Petroleum Gases 283 - - 9 83 -18 - - -50 36 34 337 Ethane/Ethylene 111 - - 0 - -118 - - 6 - - -12 Propane/Propylene 118 - - 33 79 100 - - -52 - 30 352 Normal Butane/Butylene 37 - - -23 1 0 - - -4 23 4 -8 Isobutane/Isobutylene 17 - - -1 3 0 - - 1 14 0 5 Other Liquids - -

  20. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    ,519 948 4,459 2,809 -864 -155 -6 4,234 463 5,025 Crude Oil 1,756 - - - - 2,675 -476 -195 78 3,627 55 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 763 -20 59 103 -130 - - -173 104 297 547 Pentanes Plus 87 -20 - - 0 126 - - 16 11 214 -47 Liquefied Petroleum Gases 676 - - 59 103 -257 - - -189 93 83 594 Ethane/Ethylene 213 - - - - -75 - - -1 - 76 64 Propane/Propylene 306 - - 113 89 -130 - - -101 - 3 475 Normal Butane/Butylene 108 - - -53 8 -59 - - -86 44 5 42 Isobutane/Isobutylene 49 -

  1. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    1,033 13 625 311 -624 -4 18 593 10 733 Crude Oil 686 - - - - 292 -387 -11 4 575 0 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 347 0 12 15 -243 - - -3 19 7 107 Pentanes Plus 55 0 - - - -39 - - -1 5 5 7 Liquefied Petroleum Gases 292 - - 12 15 -205 - - -2 15 2 100 Ethane/Ethylene 83 - - - - -50 - - 0 - - 33 Propane/Propylene 133 - - 8 14 -96 - - -1 - - 61 Normal Butane/Butylene 52 - - 3 - -37 - - -3 7 2 11 Isobutane/Isobutylene 23 - - 1 1 -22 - - 1 7 - -6 Other Liquids - - 14 - - 2 7

  2. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    1,144 20 3,034 1,322 534 10 -90 2,858 384 2,914 Crude Oil 1,074 - - - - 1,113 129 -26 10 2,279 - 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 71 0 15 8 - - - -27 81 37 3 Pentanes Plus 34 0 - - - - - - 0 29 0 4 Liquefied Petroleum Gases 37 - - 15 8 - - - -27 52 37 -2 Ethane/Ethylene 0 - - - - - - - - - - 0 Propane/Propylene 12 - - 40 8 - - - -7 - 32 35 Normal Butane/Butylene 14 - - -29 - - - - -23 32 4 -29 Isobutane/Isobutylene 11 - - 4 - - - - 3 20 - -7 Other Liquids - - 21 - - 119

  3. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    1,070 15 662 340 -715 -21 10 637 18 686 Crude Oil 746 - - - - 326 -425 -28 9 602 8 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 323 0 13 10 -297 - - 1 20 7 21 Pentanes Plus 55 0 - - - -45 - - 0 6 5 -1 Liquefied Petroleum Gases 268 - - 13 10 -252 - - 1 14 2 22 Ethane/Ethylene 77 - - - - -76 - - 0 - - 1 Propane/Propylene 122 - - 9 9 -110 - - 0 - 0 29 Normal Butane/Butylene 50 - - 3 0 -40 - - 1 7 2 5 Isobutane/Isobutylene 19 - - 0 1 -25 - - 0 7 0 -13 Other Liquids - - 15 - - 1 16 -12 1

  4. table05.chp:Corel VENTURA

    Gasoline and Diesel Fuel Update (EIA)

    27 - 1,721 -65 -3 170 0 1,511 0 0 Natural Gas Liquids and LRGs ....... 27 18 40 - 153 -28 - 8 1 257 Pentanes Plus .................................. 3 - 0 - 0 (s) - 0 (s) 2 Liquefied Petroleum Gases .............. 24 18 40 - 153 -28 - 8 1 254 Ethane/Ethylene ............................ 8 0 0 - 0 0 - 0 0 8 Propane/Propylene ........................ 11 54 39 - 149 -8 - 0 1 261 Normal Butane/Butylene ............... 4 -27 1 - 3 -18 - 5 (s) -7 Isobutane/Isobutylene ................... 1 -9 0 - 0 -2

  5. LPG--a direct source of C/sub 3/-C/sub 4/ olefins

    SciTech Connect (OSTI)

    Pujado, P.R.; Berg, R.C.; Vora, B.V.

    1983-03-28

    This article describes the selective production of olefins by the catalytic dehydrogenation of the corresponding paraffins by means of UOP's Oleflex process. In this process, propylene can be obtained at about 85 mol % selectivity by the catalytic dehydrogenation of propane. Isobutylene can be obtained at selectivities in excess of 90 mol % from isobutane, and n-butenes (1-butene plus 2-butene) at about 80 mol % from n-butane. The availability of this technology, coupled with an abundant supply of LPG (C/sub 3/ and C/sub 4/ paraffins), opens new avenues for the selective production of propylene and butylenes.

  6. Support shape effect in metal oxide catalysis: ceria nanoshapes supported vanadia catalysts for oxidative dehydrogenation of iso-butane

    SciTech Connect (OSTI)

    Wu, Zili; Schwartz, Viviane; Li, Meijun; Rondinone, Adam Justin; Overbury, Steven {Steve} H

    2012-01-01

    The activation energy of VOx/CeO2 catalysts in oxidative dehydrogenation of iso-butane was found dependent on the shape of ceria support: rods < octahedra, closely related to the surface oxygen vacancy formation energy and defects amount of the two ceria supports with different crystallographic surface planes.

  7. Thermodynamic properties of isobutane-isopentane mixtures from -40 to +600/sup 0/F and up to 1000 psia

    SciTech Connect (OSTI)

    Gallagher, J.S.; Levelt Sengers, J.M.H.; Morrison, G.; Sengers, J.V.

    1984-07-01

    The Helmholtz function for pure isobutane from a recent correlation has been converted to a dimensionless form and a pressure-enthalpy chart based on this function has been generated by computer. A Helmholtz function for mixtures of isobutane and isopentane has been formed based upon the dimensionless isobutane Helmholtz function as the reference fluid by means of an extended corresponding-states principle. Scarce literature data for saturation properties of isopentane, and new data for its vapor pressure and for the critical line of the mixture were used. The accuracy of the surface was checked by comparing with literature enthalpy data and with new VLE data for the mixture. Tables of thermodynamic properties have been generated from this Helmholtz function for the 0.1 mole fraction isopentane-in-isobutane mixture in the single-phase region and on the dew- and bubble-point curves, together with properties of the coexisting phase. A pressure-enthalpy chart for this mixture has also been generated.

  8. EIA-800

    U.S. Energy Information Administration (EIA) Indexed Site

    Greater than 15 ppm to 500 ppm sulfur (incl.) 466 Greater than 500 ppm sulfur 467 Total 999 * Includes propane, propylene, ethane, ethylene, normal butane, butylene, isobutane, ...

  9. EIA-801

    U.S. Energy Information Administration (EIA) Indexed Site

    ... Residual Fuel Oil 511 Asphalt and Road Oil 931 Product Code PADD 1 Item Description * Includes ethane, ethylene, propane, propylene, normal butane, butylene, isobutane, ...

  10. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    12,704 1,095 19,893 9,401 343 434 18,855 4,750 19,396 Crude Oil 9,431 - - - - 7,351 136 252 16,207 458 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 3,273 -21 612 144 - - 60 516 967 2,465 Pentanes Plus 429 -21 - - 11 - - 0 146 182 91 Liquefied Petroleum Gases 2,844 - - 612 133 - - 60 369 785 2,375 Ethane/Ethylene 1,108 - - 6 0 - - -3 - 65 1,051 Propane/Propylene 1,117 - - 559 112 - - 51 - 615 1,121 Normal Butane/Butylene 324 - - 55 10 - - 12 169 98 110 Isobutane/Isobutylene 296 - - -7

  11. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    327 28 3,799 1,686 3,672 113 96 3,748 247 5,534 Crude Oil 50 - - - - 624 421 110 3 1,121 79 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 277 -1 39 46 -12 - - 3 35 45 267 Pentanes Plus 32 -1 - - 0 0 - - 0 2 2 28 Liquefied Petroleum Gases 245 - - 39 46 -12 - - 2 33 43 239 Ethane/Ethylene 84 - - 0 - -87 - - 0 - - -2 Propane/Propylene 110 - - 37 41 76 - - 3 - 38 223 Normal Butane/Butylene 36 - - 2 1 0 - - -1 23 6 11 Isobutane/Isobutylene 14 - - -1 4 0 - - 0 10 0 7 Other Liquids - - 29 -

  12. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    569 926 4,517 2,414 -489 17 125 4,312 433 5,082 Crude Oil 1,872 - - - - 2,305 -411 -17 109 3,561 79 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 696 -19 112 70 -45 - - 6 92 253 463 Pentanes Plus 88 -19 - - 0 127 - - 2 18 172 3 Liquefied Petroleum Gases 608 - - 112 70 -172 - - 4 73 81 460 Ethane/Ethylene 191 - - 0 0 -27 - - 2 - 65 98 Propane/Propylene 274 - - 112 57 -122 - - -2 - 4 318 Normal Butane/Butylene 94 - - 2 7 -26 - - 4 27 12 33 Isobutane/Isobutylene 48 - - -1 6 4 - - 0 46 0

  13. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    7,605 102 7,850 3,587 -2,995 123 193 7,261 3,647 5,172 Crude Oil 5,695 - - - - 2,974 261 -1 114 8,531 284 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 1,910 -1 398 13 354 - - 51 299 625 1,699 Pentanes Plus 223 -1 - - 11 -81 - - -3 96 1 58 Liquefied Petroleum Gases 1,687 - - 398 2 435 - - 54 204 624 1,641 Ethane/Ethylene 755 - - 5 - 190 - - -4 - - 955 Propane/Propylene 599 - - 360 0 156 - - 52 - 551 512 Normal Butane/Butylene 131 - - 40 2 67 - - 6 86 66 81 Isobutane/Isobutylene 202 -

  14. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    1,134 24 3,064 1,374 527 110 10 2,897 404 2,923 Crude Oil 1,068 - - - - 1,122 153 72 16 2,391 8 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 66 0 50 6 0 - - 0 71 36 16 Pentanes Plus 30 0 - - 0 - - - 0 25 2 3 Liquefied Petroleum Gases 36 - - 50 6 0 - - 0 46 34 13 Ethane/Ethylene 0 - - - - - - - - - - 0 Propane/Propylene 12 - - 41 5 - - - -2 - 22 39 Normal Butane/Butylene 12 - - 7 0 - - - 2 25 12 -20 Isobutane/Isobutylene 11 - - 3 0 0 - - 0 21 0 -6 Other Liquids - - 24 - - 114 314 15 3

  15. Injection of LPG into TCC unit

    SciTech Connect (OSTI)

    Chou, T.S.

    1987-02-03

    A process is described for catalytically cracking hydrocarbon feed in a bed of catalyst effective to crack the hydrocarbon feed, comprising contacting the feed under catalytic cracking conditions, with the catalyst in a first portion of the bed, to produce cracked product. Another portion of that bed of catalyst is sealed by introducing into another portion of that bed a seal selected from the group consisting of ethane, propane, butane, isobutane, ethylene, propylene, butylene, isobutylene and mixtures thereof whereby feed and cracked product are prevented from surging into another portion; whereby contact of the seal with catalyst in another portion of the bed results in conversion of the seal to the higher molecular weight adducts thereof, the condition in another portion of the bed being effective to provide the conversion.

  16. Development of a catalyst for conversion of syngas-derived materials to isobutylene. Quarterly report number 19, October 1--December 31, 1995

    SciTech Connect (OSTI)

    Spehlmann, B.C.

    1996-07-01

    The goals of this project are to develop a catalyst and process for the conversion of syngas to isobutanol. After identification and optimization of key catalyst and process characteristics, the commercial potential of the process is to be evaluated by an economic analysis. From independent process variable studies to investigate the conversion of a methanol/ethanol feed to isobutanol, the best performance to date has been achieved with the 2% Pt on Zn/Mn/Zr oxide catalyst. Using Hyprotech Hysim v2.5 process simulation software, and considering both gas and liquid recycle loops in the process flow diagram, the overall carbon conversion is 98% with 22% selectivity to isobutanol. The expected production of isobutanol is 92 MT/day from 500 MT/day of methanol and 172 MT/day of ethanol feed. An additional 13 MT/day of isobutryaldehyde intermediate is recovered in the liquid product and vent streams. Because of the low selectivity (22%) of the methanol conversion catalyst to isobutanol, the process is uneconomical, even if the isobutanol is valued as a solvent ($903/MT) and not as isobutylene for MTBE production ($352/MT).

  17. U.S. Product Supplied for Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    IsobutaneIsobutylene 75 107 102 109 108 83 1981-2016 Other Liquids -90 -138 36 73 -20 185 1981-2016 HydrogenOxygenatesRenewables Other Hydrocarbons 0 0 0 0 0 0 1991-2016 ...

  18. U.S. Exports of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    Pentanes Plus 234 153 201 170 199 223 1984-2016 Liquefied Petroleum Gases 903 817 857 898 ... IsobutaneIsobutylene 5 10 7 5 5 5 1984-2016 Other Liquids 509 466 552 683 571 546 ...

  19. untitled

    Annual Energy Outlook [U.S. Energy Information Administration (EIA)]

    741 317 267 1,325 IsobutaneIsobutylene 206 7 213 155 55 170 380 Other HydrocarbonsHydrogenOxygenates 512 0 512 29 18 0 47 Other HydrocarbonsHydrogen 0 0 0 28 0 0 28...

  20. PSA Vol 1 Tables Revised Ver 2 Print.xls

    Gasoline and Diesel Fuel Update (EIA)

    741 317 245 1,303 IsobutaneIsobutylene 206 7 213 155 55 184 394 Other HydrocarbonsHydrogenOxygenates 512 0 512 29 18 0 47 Other HydrocarbonsHydrogen 0 0 0 28 0 0 28...

  1. untitled

    Gasoline and Diesel Fuel Update (EIA)

    1,361 415 768 2,544 IsobutaneIsobutylene 151 4 155 99 62 164 325 Other HydrocarbonsHydrogenOxygenates 553 0 553 20 28 0 48 Other HydrocarbonsHydrogen 0 0 0 19 0 0 19...

  2. Crude Oil and Petroleum Products Total Stocks Stocks by Type

    U.S. Energy Information Administration (EIA) Indexed Site

    Stocks by Type Product: Crude Oil and Petroleum Products Crude Oil All Oils (Excluding Crude Oil) Pentanes Plus Liquefied Petroleum Gases Ethane/Ethylene Propane/Propylene Normal Butane/Butylene Isobutane/Butylene Other Hydrocarbons Oxygenates (excluding Fuel Ethanol) MTBE Other Oxygenates Renewables (including Fuel Ethanol) Fuel Ethanol Renewable Diesel Fuel Other Renewable Fuels Unfinished Oils Unfinished Oils, Naphthas & Lighter Unfinished Oils, Kerosene & Light Gas Unfinished Oils,

  3. U.S. Total Stocks

    U.S. Energy Information Administration (EIA) Indexed Site

    Pentanes Plus 12,510 17,596 12,739 14,471 20,608 20,543 1981-2015 Liquefied Petroleum ... Normal ButaneButylene 27,652 26,779 28,574 30,288 33,230 37,509 1981-2015 Isobutane...

  4. Transport of Injected Isobutane by Thermal Groundwater in Long...

    Open Energy Info (EERE)

    understanding of water-rock interaction. For example, new uses of isotopes have led to novel interpretations of the evolution of fluid and rock chemistry over time. New modelling...

  5. Dehydrogenation links LPG to more octanes

    SciTech Connect (OSTI)

    Gussow, S.; Spence, D.C.; White, E.A.

    1980-01-01

    Air Products and Chemicals Inc.'s Houdry Catofin process, a new application of well-known Houdry catalytic dehydrogenation technology, is an adiabatic, fixed-bed, multireactor catalytic process which produces propylene, isobutylene, and mixed n-butylenes by dehydrogenation of the corresponding saturates. The process is very flexible in that propylene, isobutylene, and mixed n-butylenes can be produced either separately or simultaneously from the corresponding saturates. The process will be used to prepare purity propylene at a Morelos, Mex., plant, which is now in the engineering stage. Five variations of the procedure for producing propylene; methyl tert.-butyl ether; propylene and alkylate; methyl tert.-butyl ether and alkylate; and methyl tert.-butyl ether, alkylate, and 1-butylene are compared with respect to typical product yields, costs and values for process economics, the dehydrogenation route to the three products, manufacturing costs, the sensitivity of return on investment to feedstock costs, and the return on investment, which varies from a low of 11.5% for the third case to a high of 14.4% for the fourth case. The Catofin process is discussed.

  6. Experimental and DFT studies of initiation processes for butane isomerization over sulfated-zirconia catalysts

    SciTech Connect (OSTI)

    Hong, Z.; Watwe, R.M.; Natal-Santiago, M.A.; Hill, J.M.; Dumesic, J.A.; Fogash, K.B.; Kim, B.; Masqueda-Jimenez, B.I.

    1998-09-10

    Reaction kinetics studies were conducted of isobutane and n-butane isomerization at 423 K over sulfated-zirconia, with the butane feeds purified of olefins. Dihydrogen evolution was observed during butane isomerization over fresh catalysts, as well as over catalysts selectively poisoned by preadsorbed ammonia. Butane isomerization over sulfated-zirconia can be viewed as a surface chain reaction comprised of initiation, propagation, and termination steps. The primary initiation step in the absence of feed olefins is considered to be the dehydrogenation of butane over sulfated-zirconia, generating butenes which adsorb onto acid sites to form protonated olefinic species associated with the conjugate base form of the acid sites. Quantum-chemical calculations, employing density-functional theory, suggest that the dissociative adsorption of dihydrogen, isobutylene hydrogenation, and dissociative adsorption of isobutane are feasible over the sulfated-zirconia cluster, and these reactions take place over Zr-O sites.

  7. U.S. Natural Gas Processing Plant

    U.S. Energy Information Administration (EIA) Indexed Site

    All Oils (Excluding Crude Oil) 6,877 6,774 5,691 4,837 5,272 5,252 1993-2016 Pentanes Plus 728 852 804 780 780 727 1993-2016 Liquefied Petroleum Gases 6,149 5,922 4,887 4,057 4,492 4,525 1993-2016 Ethane/Ethylene 1,243 1,336 1,311 819 1,017 828 1993-2016 Propane/Propylene 1,843 1,671 1,598 1,677 2,216 2,185 1993-2016 Normal Butane/Butylene 2,529 2,411 1,701 1,160 712 1,000 1993-2016 Isobutane/Butylene 534 504 277 401 547 512

  8. Table Definitions, Sources, and Explanatory Notes

    Gasoline and Diesel Fuel Update (EIA)

    Natural Gas Plant Net Stocks Definitions Key Terms Definition Barrel A unit of volume equal to 42 U.S. gallons. Butylene (C4H8) An olefinic hydrocarbon recovered from refinery processes. Ethane (C2H6) A normally gaseous straight-chain hydrocarbon. It is a colorless paraffinic gas that boils at a temperature of -127.48º F. It is extracted from natural gas and refinery gas streams. Isobutane (C4H10) A normally gaseous branch-chain hydrocarbon. It is a colorless paraffinic gas that boils at a

  9. From PADD 1 to PADD 2 Movements of Crude Oil by Rail

    Gasoline and Diesel Fuel Update (EIA)

    2010 2011 2012 2013 2014 2015 View History Crude Oil and Petroleum Products 110,859 111,081 109,179 110,752 136,352 148,001 1985-2015 Crude Oil 0 0 1,352 1,629 2,423 1,821 1985-2015 Petroleum Products 110,859 111,081 107,827 109,123 133,929 146,180 1981-2015 Pentanes Plus 452 113 19 2 30 121 2009-2015 Liquefied Petroleum Gases 0 0 0 236 23,034 33,098 1981-2015 Ethane/Ethylene 236 22,845 32,344 2013-2015 Propane/Propylene 0 0 0 0 135 538 2005-2015 Isobutane/Isobutylene 0 0 0 39 156 2008-2015

  10. From PADD 1 to PADD 2 Movements by Pipeline

    U.S. Energy Information Administration (EIA) Indexed Site

    Sep-15 Oct-15 Nov-15 Dec-15 Jan-16 Feb-16 View History Crude Oil and Petroleum Products 12,645 13,446 13,070 11,827 13,128 11,470 1986-2016 Crude Oil 121 152 113 126 115 90 1986-2016 Petroleum Products 12,524 13,294 12,957 11,701 13,013 11,380 1986-2016 Pentanes Plus 11 10 10 11 10 10 2009-2016 Liquefied Petroleum Gases 2,828 2,956 3,262 3,331 3,947 3,528 1986-2016 Ethane/Ethylene 2,766 2,893 3,200 3,269 3,884 3,465 2013-2016 Propane/Propylene 44 45 44 44 45 45 2005-2016 Isobutane/Isobutylene 13

  11. Gasoline and Diesel Fuel Update

    Gasoline and Diesel Fuel Update (EIA)

    Sep-15 Oct-15 Nov-15 Dec-15 Jan-16 Feb-16 View History Crude Oil and Petroleum Products 12,645 13,446 13,070 11,827 13,128 11,470 1986-2016 Crude Oil 121 152 113 126 115 90 1986-2016 Petroleum Products 12,524 13,294 12,957 11,701 13,013 11,380 1986-2016 Pentanes Plus 11 10 10 11 10 10 2009-2016 Liquefied Petroleum Gases 2,828 2,956 3,262 3,331 3,947 3,528 1986-2016 Ethane/Ethylene 2,766 2,893 3,200 3,269 3,884 3,465 2013-2016 Propane/Propylene 44 45 44 44 45 45 2005-2016 Isobutane/Isobutylene 13

  12. Selective oxidation of alkanes and/or alkenes to valuable oxygenates

    DOE Patents [OSTI]

    Lin, Manhua; Pillai, Krishnan S.

    2011-02-15

    A catalyst, its method of preparation and its use for producing at least one of methacrolein and methacrylic acid, for example, by subjecting isobutane or isobutylene or a mixture thereof to a vapor phase catalytic oxidation in the presence of air or oxygen. In the case where isobutane alone is subjected to a vapor phase catalytic oxidation in the presence of air or oxygen, the product is at least one of isobutylene, methacrolein and methacrylic acid. The catalyst comprises a compound having the formula A.sub.aB.sub.bX.sub.xY.sub.yZ.sub.zO.sub.o wherein A is one or more elements selected from the group of Mo, W and Zr, B is one or more elements selected from the group of Bi, Sb, Se, and Te, X is one or more elements selected from the group of Al, Bi, Ca, Ce, Co, Fe, Ga, Mg, Ni, Nb, Sn, W and Zn, Y is one or more elements selected from the group of Ag, Au, B, Cr, Cs, Cu, K, La, Li, Mg, Mn, Na, Nb, Ni, P, Pb, Rb, Re, Ru, Sn, Te, Ti, V and Zr, and Z is one or more element from the X or Y groups or from the following: As, Ba, Pd, Pt, Sr, or mixtures thereof, and wherein a=1, 0.05

  13. U.S. Imports of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    11,793 11,436 10,598 9,859 9,241 9,401 1973-2015 Crude Oil 9,213 8,935 8,527 7,730 7,344 7,351 1910-2015 Natural Gas Plant Liquids and Liquefied Refinery Gases 179 183 170 182 143 144 1983-2015 Pentanes Plus 26 48 29 34 14 11 1983-2015 Liquefied Petroleum Gases 153 135 141 148 128 133 1973-2015 Ethane 1993-2007 Ethylene 0 0 0 0 0 0 1993-2015 Propane 93 82 85 103 89 93 1995-2015 Propylene 29 28 31 24 19 19 1993-2015 Normal Butane 12 8 9 6 7 6 1995-2015 Butylene 9 7 6 5 6 4 1993-2015 Isobutane 10

  14. Development of a catalyst for conversion of syngas-derived materials to isobutylene. Quarterly report No. 10, July 1, 1993--September 30, 1993

    SciTech Connect (OSTI)

    Barger, P.T.

    1993-12-31

    Two types of basic metal oxide co-catalysts have been evaluated in combination with CU/Zn/Al oxide methanol synthesis catalyst for the production of isoalcohols, KOH on Al{sub 2}O{sub 3} or SiO{sub 2} and alkali metal impregnated Mg/Al MOSSs. Catalytic performance with the K/Al{sub 2}O{sub 3} co-catalyst is virtually identical to that of the SiO{sub 2} blank, indicating that this material is inert. In contrast, the K/SiO{sub 2} co-catalyst actually reduces the activity and selectivity of the Cu/Zn/Al methanol synthesis catalyst. Therefore, this approach has been abandoned. Previous testing of Mg/Al MOSS co-catalysts has shown promotion of DME, rather than isoalcohols, presumably by methanol, dehydration on residual acid sites. Addition of 0.2--0.3 wt % alkali (Na, K, and Cs) to the Mg/Al MOSS is not effective for reducing the formation of DME. Attempts to produce isobutanol with Pd/K on Zr/Zn/Mn oxide catalysts, similar to those described by Keim and coworkers, at low pressure conditions have been successful. Catalysts were prepared by the impregnation of Pd (0.15 wt %) from either PdCl{sub 2} or Pd(NO{sub 3}){sub 2} preformed K/Zr/Zn/Mn oxide. Materials with two levels of K were also prepared. All of these catalyst show only low activity for syngas to alcohols, with methanol as the only alcohol product. The primary products in these tests are C{sub l--4} hydrocarbons. Blank reactor testing has demonstrated that a substantial portion of the light hydrocarbons produced in these 450{degrees}C tests are due to reactions on the stainless steel reactor walls and quartz reactor packing material. Attempts to reduce the extent of these side reactions by the use of a porcelain-lined reactor have been unsuccessful.

  15. Thermophysical properties of working fluids for binary geothermal cycles. Final report

    SciTech Connect (OSTI)

    Diller, D.E.; Gallagher, J.S.; Kamgar-Parsi, B.; Morrison, G.; Levelt Sengers, J.M.H.; Sengers, J.V.; Van Poolen, L.J.; Waxman, M.

    1984-07-01

    The following are presented: thermodynamic properties of isobutane and isobutane-isopentane mixtures; a scaled fundamental equation for mixtures of isobutane and isopentane near gas-liquid critical line; and viscosities of hydrocarbons and their mixtures. (MHR)

  16. ORGANIC SPECIES IN GEOTHERMAL WATERS IN LIGHT OF FLUID INCLUSION...

    Open Energy Info (EERE)

    that indicate H2 concentrations > 0.001 mol % typically have ethane > ethylene, propane > propylene, and butane > butylene. There are three end member fluid compositions:...

  17. Fluid Inclusion Analysis At Coso Geothermal Area (2003) | Open...

    Open Energy Info (EERE)

    that indicate H2 concentrations > 0.001 mol % typically have ethane > ethylene, propane > propylene, and butane > butylene. There are three end member fluid compositions...

  18. untitled

    Annual Energy Outlook [U.S. Energy Information Administration (EIA)]

    The principal constituents are methane, ethane, ethylene, normal butane, butylene, propane, propylene, etc. Still gas is used as a refinery fuel and a petrochemical...

  19. MICROMEGAS: High rate and radiation hardness results

    SciTech Connect (OSTI)

    Puill, G.; Derre, J.; Giomataris, Y.; Rebourgeard, P.

    1999-12-01

    In this report, the authors present results of gain studies using various gas mixtures in a novel structure of gaseous detector called MICROMEGAS which is under development at Saclay. The authors in particular studied the maximum of gain achievable with MICROMEGAS before the discharge. They tried various gas mixtures (Argon, Neon, CF{sub 4}) with various proportions of quencher (Isobutane, Cyclohexane, DME). They also studied the radiation hardness of MICROMEGAS using Argon-Isobutane and CF{sub 4}-Isobutane mixtures.

  20. Chemical Kinetics of Combustion Processes

    Broader source: All U.S. Department of Energy (DOE) Office Webpages (Extended Search)

    Combustion (work-in-progress) * Chemical kinetic submodel of iso-butanol ... oxidation of isobutane and isobutene. * Chemical kinetic submodel of iso-butanol ...

  1. Natural Gas Plant Stocks of Natural Gas Liquids

    Annual Energy Outlook [U.S. Energy Information Administration (EIA)]

    Product: Natural Gas Liquids Pentanes Plus Liquefied Petroleum Gases Ethane Propane Normal Butane Isobutane Period: Monthly Annual Download Series History Download Series History...

  2. CRF

    Broader source: All U.S. Department of Energy (DOE) Office Webpages (Extended Search)

    ... Permalink New Conceptual Insights into Diesel Engine Fuel-Injection Processes Capabilities, ... reactions: Product formation in low-temperature isobutane oxidation" by Arkke Eskola, ...

  3. U.S. Energy Information Administration (EIA)

    Gasoline and Diesel Fuel Update (EIA)

    to 12.10 per MMBtu, and isobutane, which rose by 1.6% to 14.61 per MMBtu. more summary data PricesDemandSupply: Natural gas prices dipped during the weekend due to cooler...

  4. Word Pro - Untitled1

    U.S. Energy Information Administration (EIA) Indexed Site

    Thousand Barrels per Day Plus Butane Isobutane Normal Butane Propane 1950 1955 1960 1965 1970 1975 1980 1985 1990 1995 2000 2005 2010 0 300 600 900 1,200 Thousand Barrels per Day ...

  5. Direct contact, binary fluid geothermal boiler

    DOE Patents [OSTI]

    Rapier, Pascal M.

    1982-01-01

    Energy is extracted from geothermal brines by direct contact with a working fluid such as isobutane which is immiscible with the brine in a geothermal boiler. The geothermal boiler provides a distributor arrangement which efficiently contacts geothermal brine with the isobutane in order to prevent the entrainment of geothermal brine in the isobutane vapor which is directed to a turbine. Accordingly the problem of brine carry-over through the turbine causes corrosion and scaling thereof is eliminated. Additionally the heat exchanger includes straightening vanes for preventing startup and other temporary fluctuations in the transitional zone of the boiler from causing brine carryover into the turbine. Also a screen is provided in the heat exchanger to coalesce the working fluid and to assist in defining the location of the transitional zone where the geothermal brine and the isobutane are initially mixed.

  6. Direct contact, binary fluid geothermal boiler

    DOE Patents [OSTI]

    Rapier, P.M.

    1979-12-27

    Energy is extracted from geothermal brines by direct contact with a working fluid such as isobutane which is immiscible with the brine in a geothermal boiler. The geothermal boiler provides a distributor arrangement which efficiently contacts geothermal brine with the isobutane in order to prevent the entrainment of geothermal brine in the isobutane vapor which is directed to a turbine. Accordingly the problem of brine carryover through the turbine causing corrosion and scaling thereof is eliminated. Additionally the heat exchanger includes straightening vanes for preventing startup and other temporary fluctuations in the transitional zone of the boiler from causing brine carryover into the turbine. Also a screen is provided in the heat exchanger to coalesce the working fluid and to assist in defining the location of the transitional zone where the geothermal brine and the isobutane are initially mixed.

  7. Compound and Elemental Analysis At Long Valley Caldera Geothermal...

    Open Energy Info (EERE)

    from locations west and east of the plant revealed the presence of isobutane related to plant operations. The 13C values of diffuse CO2 range from - 5.7 to - 3.4, similar...

  8. Carbon Dioxide Emissions From Vegetation-Kill Zones Around The...

    Open Energy Info (EERE)

    from locations west and east of the plant revealed the presence of isobutane related to plant operations. The 13C values of diffuse CO2 range from - 5.7 to - 3.4, similar...

  9. Gas Flux Sampling At Long Valley Caldera Geothermal Area (Bergfeld...

    Open Energy Info (EERE)

    from locations west and east of the plant revealed the presence of isobutane related to plant operations. The 13C values of diffuse CO2 range from - 5.7 to - 3.4, similar...

  10. U.S. Energy Information Administration (EIA)

    Annual Energy Outlook [U.S. Energy Information Administration (EIA)]

    butane, and isobutane rose 2.2%, 3.0%, and 3.2%, respectively, while the prices of propane and ethane fell by 0.4% and 3.2%, respectively. more summary data PricesDemand...

  11. untitled

    Annual Energy Outlook [U.S. Energy Information Administration (EIA)]

    -109 -12 Isobutylene 7 0 7 0 0 0 0 Finished Motor Gasoline 21,280 1,066 22,346 25,478 3,607 12,672 41,757 Reformulated 11,460 0 11,460 0 0 0 0 Reformulated Blended with Ether...

  12. Normal butane/iso-butane separation

    SciTech Connect (OSTI)

    Volles, W.K.; Cusher, N.A.

    1986-08-26

    This patent describes an improved pressure swing adsorption process for the separation of iso-butane from normal butane in an adsorption system having at least three adsorbent beds, each bed of which undergoes, on a cyclic basis and a processing sequence comprising: introducing a feed gas mixture of iso-butane and normal butane at an upper adsorption pressure to the feed end of the bed capable of selectively adsorbing normal butane as the more selectivity adsorbable component of the gas mixture. The iso-butane as the less readily adsorbable component passes through the bed and is discharged from the discharge end. The feed gas introduction is continued as a normal butane adsorption front is formed in the bed and passes through the bed from the feed end and breaks through at the discharge end of the bed, a portion of the iso-butane effluent stream thus discharged being diverted for passage as purge gas to another bed in the system; and countercurrently depressurizing the bed with release of gas from the feed end.

  13. Catalytic oxidation of light alkanes in presence of a base

    DOE Patents [OSTI]

    Bhinde, M.V.; Bierl, T.W.

    1998-03-03

    The presence of a base in the reaction mixture in a metal-ligand catalyzed partial oxidation of alkanes results in sustained catalyst activity, and in greater percent conversion as compared with oxidation in the absence of base, while maintaining satisfactory selectivity for the desired oxidation, for example the oxidation of isobutane to isobutanol. 1 fig.

  14. Catalytic oxidation of light alkanes in presence of a base

    DOE Patents [OSTI]

    Bhinde, Manoj V.; Bierl, Thomas W.

    1998-01-01

    The presence of a base in the reaction mixture in a metal-ligand catalyzed partial oxidation of alkanes results in sustained catalyst activity, and in greater percent conversion as compared with oxidation in the absence of base, while maintaining satisfactory selectivity for the desired oxidation, for example the oxidation of isobutane to isobutanol.

  15. Roaming radical pathways for the decomposition of alkanes.

    SciTech Connect (OSTI)

    Harding, L. B.; Klippenstein, S. J.

    2010-01-01

    CASPT2 calculations predict the existence of roaming radical pathways for the decomposition of propane, n-butane, isobutane and neopentane. The roaming radical paths lead to the formation of an alkane and an alkene instead of the expected radical products. The predicted barriers for the roaming radical paths lie {approx}1 kcal/mol below the corresponding radical asymptotes.

  16. War against water

    SciTech Connect (OSTI)

    Fitz-Hugh, S.

    1982-01-01

    It is stressed that waterproofing should be the most important concern in an earth-sheltered home, starting with the design and continuing throughout the construction. Damage which may be caused by water leakage is discussed. Proper site selection is most important and the need for outside professionals and consultants is emphasized. The ideal waterproofing system is discussed and illustrated. Waterproofing agents are discussed in detail. They are: (1) sodium bentonite; (2) elastomers, such as isobutylene isoprene (butyl rubber), EPDM (ethylene propylene diene monomer), and liquid elastomers (polyurethanes); and (3) rubberized asphalt. Availability, sheet sizes and application of these waterproofing agents are discussed. (MJJ)

  17. Total

    U.S. Energy Information Administration (EIA) Indexed Site

    Product: Total Crude Oil Liquefied Petroleum Gases Propane/Propylene Normal Butane/Butylene Other Liquids Oxygenates Fuel Ethanol MTBE Other Oxygenates Biomass-based Diesel Other Renewable Diesel Fuel Other Renewable Fuels Gasoline Blending Components Petroleum Products Finished Motor Gasoline Reformulated Gasoline Conventional Gasoline Kerosene-Type Jet Fuel Kerosene Distillate Fuel Oil Distillate Fuel Oil, 15 ppm Sulfur and Under Distillate Fuel Oil, Greater than 15 ppm to 500 ppm Sulfur

  18. Refinery Capacity Report

    U.S. Energy Information Administration (EIA) Indexed Site

    State/Refiner/Location Alkylates Aromatics Isobutane Lubricants Isomers Isopentane and Isohexane Asphalt and Road Oil Marketable Petroleum Coke Hydrogen (MMcfd) Sulfur (short tons per day) Table 4. Production Capacity of Operable Petroleum Refineries by State as of January 1, 2015 (Barrels per Stream Day, Except Where Noted) Isooctane a ..................................................................... Alabama 0 0 15,000 711 3,500 0 7,120 33 245 0 Hunt Refining Co 0 0 15,000 0 3,500 0 7,120

  19. Weak interactions between water and clathrate-forming gases at low pressures

    DOE Public Access Gateway for Energy & Science Beta (PAGES Beta)

    Thürmer, Konrad; Yuan, Chunqing; Kimmel, Greg A.; Kay, Bruce D.; Smith, R. Scott

    2015-07-17

    Using scanning probe microscopy and temperature programed desorption we examined the interaction between water and two common clathrate-forming gases, methane and isobutane, at low temperature and low pressure. Water co-deposited with up to 10–1 mbar methane or 10–5 mbar isobutane at 140 K onto a Pt(111) substrate yielded pure crystalline ice, i.e., the exposure to up to ~ 107 gas molecules for each deposited water molecule did not have any detectable effect on the growing films. Exposing metastable, less than 2 molecular layers thick, water films to 10–5 mbar methane does not alter their morphology, suggesting that the presence ofmore » the Pt(111) surface is not a strong driver for hydrate formation. This weak water–gas interaction at low pressures is supported by our thermal desorption measurements from amorphous solid water and crystalline ice where 1 ML of methane desorbs near ~ 43 K and isobutane desorbs near ~ 100 K. As a result, similar desorption temperatures were observed for desorption from amorphous solid water.« less

  20. Catalytic conversion of light alkanes. Final report, January 1, 1990--October 31, 1994

    SciTech Connect (OSTI)

    1998-12-31

    During the course of the first three years of the Cooperative Agreement (Phase I-III), we uncovered a family of metal perhaloporphyrin complexes which had unprecedented activity for the selective air-oxidation of fight alkanes to alcohols. The reactivity of fight hydrocarbon substrates with air or oxygen was in the order: isobutane>propane>ethane>methane, in accord with their homolytic bond dissociation energies. Isobutane was so reactive that the proof-of concept stage of a process for producing tert-butyl alcohol from isobutane was begun (Phase V). It was proposed that as more active catalytic systems were developed (Phases IV, VI), propane, then ethane and finally methane oxidations will move into this stage (Phases VII through IX). As of this writing, however, the program has been terminated during the later stages of Phases V and VI so that further work is not anticipated. We made excellent progress during 1994 in generating a class of less costly new materials which have the potential for high catalytic activity. New routes were developed for replacing costly perfluorophenyl groups in the meso-position of metalloporphyrin catalysts with far less expensive and lower molecular weight perfluoromethyl groups.

  1. Binary module test. Final report

    SciTech Connect (OSTI)

    Schilling, J.R.; Colley, T.C.; Pundyk, J.

    1980-12-01

    The objective of this project was to design and test a binary loop module representative of and scaleable to commercial size units. The design was based on state-of-the-art heat exchanger technology, and the purpose of the tests was to confirm performance of a supercritical boiling cycle using isobutane and a mixture of isobutane and isopentane as the secondary working fluid. The module was designed as one percent of a 50 MW unit. It was installed at Magma Power's East Mesa geothermal field and tested over a period of approximately 4 months. Most of the test runs were with isobutane but some data were collected for hydrocarbon mixtures. The results of the field tests are reported. In general these results indicate reasonably good heat balances and agreement with overall heat transfer coefficients calculated by current stream analysis methods and available fluid property data; however, measured pressure drops across the heat exchangers were 20 percent higher than estimated. System operation was stable under all conditions tested.

  2. Weak interactions between water and clathrate-forming gases at low pressures

    SciTech Connect (OSTI)

    Thurmer, Konrad; Yuan, Chunqing; Kimmel, Gregory A.; Kay, Bruce D.; Smith, R. Scott

    2015-11-01

    Using scanning probe microscopy and temperature programed desorption we examined the interaction between water and two common clathrate-forming gases, methane and isobutane, at low temperature and low pressure. Water co-deposited with up to 10-1 mbar methane or 10-5 mbar isobutane at 140 K onto a Pt(111) substrate yielded pure crystalline ice, i.e., the exposure to up to ~107 gas molecules for each deposited water molecule did not have any detectable effect on the growing films. Exposing metastable, less than 2 molecular layers thick, water films to 10-5 mbar methane does not alter their morphology, suggesting that the presence of the Pt(111) surface is not a strong driver for hydrate formation. This weak water-gas interaction at low pressures is supported by our thermal desorption measurements from amorphous solid water and crystalline ice where 1 ML of methane desorbs near ~43 K and isobutane desorbs near ~100 K. Similar desorption temperatures were observed for desorption from amorphous solid water.

  3. Weak interactions between water and clathrate-forming gases at low pressures

    SciTech Connect (OSTI)

    Thürmer, Konrad; Yuan, Chunqing; Kimmel, Greg A.; Kay, Bruce D.; Smith, R. Scott

    2015-07-17

    Using scanning probe microscopy and temperature programed desorption we examined the interaction between water and two common clathrate-forming gases, methane and isobutane, at low temperature and low pressure. Water co-deposited with up to 10–1 mbar methane or 10–5 mbar isobutane at 140 K onto a Pt(111) substrate yielded pure crystalline ice, i.e., the exposure to up to ~ 107 gas molecules for each deposited water molecule did not have any detectable effect on the growing films. Exposing metastable, less than 2 molecular layers thick, water films to 10–5 mbar methane does not alter their morphology, suggesting that the presence of the Pt(111) surface is not a strong driver for hydrate formation. This weak water–gas interaction at low pressures is supported by our thermal desorption measurements from amorphous solid water and crystalline ice where 1 ML of methane desorbs near ~ 43 K and isobutane desorbs near ~ 100 K. As a result, similar desorption temperatures were observed for desorption from amorphous solid water.

  4. table09.chp:Corel VENTURA

    Gasoline and Diesel Fuel Update (EIA)

    3,434 - 5,080 -9 -1,729 230 0 6,546 0 0 Natural Gas Liquids and LRGs ....... 1,272 347 65 - -68 -208 - 229 29 1,566 Pentanes Plus .................................. 188 - 33 - -5 30 - 66 0 119 Liquefied Petroleum Gases .............. 1,084 347 31 - -63 -238 - 163 29 1,446 Ethane/Ethylene ........................... 503 24 18 - 112 -52 - 0 0 709 Propane/Propylene ....................... 363 301 4 - -158 -120 - 0 21 610 Normal Butane/Butylene .............. 76 3 6 - -11 -89 - 100 8 54

  5. table10.chp:Corel VENTURA

    Gasoline and Diesel Fuel Update (EIA)

    1,049 - 6,332 1,608 -4,050 -23 0 14,962 0 0 12,816 Natural Gas Liquids and LRGs ......... 4,049 -11 536 - -2,893 -15 - 595 6 1,095 1,354 Pentanes Plus ................................... 771 - 112 - -352 -8 - 163 5 371 219 Liquefied Petroleum Gases ............... 3,278 -11 424 - -2,541 -7 - 432 (s) 725 1,135 Ethane/Ethylene ............................ 950 0 0 - -1,270 0 - 0 0 -320 213 Propane/Propylene ....................... 1,473 284 233 - -705 -50 - 0 (s) 1,335 439 Normal Butane/Butylene

  6. Composites structures for bone tissue reconstruction

    SciTech Connect (OSTI)

    Neto, W.; Santos, João; Avérous, L.; Schlatter, G.; Bretas, Rosario

    2015-05-22

    The search for new biomaterials in the bone reconstitution field is growing continuously as humane life expectation and bone fractures increase. For this purpose, composite materials with biodegradable polymers and hydroxyapatite (HA) have been used. A composite material formed by a film, nanofibers and HA has been made. Both, the films and the non-woven mats of nanofibers were formed by nanocomposites made of butylene adipate-co-terephthalate (PBAT) and HA. The techniques used to produce the films and nanofibers were spin coating and electrospinning, respectively. The composite production and morphology were evaluated. The composite showed an adequate morphology and fibers size to be used as scaffold for cell growth.

  7. Low-temperature superacid catalysis: Reactions of n-butane catalyzed by iron- and manganese-promoted sulfated zirconia

    SciTech Connect (OSTI)

    Cheung, T.K.; D`Itri, J.L.; Gates, B.C.

    1995-02-01

    Environmental concerns are leading to the replacement of aromatic hydrocarbons in gasoline with high-octane-number branched paraffins and oxygenated compounds such as methyl t-butyl ether, which is produced from methanol and isobutylene. The latter can be formed from n-butane by isomerization followed by dehydrogenation. To meet the need for improved catalysts for isomerization of n-butane and other paraffins, researchers identified solid acids that are noncorrosive and active at low temperatures. Sulfated zirconia catalyzes the isomerization of n-butane even at 25{degrees}C, and the addition of Fe and Mn promoters increases its activity by three orders of magnitude. Little is known about this new catalyst. Here the authors provide evidence of its performance for n-butane conversion, demonstrating that isomerization is accompanied by disproportionation and other, less well understood, acid-catalyzed reactions and undergoes rapid deactivation associated with deposition of carbonaceous material. 10 refs., 3 figs.

  8. Urban leakage of liquefied petroleum gas and its impact on Mexico City air quality

    SciTech Connect (OSTI)

    Blake, D.R.; Rowland, F.S.

    1995-08-18

    Alkane hydrocarbons (propane, isobutane, and n-butane) from liquefied petroleum gas (LPG) are present in major quantities throughout Mexico City air because of leakage of the unburned gas from numerous urban sources. These hydrocarbons, together with olefinic minor LPG components, furnish substantial amounts of hydroxyl radical reactivity, a major precursor to formation of the ozone component of urban smog. The combined processes of unburned leakage and incomplete combustion of LPG play significant role in causing the excessive ozone characteristic of Mexico City. Reductions in ozone levels should be possible through changes in LPG composition and lowered rates of leakage. 23 refs., 3 tabs.

  9. Alkylate

    U.S. Energy Information Administration (EIA) Indexed Site

    Day) Product: Alkylate Aromatics Asphalt & Road Oil Isomers Isobutane Isopentane & Isohexane Isooctane Lubricants Marketable Petroleum Coke Hydrogen Sulfur Period: Annual (as of January 1) Download Series History Download Series History Definitions, Sources & Notes Definitions, Sources & Notes Show Data By: Product Area 2010 2011 2012 2013 2014 2015 View History U.S. 1,248,514 1,262,443 1,246,875 1,269,361 1,266,352 1,267,246 1982-2015 PAD District 1 95,500 108,629 79,429 91,429

  10. A high rate proportional chamber

    SciTech Connect (OSTI)

    Henderson, R.; Fraszer, W.; Openshaw, R.; Sheffer, G.; Salomon, M.; Dew, S.; Marans, J.; Wilson, P.

    1987-02-01

    Gas mixtures with high specific ionization allow the use of small interelectrode distances while still maintaining full efficiency. With the short electron drift distances the timing resolution is also improved. The authors have built and operated two 25 cm/sup 2/ chambers with small interelectrode distances. Also single wire detector cells have been built to test gas mixture lifetimes. Various admixtures of CF/sub 4/, DME, Isobutane, Ethane and Argon have been tested. Possible applications of such chambers are as beam profile monitors, position tagging of rare events and front end chambers in spectrometers.

  11. Crystalline mesoporous zirconia catalysts having stable tetragonal pore wall structure

    DOE Patents [OSTI]

    Sachtler, W.M.H.; Huang, Y.Y.

    1998-07-28

    Methods are disclosed for the preparation of new sulfated mesoporous zirconia materials/catalysts with crystalline pore walls of predominantly tetragonal crystal structure, characterized by nitrogen physical sorption measurement, X-ray diffraction, transmission electron microscopy and catalytic tests using n-butane isomerization to iso-butane and alkylation of 1-naphthol with 4-tert-butylstyrene as probe reactions. Sulfate deposition is preferred for the transformation of a mesoporous precursor with amorphous pore walls into a material with crystalline pore walls maintaining the mesoporous characteristics. 17 figs.

  12. Crystalline mesoporous zirconia catalysts having stable tetragonal pore wall structure

    DOE Patents [OSTI]

    Sachtler, Wolfgang M. H.; Huang, Yin-Yan

    1998-01-01

    Methods for the preparation of new sulfated mesoporous zirconia materials/catalysts with crystalline pore walls of predominantly tetragonal crystal structure, characterized by nitrogen physisorption measurement, X-ray diffraction, transmission electron microscopy and catalytic tests using n-butane isomerization to iso-butane and alkylation of 1-naphthol with 4-tert-butylstyrene as probe reactions. Sulfate deposition is preferred for the transformation of a mesoporous precursor with amorphous pore walls into a material with crystalline pore walls maintaining the mesoporous characteristics.

  13. FCC LPG olefinicity and branching enhanced by octane catalysts

    SciTech Connect (OSTI)

    Keyworth, D.A.; Reid, T.A.; Kreider, K.R.; Yatsu, C.A.

    1989-05-29

    Refiners are increasingly recognizing the downstream opportunities for fluid catalytic cracking LPG olefins for the production of methyl tertiary butyl ether (MTBE), ethyl tertiary butyl ether (ETBE, if the ethanol subsidy is extended to the production of ETBE), and as petrochemical feedstocks. Some of new gasoline FCC octane-enhancing catalysts can support those opportunities because their low non-framework alumina (low NFA) preserve both LPG olefinicity and promote branching of the LPG streams from the FCCU. The combined effect results in more isobutane for alkylate feed, more propylene in the propane/propylene stream, and more isobutene - which makes the addition of an MTBE unit very enticing.

  14. Flame Chemistry and Diagnostics

    Broader source: All U.S. Department of Energy (DOE) Office Webpages (Extended Search)

    Hansen 1 , M. R. Harper 2 , W. H. Green 2 , B. Yang 1,3 , H. Wang 3 High-Temperature Oxidation of n-Butanol, iso-Butane, and iso-Butene in Low-Pressure Premixed Flames 1 Combustion Research Facility, Sandia National Laboratories 1 st Annual Conference of the Combustion EFRC Sept. 23 rd - Sept. 24 th 2010 3 Department of Aerospace and Mechanical Engineering, University of Southern California 2 Department of Chemical Engineering, Massachusetts Institute of Technology Outline  Experimental

  15. Catalyst Activity Comparison of Alcohols over Zeolites

    SciTech Connect (OSTI)

    Ramasamy, Karthikeyan K.; Wang, Yong

    2013-01-01

    Alcohol transformation to transportation fuel range hydrocarbon on HZSM-5 (SiO2 / Al2O3 = 30) catalyst was studied at 360oC and 300psig. Product distributions and catalyst life were compared using methanol, ethanol, 1-propanol or 1-butanol as a feed. The catalyst life for 1-propanol and 1-butanol was more than double compared to that for methanol and ethanol. For all the alcohols studied, the product distributions (classified to paraffin, olefin, napthene, aromatic and naphthalene compounds) varied with time on stream (TOS). At 24 hours TOS, liquid product from 1-propanol and 1-butanol transformation primarily contains higher olefin compounds. The alcohol transformation process to higher hydrocarbon involves a complex set of reaction pathways such as dehydration, oligomerization, dehydrocyclization, and hydrogenation. Compared to ethylene generated from methanol and ethanol, oligomerization of propylene and butylene has a lower activation energy and can readily take place on weaker acidic sites. On the other hand, dehydrocyclization of propylene and butylene to form the cyclic compounds requires the sits with stronger acid strength. Combination of the above mentioned reasons are the primary reasons for olefin rich product generated in the later stage of the time on stream and for the extended catalyst life time for 1 propanol and 1 butanol compared to methanol and ethanol conversion over HZSM-5.

  16. Separation of vapour and gas mixtures using a thin zeolite MFI membrane

    SciTech Connect (OSTI)

    Vroon, Z.A.E.P.; Gilde, M.J.; Kiezer, K.

    1994-12-31

    Zeolite MFI composite membranes were prepared by in situ crystallisation. A very thin (L < 5 {mu}m) polycrystalline MFI layer was grown on a flat {alpha}-Al{sub 2}O{sub 3} support (pore radii 80 nm). XRD and SEM showed that the layer was built of small MFI particles ({+-}200 nm). The single gas flux of methane, n-butane and iso-butane are respectively 9.7, 2.7 and 0.032 10{sup -3} mol.m{sup -2}.s{sup -1} at 25{degrees}C and 100 kPa. The separation of n-butane/methane is reversible. At 25{degrees}C it is possible to separate n-butane from methane. At 200{degrees}C it is possible to separate methane from n-butane. The separation factor for 50 n-butane/50 iso-butane is 26 at 50{degrees}C. Experiments with large molecules showed that the zeolite MFI membrane contains no pores larger than inherent to the zeolite.

  17. Performance of a new LMRPC prototype for the STAR MTD system

    SciTech Connect (OSTI)

    Ruan, L.J.; Wang, Y.; Chen, H. S.; Ding, W. C.; Qiu, X. Z.; Wang, J. B.; Zhu, X. L.; Kang, K. J.; Cheng, J. P.; Li, Y. J.; Ruan, L.; Xu, Z.; Asselta, K.; Christie, W.; D'Agostino, C.; Dunlop, J.; Landgraf, J.; Ljubicic, T.; Scheblein, J.; Soja, R.; Tang, A. H.; Ullrich, T.; Crawford, H. J.; Engelage, J.; Sanchez, M. Calderon de la Barca; Reed, R.; Liu, H. D.; Butterworth, J.; Eppley, G.; Geurts, F.; Llope, W. J.; McDonald, D.; Nussbaum, T.; Roberts, J.; Xin, K.; Bridges, L.; Li, J. C.; Qian, S.; Ning, Z.; Chen, H. F.; Huang, B. C.; Li, C.; Shao, M.; Sun, Y. J.; Tang, Z. B.; Wang, X. L.; Xu, Y. C.; Zhang, Z. P.; Zeng, H.; Zhou, Y.; Clarke, R.; Mioduszewski, S.; Davila, A.; Hoffmann, G. W.; Li, L.; Markert, C.; Ray, L.; Schambach, J.; Thein, D.; Wada, M.; Ahammed, Z.; Bhaduri, P. P.; Chattopadhyay, S.; Dubey, A. K.; Dutt-Mazumdar, M. R.; Ghosh, P.; Khan, S. A.; Muhuri, S.; Mohanty, B.; Nayak, T. K.; Pal, S.; Singaraju, R.; Singhal, V.; Tribedy, P.; Viyogi, Y. P.

    2011-03-21

    A new prototype of a Long-Strip Multi-Gap Resistive Plate Chamber (LMRPC) for the STAR Muon Telescope Detector (MTD) at RHIC has been developed. This prototype has an active area of 52 x 90 cm{sup 2} and consists of six 250 {mu}m wide gaps. Each detector has 12 strips, read-out at both ends, which are each 3.8 cm wide and 90 cm long with 0.6 cm intervals. In cosmic-ray tests, the efficiency was larger than 95% and the time resolution was {approx}75 ps for the 94% Freon, 5% iso-butane, and 1% SF{sub 6} gas mixture. There was good uniformity in the performance across the different strips. The module was also tested in a proton beam at IHEP in Beijing. The efficiency was close to 100% and the best timing resolution achieved was 55 ps for the 90% Freon, 5% iso-butane, and 5% SF6 gas mixture. Trigger scans along and across the strip direction were also performed.

  18. Reactivity Screening of Anatase TiO2 Nanotube Arrays and Anatase Thin Films: A Surface Chemistry Point of View

    SciTech Connect (OSTI)

    Funk, S.; Hokkanen, B.; Nurkic, T.; Goering, J.; Kadossov, E.; Burghaus, Uwe; Ghicov, A.; Schmuki, P.; Yu, Zhongqing; Thevuthasan, Suntharampillai; Saraf, Laxmikant V.

    2008-09-19

    As a reactivity screening we collected thermal desorption spectroscopy (TDS) data of iso-butane, O2, CO2, and CO adsorbed on ordered TiO2 nanotube (TiNTs) arrays. As a reference system iso-butane adsorption on an anatase TiO2 thin film has been considered as well. The as-grown TiNTs are vertically aligned and amorphous. Polycrystalline (poly.) anatase or poly. anatase/rutile mixed nanotubes are formed by annealing confirmed by x-ray diffraction (XRD) and scanning electron microscopy (SEM). The anatase thin film was grown on SrTiO3(001) and characterized by XRD and atomic force microscopy (AFM). Surprisingly, oxygen distinctly interacts with the TiNTs whereas this process is not observed on fully oxidized single crystal rutile TiO2(110). Desorption temperatures of 110-150 K and 100-120 K were observed for CO2 and CO, respectively, on the TiNTs. Variations in the binding energies of the alkanes on TiNTs and anatase thin films also were present, i.e., a structure-activity relationship (SAR) is evident.

  19. Kinetics and deactivation of sulfated zirconia catalysts for butane isomerization

    SciTech Connect (OSTI)

    Fogash, K.B.; Larson, R.B.; Gonzalez, M.R.

    1996-09-15

    Reaction kinetics studies were conducted of n-butane and isobutane isomerization over sulfated zirconia at 423 K. The kinetic data can be described well by a rate expression based on a reversible, bimolecular surface reaction between two adsorbed n-C{sub 4} species, probably through a C{sub 8} intermediate, to produce one i-C{sub 4} species, as well as surface reaction between two adsorbed i-C{sub 4} species to produce one n-C{sub 4} species. This reaction sequence also describes well the rates of C{sub 4}-disproportionation reactions to produce C{sub 3} and C{sub 5} species. The initial rate of catalyst deactivation is faster during n-butane isomerization than during isobutane isomerization, and the longer-term rate of deactivation during n-butane isomerization increases with the pressures of n-butane. The more rapid catalyst deactivation during n-butane isomerization may be related to the formation of n-C{sub 4}-diene species. 25 refs., 10 figs., 4 tabs.

  20. Oxygenates from light alkanes catalyzed by NO{sub x} in the gas phase

    SciTech Connect (OSTI)

    Otsuka, Kiyoshi; Takahashi, Ryo; Yamanaka, Ichiro

    1999-07-01

    The partial oxidations of light alkanes (methane, ethane, propane, and iso-butane) catalyzed by NO{sub x} in the gas phase have been studied at a pressure of less than 1 bar. For all the alkanes tested, the addition of NO to the mixture of alkanes and O{sub 2} enhanced the selectivities and the yields of oxygenates remarkably. It was suggested that NO{sub 2} generated from NO and O{sub 2} initiated the oxidation of alkanes and would specifically accelerate the C-C bond fission, enhancing the formation of C{sub 1}-oxygenates from ethane, propane, and iso-butane. No{sub 2} and NO would be used as a homogeneous catalyst at >600 C because nitroalkanes formed were decomposed completely, releasing the NO{sub x}. The comparison of the product distributions for the decomposition and oxidation of nitroalkanes and alkylnitrites strongly suggested that the oxygenates (HCHO, CH{sub 3}CHO, and CH{sub 3}COCH{sub 3}) were formed from the corresponding alkylnitrites which must be the reaction intermediates during the oxidation of alkanes with an O{sub 2} and NO mixture.

  1. Analyses of mixed-hydrocarbon binary thermodynamic cycles for moderate-temperature geothermal resources

    SciTech Connect (OSTI)

    Demuth, O.J.

    1981-02-01

    A number of binary geothermal cycles utilizing mixed hydrocarbon working fluids were analyzed with the overall objective of finding a working fluid which can produce low-cost electrical energy using a moderately-low temperature geothermal resource. Both boiling and supercritical shell-and-tube cycles were considered. The performance of a dual-boiling isobutane cycle supplied by a 280/sup 0/F hydrothermal resource (corresponding to the 5 MW pilot plant at the Raft River site in Idaho) was selected as a reference. To investigate the effect of resource temperature on the choice of working fluid, several analyses were conducted for a 360/sup 0/F hydrothermal resource, which is representative of the Heber resource in California. The hydrocarbon working fluids analyzed included methane, ethane, propane, isobutane, isopentane, hexane, heptane, and mixtures of those pure hydrocarbons. For comparison, two fluorocarbon refrigerants were also analyzed. These fluorocarbons, R-115 and R-22, were suggested as resulting in high values of net plant geofluid effectiveness (watt-hr/lbm geofluid) at the two resource temperatures chosen for the study. Preliminary estimates of relative heat exchanger size (product of overall heat transfer coefficient times heater surface area) were made for a number of the better performing cycles.

  2. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    2,458 1,124 19,312 10,020 107 138 18,254 4,948 19,680 Crude Oil 9,129 - - - - 7,910 -105 677 15,884 374 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 3,329 -21 418 220 - - -591 567 1,245 2,724 Pentanes Plus 404 -21 - - 10 - - 32 137 223 1 Liquefied Petroleum Gases 2,925 - - 418 210 - - -623 431 1,022 2,723 Ethane/Ethylene 1,148 - - 4 - - - -18 - 76 1,094 Propane/Propylene 1,149 - - 566 190 - - -470 - 884 1,490 Normal Butane/Butylene 326 - - -149 9 - - -161 234 57 57

  3. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    7,397 114 7,459 3,648 -2,747 247 161 6,885 3,807 5,265 Crude Oil 5,567 - - - - 2,956 339 122 494 8,310 180 0 Natural Gas Plant Liquids and Liquefied Refinery Gases 1,830 -1 324 10 393 - - -339 320 869 1,706 Pentanes Plus 193 -1 - - 10 -87 - - 16 85 2 12 Liquefied Petroleum Gases 1,637 - - 324 - 480 - - -355 235 866 1,694 Ethane/Ethylene 741 - - 4 - 242 - - -22 - - 1,009 Propane/Propylene 580 - - 371 - 127 - - -309 - 819 567 Normal Butane/Butylene 116 - - -48 - 96 - - -46 128 41 41

  4. Supply and Disposition of Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    33,189 582 87,994 38,350 15,497 301 -2,608 82,871 11,140 84,511 151,614 Crude Oil 31,141 - - - - 32,266 3,747 -765 293 66,096 - 0 57,375 Natural Gas Plant Liquids and Liquefied Refinery Gases 2,048 -13 427 237 - - - -781 2,338 1,069 73 2,464 Pentanes Plus 976 -13 - - - - - - 2 830 2 129 41 Liquefied Petroleum Gases 1,072 - - 427 237 - - - -783 1,508 1,066 -55 2,423 Ethane/Ethylene 2 - - - - - - - - - - 2 - Propane/Propylene 338 - - 1,169 237 - - - -200 - 937 1,007 733 Normal Butane/Butylene 401

  5. Jet fuel from LPG

    SciTech Connect (OSTI)

    Maples, R.E.; Jones, J.R.

    1983-02-01

    Explains how jet fuel can be manufactured from propane and/or butane with attractive rates of return. This scheme is advantageous where large reserves of LPG-bearing gas is available or LPG is in excess. The following sequence of processes in involved: dehydrogenation of propane (and/or butane) to propylene (and/or butylene); polymerization of this monomer to a substantial yield of the desired polymer by recycling undesired polymer; and hydrotreating the polymer to saturate double bonds. An attribute of this process scheme is that each of the individual processes has been practiced commercially. The process should have appeal in those parts of the world which have large reserves of LPG-bearing natural gas but little or no crude oil, or where large excesses of LPG are available. Concludes that economic analysis shows attractive rates of return in a range of reasonable propane costs and product selling prices.

  6. Production of biodiesel using expanded gas solvents

    SciTech Connect (OSTI)

    Ginosar, Daniel M; Fox, Robert V; Petkovic, Lucia M

    2009-04-07

    A method of producing an alkyl ester. The method comprises providing an alcohol and a triglyceride or fatty acid. An expanding gas is dissolved into the alcohol to form a gas expanded solvent. The alcohol is reacted with the triglyceride or fatty acid in a single phase to produce the alkyl ester. The expanding gas may be a nonpolar expanding gas, such as carbon dioxide, methane, ethane, propane, butane, pentane, ethylene, propylene, butylene, pentene, isomers thereof, and mixtures thereof, which is dissolved into the alcohol. The gas expanded solvent may be maintained at a temperature below, at, or above a critical temperature of the expanding gas and at a pressure below, at, or above a critical pressure of the expanding gas.

  7. Luminescence-Based Spectroelectrochemical Sensor for [Tc(dmpe)3]2+/+ (dmpe = 1,2-bis(dimethylphosphino)ethane) within a Charge-Selective Polymer Film

    SciTech Connect (OSTI)

    Chatterjee, Sayandev; Del Negro, Andrew S.; Edwards, Matthew K.; Bryan, Samuel A.; Kaval, Necati; Pantelic, Nebojsa; Morris, Laura K.; Heineman, W. R.; Seliskar, Carl J.

    2011-03-01

    A spectroelectrochemical sensor consisting of an indium tin oxide (ITO) optically transparent electrode (OTE) coated with a thin film of sulfonated polystyrene-blockpoly(ethylene-ran-butylene)-block-polystyrene (SSEBS) was developed for [Tc(dmpe)3]+.. [Tc(dmpe)3]+ preconcentrated by ion-exchange into the SSEBS film after 20 min exposure to aqueous [Tc(dmpe)3]+ solution, resulting in a 14-fold increase in cathodic peak current compared to a bare OTE. Colorless [Tc(dmpe)3]+ was reversibly oxidized to colored [Tc(dmpe)3]2+ by cyclic voltammetry. Detection of [Tc(dmpe)3]2+ was accomplished by electrochemically cycling the complex between non-emissive [Tc(dmpe)3]+ and emissive [Tc(dmpe)3]2+ and monitoring the modulated emission (?exc = 532 nm; ?em = 660 nm). The sensor gave a linear response over the range of 0.16 to 340.0 M.

  8. Amphiphilic Surface Active Triblock Copolymers with Mixed Hydrophobic and Hydrophilic Side Chains for Tuned Marine Fouling-Release Properties

    SciTech Connect (OSTI)

    Park, D.; Weinman, C; Finlay, J; Fletcher, B; Paik, M; Sundaram, H; Dimitriou, M; Sohn, K; Callow, M; et al.

    2010-01-01

    Two series of amphiphilic triblock surface active block copolymers (SABCs) were prepared through chemical modification of two polystyrene-block-poly(ethylene-ran-butylene)-block-polyisoprene ABC triblock copolymer precursors. The methyl ether of poly(ethylene glycol) [M{sub n} {approx} 550 g/mol (PEG550)] and a semifluorinated alcohol (CF{sub 3}(CF{sub 2}){sub 9}(CH{sub 2}){sub 10}OH) [F10H10] were attached at different molar ratios to impart both hydrophobic and hydrophilic groups to the isoprene segment. Coatings on glass slides consisting of a thin layer of the amphiphilic SABC deposited on a thicker layer of an ABA polystyrene-block-poly(ethylene-ran-butylene)-block-polystyrene thermoplastic elastomer were prepared for biofouling assays with algae. Dynamic water contact angle analysis, X-ray photoelectron spectroscopy (XPS) and near-edge X-ray absorption fine structure (NEXAFS) measurements were utilized to characterize the surfaces. Clear differences in surface structure were realized as the composition of attached side chains was varied. In biofouling assays, the settlement (attachment) of zoospores of the green alga Ulva was higher for surfaces incorporating a large proportion of the hydrophobic F10H10 side chains, while surfaces with a large proportion of the PEG550 side chains inhibited settlement. The trend in attachment strength of sporelings (young plants) of Ulva did not show such an obvious pattern. However, amphiphilic SABCs incorporating a mixture of PEG550 and F10H10 side chains performed the best. The number of cells of the diatom Navicula attached after exposure to flow decreased as the content of PEG550 to F10H10 side chains increased.

  9. Table 5.10 Natural Gas Plant Liquids Production, 1949-2011 (Thousand Barrels)

    U.S. Energy Information Administration (EIA) Indexed Site

    0 Natural Gas Plant Liquids Production, 1949-2011 (Thousand Barrels) Year Finished Petroleum Products 1 Liquefied Petroleum Gases Pentanes Plus 4 Total Ethane 2 Isobutane Normal Butane 3 Propane 2,3 Total 1949 19,210 3,056 4,182 22,283 27,114 56,634 81,241 157,086 1950 23,931 4,253 4,667 25,323 37,018 71,261 86,769 181,961 1951 26,505 5,545 5,509 27,960 45,798 84,812 93,437 204,754 1952 25,488 7,089 6,568 31,349 54,732 99,738 98,289 223,515 1953 25,739 6,151 7,006 35,308 61,544 110,009 102,831

  10. U.S. Blender Net Input

    U.S. Energy Information Administration (EIA) Indexed Site

    Sep-15 Oct-15 Nov-15 Dec-15 Jan-16 Feb-16 View History Total Input 248,620 258,292 242,060 252,467 242,396 238,655 2005-2016 Natural Gas Plant Liquids and Liquefied Refinery Gases 1,681 2,789 2,599 2,073 2,044 1,531 2008-2016 Pentanes Plus 111 413 479 223 489 347 2005-2016 Liquid Petroleum Gases 1,570 2,376 2,120 1,850 1,555 1,184 2008-2016 Normal Butane 1,563 2,376 2,120 1,850 1,555 1,184 2005-2016 Isobutane 7 2005-2015 Other Liquids 246,939 255,503 239,461 250,394 240,352 237,124 2008-2016

  11. U.S. Crude Oil Developmental Wells Drilled (Number of Elements)

    Gasoline and Diesel Fuel Update (EIA)

    2010 2011 2012 2013 2014 2015 View History Total Input 2,166,784 2,331,109 2,399,318 2,539,812 2,824,480 2,987,634 2005-2015 Natural Gas Plant Liquids and Liquefied Refinery Gases 6,538 7,810 10,663 12,304 14,038 16,334 2008-2015 Pentanes Plus 1,989 2,326 4,164 4,241 3,184 2,554 2005-2015 Liquid Petroleum Gases 4,549 5,484 6,499 8,063 10,854 13,780 2008-2015 Normal Butane 4,549 5,484 6,499 8,063 10,823 13,741 2005-2015 Isobutane 31 39 2005-2015 Other Liquids 2,160,246 2,323,299 2,388,655

  12. Countercurrent direct contact heat exchange process and system

    DOE Patents [OSTI]

    Wahl, III, Edward F.; Boucher, Frederic B.

    1979-01-01

    Recovery of energy from geothermal brines and other hot water sources by direct contact heat exchange with a working fluid, such as a hydrocarbon working fluid, e.g. isobutane. The process and system consists of a plurality of stages, each stage including mixing and settling units. In the first stage, hot brine and arm working fluid are intimately mixed and passed into a settler wherein the brine settles to the bottom of the settler and the hot working fluid rises to the top. The hot working fluid is passed to a heat engine or turbine to produce work and the working fluid is then recycled back into the system. The system is comprised of a series of stages each containing a settler and mixer, and wherein the working fluid and the brine flow in a countercurrent manner through the stages to recover the heat from the brine in increments and raise the temperature of the working fluid in increments.

  13. Process boasts 95% selectivity for LPG

    SciTech Connect (OSTI)

    Brinkmeyer, F.M.; Drehman, L.E.; Olbrich, M.E.; Rohr, D.F.

    1983-03-28

    This article describes a new Phillips catalytic process for the dehydrogenation and/or the dehydrocyclization of paraffinic feedstocks, steam active reforming (STAR), which produces no structural isomerization. Light paraffins such as propane, isobutane, and normal butane can be dehydrogenated to their respective mono-olefins with selectivities as high as 95%. The process offers such advantages as: it will accept a wide range of feedstocks; selectivity to desired products is high; there is a minimum of structural isomerization which permits the production of specific products from particular feedstocks with high purity; it works well with paraffinic and olefinic materials which make poor feeds in conventional reforming processes; and the catalyst has moderate tolerance for sulfur and nitrogen compounds.

  14. Simple electronic apparatus for the analysis of radioactively labeled gel electrophoretograms

    DOE Patents [OSTI]

    Goulianos, Konstantin; Smith, Karen K.; White, Sebastian N.

    1982-01-01

    A high resolution position sensitive radiation detector for analyzing radiation emanating from a source, constructed of a thin plate having an elongated slot with conductive edges acting as a cathode, a charged anode wire positioned within 0.5 mm adjacent the source and running parallel to the slot and centered therein, an ionizable gas ionized by radiation emanating from the source provided surrounding the anode wire in the slot, a helical wire induction coil serving as a delay line and positioned beneath the anode wire for detecting gas ionization and for producing resulting ionization signals, and processing circuits coupled to the induction coil for receiving ionization signals induced therein after determining therefrom the location along the anode wire of any radiation emanating from the source. An ionization gas of 70% Ar, 29% Isobutane, 0.6% Freon 13BI, and 0.4% Methylal is used.

  15. Mass transfer of volatile organic compounds from drinking water to indoor air: The role of residential dishwashers

    SciTech Connect (OSTI)

    Howard-Reed, C.; Corsi, R.L.; Moya, J.

    1999-07-01

    Contaminated tap water may be a source of volatile organic compounds (VOCs) in residential indoor air. To better understand the extent and impact of chemical emissions from this source, a two-phase mass balance model was developed based on mass transfer kinetics between each phase. Twenty-nine experiments were completed using a residential dishwasher to determine model parameters. During each experiment, inflow water was spiked with a cocktail of chemical tracers with a wide range of physicochemical properties. In each case, the effects of water temperature, detergent, and dish-loading pattern on chemical stripping efficiencies and mass transfer coefficients were determined. Dishwasher headspace ventilation rates were also measured using an isobutylene tracer gas. Chemical stripping efficiencies for a single cycle ranged from 18% to 55% for acetone, from 96% to 98% for toluene, and from 97% to 98% for ethylbenzene and were consistently 100% for cyclohexane. Experimental results indicate that dishwashers have a relatively low but continuous ventilation rate that results in significant chemical storage within the headspace of the dishwasher. In conjunction with relatively high mass transfer coefficients, low ventilation rates generally lead to emissions that are limited by equilibrium conditions after approximately 1--2 min of dishwasher operation.

  16. DME-to-oxygenates process studies

    SciTech Connect (OSTI)

    Tartamella, T.L.; Sardesai, A.; Lee, S.; Kulik, C.J.

    1994-12-31

    The feasibility of the production of hydrocarbons from dimethyl ether (DNM) has been illustrated in a fixed bed micro-reactor as well as a bench scale fluidized bed reactor by the University of Akron/EPRI DME-to-Hydrocarbon (DTG) Process. The DTG process has distinct advantages over its methanol based counterpart. Specifically, the DTG process excels in the area of higher productivity, higher per-pass conversion, and lower heat duties than the MTG process. Also of special importance is the production of oxygenates -- including MTBE, ETBE, and TAME. DME may be reacted with isobutylene to produce a mixture of MTBE and ETBE. The properties of ETBE excel over MTBE in the areas of lower RVP and higher RON. According to industrial reports, MTBE is the fastest growing chemical (1992 US capacity 135,350 BPD, with expected growth of 34%/year to 1997). Also, recent renewed interest as an octane-enhancer and as a source of oxygen has spurred a growing interest in nonrefinery synthesis routes to ETBE. TAME, with its lower RVP and higher RON has proven useful as a gasoline blending agent and octane enhancer and may also be produced directly from DME. DME, therefore, serves as a valuable feedstock in the conversion of may oxygenates with wide-scale industrial importance. It should be also noted that the interest in the utilization of DME as process feedstock is based on the favorable process economics of EPRI/UA`s liquid phase DME process.

  17. Solvation and Acid Strength Effects on Catalysis by Faujasite Zeolites

    SciTech Connect (OSTI)

    Gounder, Rajamani P.; Jones, Andrew J.; Carr, Robert T.; Iglesia, Enrique

    2012-02-01

    Kinetic, spectroscopic, and chemical titration data indicate that differences in monomolecular isobutane cracking and dehydrogenation and methanol dehydration turnover rates (per H+) among FAU zeolites treated thermally with steam (H-USY) and then chemically with ammonium hexafluorosilicate (CDHUSY) predominantly reflect differences in the size and solvating properties of their supercage voids rather than differences in acid strength. The number of protons on a given sample was measured consistently by titrations with Na+, with CH3 groups via reactions of dimethyl ether, and with 2,6-di-tert-butylpyridine during methanol dehydration catalysis; these titration values were also supported by commensurate changes in acidic OH infrared band areas upon exposure to titrant molecules. The number of protons, taken as the average of the three titration methods, was significantly smaller than the number of framework Al atoms (Alf) obtained from X-ray diffraction and 27Al magic angle spinning nuclear magnetic resonance spectroscopy on H-USY (0.35 H+/Alf) and CD-HUSY (0.69 H+/Alf). These data demonstrate that the ubiquitous use of Alf sites as structural proxies for active H+ sites in zeolites can be imprecise, apparently because distorted Al structures that are not associated with acidic protons are sometimes detected as Alf sites. Monomolecular isobutane cracking and dehydrogenation rate constants, normalized non-rigorously by the number of Alf species, decreased with increasing Na+ content on both H-USY and CD-HUSY samples and became undetectable at sub-stoichiometric exchange levels (0.32 and 0.72 Na+/Alf ratios, respectively), an unexpected finding attributed incorrectly in previous studies to the presence of minority ‘‘super-acidic’’ sites. These rate constants, when normalized rigorously by the number of residual H+ sites were independent of Na+ content on both H-USY and CD-HUSY samples, reflecting the stoichiometric replacement of protons that are uniform in reactivity by Na+ cations. Monomolecular isobutane cracking and dehydrogenation rate constants (per H+; 763 K), however, were higher on H-USY than CD-HUSY (by a factor of 1.4). Equilibrium constants for the formation of protonated methanol dimers via adsorption of gaseous methanol onto adsorbed methanol monomers, determined from kinetic studies of methanol dehydration to dimethyl ether (433 K), were also higher on H-USY than CD-HUSY (by a factor of 2.1). These larger constants predominantly reflect stronger dispersive interactions in H-USY, consistent with its smaller supercage voids that result from the occlusion of void space by extraframework Al (Alex) residues. These findings appear to clarify enduring controversies about the mechanistic interpretation of the effects of Na+ and Alex species on the catalytic reactivity of FAU zeolites. They also illustrate the need to normalize rates by the number of active sites instead of more convenient but less accurate structural proxies for such sites.

  18. Blue emission of Eu2+-doped translucent alumina

    DOE Public Access Gateway for Energy & Science Beta (PAGES Beta)

    Yang, Yan; Zhang, Lihua; Kisslinger, Kim; Wei, Hua; Melcher, Charles L.; Wu, Yiquan

    2015-08-21

    Inorganic scintillators are very important in medical and industrial measuring systems in the detection and measurement of ionizing radiation. In addition to Ce3+, a widely used dopant ion in oxide scintillators, divalent Europium (Eu2+) has shown promise as a high-luminescence, fast-response luminescence center useful in the detection of ionizing radiation. In this research, aluminum oxide (Al2O3) was studied as a host material for the divalent europium ion. Polycrystalline samples of Eu2+-doped translucent Al2O3 were fabricated, and room temperature luminescence behavior was observed. Al2O3 ceramics doped with 0.1 at% Eu2+ were fabricated with a relative density of 99.75% theoretical density andmore » in-line transmittance of 22% at a wavelength of 800 nm. The ceramics were processed by a gel-casting method, followed by sintering under high vacuum. The gelling agent, a copolymer of isobutylene and maleic anhydride, is marketed under the commercial name ISOBAM, and has the advantage of simultaneously acting as both a gelling agent and as a dispersant. The microstructure and composition of the vacuum-sintered Eu2+:Al2O3 were characterized by Scanning Electric Microscopy (SEM), Transmission Electron Microscopy (TEM), and Energy-dispersive X-ray spectroscopy (EDS). The phase composition was determined by X-ray diffraction measurements (XRD) combined with Rietveld analysis. The photoluminescence behavior of the Eu2+:Al2O3 was characterized using UV light as the excitation source, which emitted blue emission at 440 nm. The radio-luminescence of Eu2+:Al2O3 was investigated by illumination with X-ray radiation, showing three emission bands at 376 nm, 575 nm and 698 nm. Furthermore, multiple level traps at different depths were detected in the Eu2+:Al2O3 by employing thermoluminescence measurements.« less

  19. Superacid catalysis of light hydrocarbon conversion. DOE PETC third quarterly report, February 25, 1994--May 24, 1994

    SciTech Connect (OSTI)

    Gates, B.C.

    1995-12-31

    Environmental concerns are leading to the replacement of aromatic hydrocarbons in gasoline by high-octane-number branched paraffins and oxygenated compounds such as methyl t-butyl ether. The ether is produced from methanol and isobutylene, and the latter can be formed from n-butane by isomerization followed by dehydrogenation. Paraffin isomerization reactions are catalyzed by very strong acids such as aluminum chloride supported on alumina. The aluminum chloride-containing catalysts are corrosive, and their disposal is expensive. Alternatively, hydroisomerization is catalyzed by zeolite-supported metals at high temperatures, but high temperatures do not favor branched products at equilibrium. Thus there is a need for improved catalysts and processes for the isomerization of n-butane and other straight-chain paraffins. Consequently, researchers have sought for solid acids that are noncorrosive and active enough to catalyze isomerization of paraffins at low temperatures. For example, sulfated zirconia catalyzes isomerization of n-butane at temperatures as low as 25{degrees}C. The addition of iron and manganese promoters has been reported to increase the activity of sulfated zirconia for n-butane isomerization by three orders of magnitude. Although the high activity of this catalyst is now established, the reaction network is not known, and the mechanism has not been investigated. The goal of this work is to investigate low-temperature reactions of light paraffins catalyzed by solid superacids of the sulfated zirconia type. The present report is concerned with catalysis of n-butane conversion catalyzed by the Fe- and Mn- promoted sulfated zirconia described in the previous report in this series.

  20. U.S. Product Supplied for Crude Oil and Petroleum Products

    U.S. Energy Information Administration (EIA) Indexed Site

    576,739 599,856 575,825 605,862 590,718 570,721 1981-2016 Crude Oil 0 0 173 0 0 0 1981-2016 Natural Gas Liquids and LRGs 64,042 75,293 76,572 85,729 91,675 79,004 1981-2016 Pentanes Plus 1,874 4,194 1,087 2,486 1,837 28 1981-2016 Liquefied Petroleum Gases 62,168 71,100 75,485 83,244 89,838 78,975 1981-2016 Ethane/Ethylene 31,059 33,115 35,088 35,366 34,222 31,731 1981-2016 Propane/Propylene 26,884 31,606 34,361 42,033 48,892 43,203 1981-2016 Normal Butane/Butylene 1,967 3,065 2,976 2,463 3,385

  1. Laser ultrasonic furnace tube coke monitor. Quarterly technical progress report No. 1, May 1--August 1, 1998

    SciTech Connect (OSTI)

    1998-08-15

    The overall aim of the project is to demonstrate the performance and practical use of a laser ultrasonic probe for measuring the thickness of coke deposits located within the high temperature tubes of a thermal cracking furnace. This aim will be met by constructing an optical probe that will be tested using simulated coke deposits that are positioned inside of a bench-scale furnace. Successful development of the optical coke detector will provide industry with the only available method for on-line measurement of coke deposits. The optical coke detector will have numerous uses in the refining and petrochemical sectors including monitoring of visbreakers, hydrotreaters, delayed coking units, vacuum tower heaters, and various other heavy oil heating applications where coke formation is a problem. The coke detector will particularly benefit the olefins industry where high temperature thermal crackers are used to produce ethylene, propylene, butylene and other important olefin intermediates. The ethylene industry requires development of an on-line method for gauging the thickness of coke deposits in cracking furnaces because the current lack of detailed knowledge of coke deposition profiles introduces the single greatest uncertainty in the simulation and control of modern cracking furnaces. The laser ultrasonic coke detector will provide operators with valuable new information allowing them to better optimize the decoking turnaround schedule and therefore maximize production capacity.

  2. Polymer Growth Rate in a Wire Chamber with Oxygen,Water, or Alcohol Gas Additives

    SciTech Connect (OSTI)

    Boyarski, Adam; /SLAC

    2008-07-02

    The rate of polymer growth on wires was measured in a wire chamber while the chamber was aged initially with helium-isobutane (80:20) gas, and then with either oxygen, water, or alcohol added to the gas. At the completion of the aging process for each gas mixture, the carbon content on the wires was measured in a SEM/EDX instrument. The same physical wires were used in all the gas mixtures, allowing measurement of polymer build up or polymer depletion by each gas additive. It is found that the rate of polymer growth is not changed by the presence of oxygen, water or alcohol. Conjecture that oxygen reduces breakdown by removing polymer deposits on field wires is negated by these measurements. Instead, it appears that the reduced breakdown is due to lower resistance in the polymer from oxygen ions being transported into the polymer. It is also observed that field wires bombarded by the electrons in the SEM and then placed back into the chamber show an abundance of single electrons being emitted, indicating that electron charge is stored in the polymer layer and that a high electric field is necessary to remove the charge.

  3. U.S. Natural Gas Plant Field Production

    U.S. Energy Information Administration (EIA) Indexed Site

    Sep-15 Oct-15 Nov-15 Dec-15 Jan-16 Feb-16 View History Natural Gas Liquids 100,283 106,269 103,071 104,629 102,401 96,538 1981-2016 Pentanes Plus 13,829 13,963 12,798 12,666 12,323 11,708 1981-2016 Liquefied Petroleum Gases 86,454 92,306 90,273 91,963 90,078 84,830 1981-2016 Ethane 32,977 35,905 36,534 37,506 35,939 33,304 1981-2016 Propane 34,187 36,192 34,569 35,143 34,929 33,311 1981-2016 Normal Butane 10,103 10,387 10,054 9,735 9,656 9,463 1981-2016 Isobutane 9,187 9,822 9,116 9,579 9,554

  4. U.S. Refinery Net Input

    U.S. Energy Information Administration (EIA) Indexed Site

    Sep-15 Oct-15 Nov-15 Dec-15 Jan-16 Feb-16 View History Total 321,878 318,765 321,561 328,213 302,955 290,718 2005-2016 Crude Oil 485,221 479,416 494,682 519,726 495,806 460,629 2005-2016 Natural Gas Plant Liquids 14,690 15,903 17,686 18,057 18,673 14,924 2005-2016 Pentanes Plus 4,693 4,431 3,897 3,932 4,389 3,616 2005-2016 Liquefied Petroleum Gases 9,997 11,472 13,789 14,125 14,284 11,308 2005-2016 Normal Butane 3,144 5,323 7,093 7,560 7,947 5,592 2005-2016 Isobutane 6,853 6,149 6,696 6,565

  5. Improving the stability of H-mordenite for n-butane isomerization

    SciTech Connect (OSTI)

    Asuquo, R.A.; Eder-Mirth, G.; Lercher, J.A.

    1997-06-01

    The conversion of n-butane over mordenite-based catalysts in the presence of hydrogen and water was investigated for reaction temperatures between 523 and 623 K. Special attention was given to the influence of Pt upon catalytic activity, selectivity, and stability. With parent mordenite the catalytic activity for n-butane conversion decreased markedly after a short time on stream. Deactivation can be minimized by hydrogen (in the presence of Pt) and water addition. Both measures are thought to reduce the concentration of intermediate olefins in the zeolite pores. The best results with respect to selective conversion of n-butane to isobutane were obtained for 0.25 wt% Pt on mordenite in the presence of hydrogen. Higher concentrations of Pt in the catalyst are shown to be detrimental for n-butane isomerization, because of increasing selectivity to hydrogenolysis. A detailed mechanistic scheme for n-butane conversion over Pt-containing mordenites is presented. n-Butane conversion is concluded to occur via a bimolecular mechanism involving a complex network of hydrogen transfer, oligomerization/cracking, isomerization, hydrogenation/dehydrogenation, and hydrogenolysis. 23 refs., 14 figs., 5 tabs.

  6. Global gas processing will strengthen to meet expanding markets

    SciTech Connect (OSTI)

    Haun, R.R.; Otto, K.W.; Whitley, S.C.; Gist, R.L.

    1996-07-01

    The worldwide LPG industry continues to expand faster than the petroleum industry -- 4%/year for LPG vs. 2%/year for petroleum in 1995 and less than 1%/year in the early 1990s. This rapid expansion of LPG markets is occurring in virtually every region of the world, including such developing countries as China. The Far East is the focus of much of the LPG industry`s attention, but many opportunities exist in other regions such as the Indian subcontinent, Southeast Asia, and Latin America. The investment climate is improving in all phases of downstream LPG marketing, including terminaling, storage, and wholesale and retail distribution. The world LPG supply/demand balance has been relatively tight since the Gulf War and should remain so. Base demand (the portion of demand that is not highly price-sensitive) is expanding more rapidly than supplies. As a result, the proportion of total LPG supplies available for price-sensitive petrochemical feedstock markets is declining, at least in the short term. The paper discusses importers, price patterns, world LPG demand, world LPG supply, US NGL supply, US gas processing, ethane and propane supply, butane, isobutane, and natural gasoline supply, and US NGL demand.

  7. Plasma chemistry in wire chambers

    SciTech Connect (OSTI)

    Wise, J.

    1990-05-01

    The phenomenology of wire chamber aging is discussed and fundamentals of proportional counters are presented. Free-radical polymerization and plasma polymerization are discussed. The chemistry of wire aging is reviewed. Similarities between wire chamber plasma (>1 atm dc-discharge) and low-pressure rf-discharge plasmas, which have been more widely studied, are suggested. Construction and use of a system to allow study of the plasma reactions occurring in wire chambers is reported. A proportional tube irradiated by an {sup 55}Fe source is used as a model wire chamber. Condensable species in the proportional tube effluent are concentrated in a cryotrap and analyzed by gas chromatography/mass spectrometry. Several different wire chamber gases (methane, argon/methane, ethane, argon/ethane, propane, argon/isobutane) are tested and their reaction products qualitatively identified. For all gases tested except those containing methane, use of hygroscopic filters to remove trace water and oxygen contaminants from the gas resulted in an increase in the average molecular weight of the products, consistent with results from low-pressure rf-discharge plasmas. It is suggested that because water and oxygen inhibit polymer growth in the gas phase that they may also reduce polymer deposition in proportional tubes and therefore retard wire aging processes. Mechanistic implications of the plasma reactions of hydrocarbons with oxygen are suggested. Unresolved issues in this work and proposals for further study are discussed.

  8. Investigation of pressure drop in capillary tube for mixed refrigerant Joule-Thomson cryocooler

    SciTech Connect (OSTI)

    Ardhapurkar, P. M.; Sridharan, Arunkumar; Atrey, M. D.

    2014-01-29

    A capillary tube is commonly used in small capacity refrigeration and air-conditioning systems. It is also a preferred expansion device in mixed refrigerant Joule-Thomson (MR J-T) cryocoolers, since it is inexpensive and simple in configuration. However, the flow inside a capillary tube is complex, since flashing process that occurs in case of refrigeration and air-conditioning systems is metastable. A mixture of refrigerants such as nitrogen, methane, ethane, propane and iso-butane expands below its inversion temperature in the capillary tube of MR J-T cryocooler and reaches cryogenic temperature. The mass flow rate of refrigerant mixture circulating through capillary tube depends on the pressure difference across it. There are many empirical correlations which predict pressure drop across the capillary tube. However, they have not been tested for refrigerant mixtures and for operating conditions of the cryocooler. The present paper assesses the existing empirical correlations for predicting overall pressure drop across the capillary tube for the MR J-T cryocooler. The empirical correlations refer to homogeneous as well as separated flow models. Experiments are carried out to measure the overall pressure drop across the capillary tube for the cooler. Three different compositions of refrigerant mixture are used to study the pressure drop variations. The predicted overall pressure drop across the capillary tube is compared with the experimentally obtained value. The predictions obtained using homogeneous model show better match with the experimental results compared to separated flow models.

  9. Recovery of energy from geothermal brine and other hot water sources

    DOE Patents [OSTI]

    Wahl, III, Edward F.; Boucher, Frederic B.

    1981-01-01

    Process and system for recovery of energy from geothermal brines and other hot water sources, by direct contact heat exchange between the brine or hot water, and an immiscible working fluid, e.g. a hydrocarbon such as isobutane, in a heat exchange column, the brine or hot water therein flowing countercurrent to the flow of the working fluid. The column can be operated at subcritical, critical or above the critical pressure of the working fluid. Preferably, the column is provided with a plurality of sieve plates, and the heat exchange process and column, e.g. with respect to the design of such plates, number of plates employed, spacing between plates, area thereof, column diameter, and the like, are designed to achieve maximum throughput of brine or hot water and reduction in temperature differential at the respective stages or plates between the brine or hot water and the working fluid, and so minimize lost work and maximize efficiency, and minimize scale deposition from hot water containing fluid including salts, such as brine. Maximum throughput approximates minimum cost of electricity which can be produced by conversion of the recovered thermal energy to electrical energy.

  10. The importance of FCC catalyst selection on LPG profitability

    SciTech Connect (OSTI)

    Keyworth, D.A.; Gilman, R.; Pearce, J.R. )

    1989-01-01

    Recently the value of LPG in chemical operations downstream of the FCC unit has increased. Such downstream operations utilize propylene not only in alkylate, but also in rapid growth petrochemical applications such as for a raw material in the manufacture of polypropylene and propylene oxide. Isobutane and the butenes (particularly butene-2 in sulfuric acid catalyzed alkylation units) are prized for alkylate feed. The profit potential and incentives to use other LPG components such as isobutene to make MTBE is now increased because of legislative actions and increased octane performance demand; and because of the greater isobutene content in the LPG from the new FCC octane catalysts. A low non-framework alumina (NFA) zeolite studied made a more olefinic LPG with higher iso-to normal C4 ratio than the other zeolites. Pilot plant data has also shown the new low NFA zeolite gave not only outstanding motor octane (MON) performance, but produced an LPG with better propylene to propane ratio, more isobutene, more n-butenes and more C4 branching than other RE promoted zeolite catalysts. Commercial results have verified the improved performance and profitability for the new low-NFA type zeolite catalysts. Three commercial examples are described.

  11. Catalytic conversion of light alkanes, Phase 3. Topical report, January 1990--December 1992

    SciTech Connect (OSTI)

    1992-12-31

    The mission of this work is to devise a new catalyst which can be used in the first simple, economic process to convert the light alkanes in natural gas to an alcohol-rich oxygenated product which can either be used as an environmentally friendly, high-performance liquid fuel, or a precursor to a liquid hydrocarbon transportation fuel. The authors have entered the proof-of-concept stage for converting isobutane to tert butyl alcohol in a practical process and are preparing to enter proof-of-concept of a propane to isopropyl alcohol process in the near future. Methane and ethane are more refractory and thus more difficult to oxidize than the C{sub 3} and C{sub 4} hydrocarbons. Nonetheless, advances made in this area indicate that further research progress could achieve the goal of their direct conversion to alcohols. Progress in Phase 3 catalytic vapor phase methane and ethane oxidation over metals in regular oxidic lattices are the subject of this topical report.

  12. Conversion of LPG hydrocarbons to distillate fuels or lubes using integration of LPG dehydrogenation and mogdl

    SciTech Connect (OSTI)

    Chang, C.D.; Penick, J.E.; Socha, R.F.

    1987-07-07

    This patent describes an apparatus for producing distillates of lubes from paraffins, which comprise: (a) a dehydrogenation reactor including means for passing a paraffinic feedstock stream into a dehydrogenation zone at conditions of pressure and temperature selected to convert the paraffins to an olefin rich effluent stream comprising at least one of the group consisting of propylene and butylene; (b) a low pressure oligomerization catalytic reactor including means for contacting the olefin rich effluent stream in a low pressure oligomerization catalytic reactor zone with a crystalline zeolite oligomerization catalyst at conditions of pressure and temperature selected to convert olefins to a first reactor effluent stream rich in liquid olefinic gasoline range hydrocarbons; (c) a first means for separating the first reactor effluent stream to form a substantially liquid C/sub 5/+ rich stream and a C/sub 4/- rich stream; (d) means for passing the C/sub 5/+ rich stream to a high pressure oligomerization catalytic reactor zone; (e) a high pressure oligomerization catalytic reactor including means for contacting the substantially liquid C/sub 5/+ rich stream in the high pressure oligomerization catalytic reactor zone with a crystalline zeolite oligomerization catalyst at conditions of temperature and pressure selected to produce a second reactor effluent stream which is rich in distillate; (f) second means for separating the second reactor effluent stream to recover an olefinic gasoline stream and a distillate stream; and (g) a hydrotreating reactor including means for contacting the distillate stream with hydrogen in a hydrotreating unit to produce a hydrotreated distillate stream comprising lube range hydrocarbons.

  13. Ignition of ethane, propane, and butane in counterflow jets of cold fuel versus hot air under variable pressures

    SciTech Connect (OSTI)

    Fotache, C.G.; Wang, H.; Law, C.K.

    1999-06-01

    This study investigates experimentally the nonpremixed ignition of ethane, propane, n-butane, and isobutane in a configuration of opposed fuel versus heated air jets. For each of these fuels the authors explore the effects of inert dilution, system pressure, and flow strain rate, for fuel concentrations ranging between 3--100% by volume, pressures between 0.2 and 8 atm, and strain rates of 100--600 s{sup {minus}1}. Qualitatively, these fuels share a number of characteristics. First, flame ignition typically occurs after an interval of mild oxidation, characterized by minimal heat release, fuel conversion, and weak light emission. The temperature extent of this regime decreases with increasing the fuel concentration, the ambient pressure, or the flow residence time. Second, the response to strain rate, pressure, and fuel concentration is similar for all investigated fuels, in that the ignition temperatures monotonically decrease with increasing fuel content, decreasing flow strain, and increasing ambient pressure. The C{sub 4} alkanes, however, exhibit three distinct p-T ignition regimes, similar to the homogeneous explosion limits. Finally, at 1 atm, 100% fuel, and a fixed flow strain rate the ignition temperature increases in the order of ethane < propane < n-butane < i-butane. Numerical simulation was conducted for ethane ignition using detailed reaction kinetics and transport descriptions. The modeling results suggest that ignition for all fuels studied at pressures below 5 atm is initiated by fuel oxidation following the high-temperature mechanism of radical chain branching and with little contribution by low-to-intermediate temperature chemistry.

  14. Regional analysis of non-methane hydrocarbons and meteorology of the rural southeast United States

    SciTech Connect (OSTI)

    Hagerman, L.M.

    1996-11-01

    Measurements of non-methane hydrocarbons, as well as ozone, meteorological and trace gas data, were made at four rural sites located within the southeastern United States as a part of the Southern Oxidants Study. Fifty-six C2-C10 hydrocarbons were collected from 1200-1300 local time, once every six days from September 1992 through October 1993. The measurements were made in an effort to enhance the understanding of the behavior and trends of ozone and other photochemical oxidants in this region. The light molecular weight alkanes (ethane, propane, n-butane, iso-butane), ethene and acetylene display a seasonal variation with a winter maximum and summer minimum. Isoprene was virtually non-existent during the winter at all sites, and averaged from 9.8 ppbC (Yorkville, GA) to 21.15 ppbC (Centreville, AL) during the summer. The terpene concentration was greatest in the summer with averages ranging between 3.19 ppbC (Centreville, AL) to 6.38 ppbC (Oak Grove, MS), but was also emitted during the winter months, with a range of 1.25 to 1.9 ppbC for all sites. Propylene-equivalent concentrations were calculated to account for differences in reaction rates between the hydroxyl radical and individual hydrocarbons, and to thereby estimate their relative contribution to ozone, especially in regards to the highly reactive biogenic compounds such as isoprene. It was calculated that biogenics represent at least 65% of the total non-methane hydrocarbon sum at these four sites during the summer season when considering propylene-equivalent concentrations. An ozone episode which occurred from July 20 to July 24 1993 was used as an example to show ozone profiles at each of the sites, and to show the effect of synoptic meteorology on high ozone by examining NOAA daily weather maps and climatic data.

  15. Superacid catalysis of light hydrocarbon conversion. Final report, August 26, 1993--August 26, 1996

    SciTech Connect (OSTI)

    Gates, B.C.

    1996-12-31

    Motivated by the goal of finding improved catalysts for low- temperature conversion of light alkanes into fuel components or precursors of fuel components, the researchers have investigated sulfated zirconia and promoted sulfated zirconia for conversion of butane, propane, and ethane. Catalyst performance data for sulfated zirconia promoted with iron and manganese show that it is the most active noncorrosive, nonhalide catalyst known for n-butane isomerization, and it is an excellent candidate catalyst for new low- temperature n-butane isomerization processes to make isobutane, which can be converted by established technology into methyl t-butyl ether (MTBE). Various transition metals have been found to work as promoters of sulfated zirconia for n-butane isomerization. The combination of iron and manganese is the best known combination of promoters yet discovered. The iron- and manganese-promoted sulfated zirconia is also a catalyst for conversion of propane and of ethane. Ethane is converted into ethylene and butanes in the presence of the iron- and manganese-promoted sulfated zirconia; propane is also converted into butane, among other products. However, the activities of the catalyst for these reactions are orders of magnitude less than the activity for n-butane conversion, and there is no evidence that the catalyst would be of practical value for conversion of alkanes lighter than butane. The product distribution data for ethane and propane conversion provide new insights into the nature of the catalyst and its acidity. These data suggest the involvement of Olah superacid chemistry, whereby the catalyst protonates the alkane itself, giving carbonium ions (as transition states). The mechanism of protonation of the alkane may also pertain to the conversion of butane, but there is good evidence that the butane conversion also proceeds via alkene intermediates by conventional mechanisms of carbenium ion formation and rearrangement.

  16. Water-enhanced solvation of organics

    SciTech Connect (OSTI)

    Lee, J.H.

    1993-07-01

    Water-enhanced solvation (WES) was explored for Lewis acid solutes in Lewis base organic solvents, to develop cheap extract regeneration processes. WES for solid solutes was determined from ratios of solubilities of solutes in water-sat. and low-water solvent; both were determined from solid-liquid equilibrium. Vapor-headspace analysis was used to determine solute activity coefficients as function of organic phase water concentration. WES magnitudes of volatile solutes were normalized, set equal to slope of log {gamma}{sub s} vs x{sub w}/x{sub s} curve. From graph shape {Delta}(log {gamma}{sub s}) represents relative change in solute activity coefficient. Solutes investigated by vapor-headspace analysis were acetic acid, propionic acid, ethanol, 1,2-propylene glycol, 2,3-butylene glycol. Monocarboxylic acids had largest decrease in activity coefficient with water addition followed by glycols and alcohols. Propionic acid in cyclohexanone showed greatest water-enhancement {Delta} (log {gamma}{sub acid})/{Delta}(x{sub w}/x{sub acid}) = {minus}0.25. In methylcyclohexanone, the decrease of the activity coefficient of propionic acid was {minus}0.19. Activity coefficient of propionic acid in methylcyclohexanone stopped decreasing once the water reached a 2:1 water to acid mole ratio, implying a stoichiometric relation between water, ketone, and acid. Except for 2,3-butanediol, activity coefficients of the solutes studied decreased monotonically with water content. Activity coefficient curves of ethanol, 1,2-propanediol and 2,3-butanediol did not level off at large water/solute mole ratio. Solutes investigated by solid-liquid equilibrium were citric acid, gallic acid, phenol, xylenols, 2-naphthol. Saturation concentration of citric acid in anhydrous butyl acetate increased from 0.0009 to 0.087 mol/L after 1.3 % (g/g) water co-dissolved into organic phase. Effect of water-enhanced solvation for citric acid is very large but very small for phenol and its derivatives.

  17. Studies on the catalytic activity of zirconia promoted with sulfate, iron, and manganese

    SciTech Connect (OSTI)

    Wan, K.T.; Khouw, C.B.; Davis, M.E.

    1996-01-01

    The catalytic properties of iron- and manganese-promoted sulfated zirconia (SFMZ) for the isomerization of n-butane to isobutane are investigated using various catalyst pretreatments and reaction conditions. The n-butane isomerization reactivity at 30{degrees}C is effected by calcination of the catalyst at 650{degrees}C in helium and vacuum treatment at room temperature indicating that superacidity is not likely to be responsible for activity. In addition, SFMZ samples exposed to dry air at over 450{degrees}C are more active than those calcined in helium at a reaction temperature of 30{degrees}C (n-butane conversions of 18.7% vs 0.4%) suggesting the presence of an active site involving a metal {open_quotes}oxy{close_quotes} species. The oxy species is capable of reacting CO to CO{sub 2} at room temperature and is present at a number density of 10-15 {mu}mol/g. At a reaction temperature of 100{degrees}C, SFMZ catalysts calcined in air then activated in helium show similar reactivities to those activated in air up to a preheating temperature of 450{degrees}C; above 450{degrees}C the metal oxy species is formed and provides additional activity (n-butane conversions of 37.1% in air vs 15.4% in He for calcinations at 650{degrees}C). The nature of the active sites on SFMZ are investigated using temperature-programmed desorption of substituted benzenes. The liberation of CO{sub 2} and SO{sub 2} in the benzene TPD profile of SFMZ is attributed to the oxidation of benzene at the redox-active metal sites, resulting in the subsequent decomposition of the reduced iron (II) sulfate. Data from the TPD studies do not suggest the presence of superacidity on SFMZ that could contribute to the low-temperature n-butane isomerization activity. Instead, a bifunctional mechanism that involves a combination of a redox-active metal site and an acid site in close proximity is proposed. 62 refs., 17 figs., 4 tabs.

  18. Next Generation Geothermal Power Plants

    SciTech Connect (OSTI)

    Brugman, John; Hattar, Mai; Nichols, Kenneth; Esaki, Yuri

    1995-09-01

    A number of current and prospective power plant concepts were investigated to evaluate their potential to serve as the basis of the next generation geothermal power plant (NGGPP). The NGGPP has been envisaged as a power plant that would be more cost competitive (than current geothermal power plants) with fossil fuel power plants, would efficiently use resources and mitigate the risk of reservoir under-performance, and minimize or eliminate emission of pollutants and consumption of surface and ground water. Power plant concepts were analyzed using resource characteristics at ten different geothermal sites located in the western United States. Concepts were developed into viable power plant processes, capital costs were estimated and levelized busbar costs determined. Thus, the study results should be considered as useful indicators of the commercial viability of the various power plants concepts that were investigated. Broadly, the different power plant concepts that were analyzed in this study fall into the following categories: commercial binary and flash plants, advanced binary plants, advanced flash plants, flash/binary hybrid plants, and fossil/geothed hybrid plants. Commercial binary plants were evaluated using commercial isobutane as a working fluid; both air-cooling and water-cooling were considered. Advanced binary concepts included cycles using synchronous turbine-generators, cycles with metastable expansion, and cycles utilizing mixtures as working fluids. Dual flash steam plants were used as the model for the commercial flash cycle. The following advanced flash concepts were examined: dual flash with rotary separator turbine, dual flash with steam reheater, dual flash with hot water turbine, and subatmospheric flash. Both dual flash and binary cycles were combined with other cycles to develop a number of hybrid cycles: dual flash binary bottoming cycle, dual flash backpressure turbine binary cycle, dual flash gas turbine cycle, and binary gas turbine cycle. Results of this study indicate that dual flash type plants are preferred at resources with temperatures above 400 F. Closed loop (binary type) plants are preferred at resources with temperatures below 400 F. A rotary separator turbine upstream of a dual flash plant can be beneficial at Salton Sea, the hottest resource, or at high temperature resources where there is a significant variance in wellhead pressures from well to well. Full scale demonstration is required to verify cost and performance. Hot water turbines that recover energy from the spent brine in a dual flash cycle improve that cycle's brine efficiency. Prototype field tests of this technology have established its technical feasibility. If natural gas prices remain low, a combustion turbine/binary hybrid is an economic option for the lowest temperature sites. The use of mixed fluids appear to be an attractive low risk option. The synchronous turbine option as prepared by Barber-Nichols is attractive but requires a pilot test to prove cost and performance. Dual flash binary bottoming cycles appear promising provided that scaling of the brine/working fluid exchangers is controllable. Metastable expansion, reheater, Subatmospheric flash, dual flash backpressure turbine, and hot dry rock concepts do not seem to offer any cost advantage over the baseline technologies. If implemented, the next generation geothermal power plant concept may improve brine utilization but is unlikely to reduce the cost of power generation by much more than 10%. Colder resources will benefit more from the development of a next generation geothermal power plant than will hotter resources. All values presented in this study for plant cost and for busbar cost of power are relative numbers intended to allow an objective and meaningful comparison of technologies. The goal of this study is to assess various technologies on an common basis and, secondarily, to give an approximate idea of the current costs of the technologies at actual resource sites. Absolute costs at a given site will be determined by the specifics of a given project.

  19. Spectroelectrochemical Sensor for Pertechnetate Applicable to Hanford and Other DOE Sites

    SciTech Connect (OSTI)

    Heineman, William R; Seliskar, Carl J; Bryan, Samuel A

    2012-09-18

    The general aim of our work funded by DOE is the design and implementation of a new sensor technology that offers unprecedented levels of specificity needed for analysis of the complex chemical mixtures found at DOE sites nationwide. The specific goal of this project was the development of a sensor for technetium (Tc) that is applicable to characterizing and monitoring the vadose zone and associated subsurface water at the Hanford Site and other DOE sites. The concept for the spectroelectrochemical sensor is innovative and represents a breakthrough in sensor technology. The sensor combines three modes of selectivity (electrochemistry, spectroscopy, and selective partitioning) into a single sensor to substantially improve selectivity. The sensor consists of a basic spectroelectrochemical configuration that we have developed under our previous DOE grants: a waveguide with an optically transparent electrode (OTE) that is coated with a thin chemically-selective film that preconcnetrates the analyte. The key to adapting this generic sensor to detect TcO4- and Tc complexes lies in the development of chemically-selective films that preconcentrate the analyte and, when necessary, chemically convert it into a complex with electrochemical and spectroscopic properties appropriate for sensing. Significant accomplishments were made in the general areas of synthesis and characterization of polymer films that efficiently preconcentrate the analyte, development and characterization of sensors and associated instrumentation, and synthesis and characterization of relevant Re and Tc complexes. Two new polymer films for the preconcentration step in the sensor were developed: partially sulfonated polystyrene-block-poly(ethylene-ran-butylene)-block-polystyrene (SSEBS) and phosphine containing polymer films. The latter was a directed polymer film synthesis that combined the proper electrostatic properties to attract TcO4- and also incorporated a suitable ligand for covalently trapping a lower oxidation state Tc complex within the film for spectroelectrochemical detection. Spectroelectrochemical sensors were developed and demonstrated, first using [Re(dmpe)3]+ (dmpe = 1,2-bis(dimethylphosphino)ethane) as a model compound with the non-radioactive Re surrogate for radioactive Tc. A fluorescence based spectroelectrochemical sensor for [Tc(dmpe)3]+/2+was then developed using SSEBS as the preconcentrating film. Portable instrumentation for the fluorescence spectroelectrochemical sensor was fabricated and tested. The effects of components in Hanford subsurface water on sensor performance with a detailed evaluation of the effect of total ionic strength on sensitivity demonstrated the ability to use the spectroelectrochemical sensor on representative water samples. A variety Re and Tc complexes were synthesized and characterized to explore the best ligands to use for detection of Tc. A lower oxidation-state Tc-complex [Tc(dmpe)3]+ (dmpe = 1,2-bis(dimethylphosphino)ethane) was synthesized to use as a model compound for developing Tc sensors. [Tc(dmpe)3]+/2+ exhibited the important properties of solution fluorescence at ambient temperatures and reversible electrochemistry. A range of low oxidation state dioxo Re- and Tc-complexes of formulae [ReO2(py)4]+, [ReO2(CN)4]-, [ReO2(P-P)2]+ and [ReO2(S-S)2]+ (py = pyridine) were synthesized. An exhaustive study of the spectroscopy and electrochemistry of Re(diimine)(CO)3(halide) complexes was performed. These complexes served as models for the Tc(diimine)(CO)3(halide) complexes that were readily formed from Tc(CO)x(halides)6-x complexes which are themselves constituents of tank waste samples from Hanford. Of particular interest were new Tc complexes with the +5 and +6 oxidation states. Tetrabutylammonium salt of tetrachlorooxotechnetate(V), (nBu4N)[TcOCl4] (I) was synthesized and the structure determined. [TcO2(CN)4]3- , [TcO2(en)2]2+ , [TcO2(im)4]+, and [TcO2(py)4]+ (en = ethylenediamine; im = imidazole; py = pyridine) complexes were synthesized and solution and solid state 99Tc NMR spectra were acquired giving

  20. Development of Modified Pag (Polyalkylene Glycol) High VI High Fuel Efficient Lubricant for LDV Applications

    SciTech Connect (OSTI)

    Gangopadhyay, Arup; McWatt, D. G.; Zdrodowski, R. J.; Liu, Zak; Elie, Larry; Simko, S. J.; Erdemir, Ali; Ramirez, Giovanni; Cuthbert, J.; Hock, E. D.

    2015-09-30

    Engine oils play a critical role in friction reduction. Improvements in engine oil technology steadily improved fuel economy as the industry moved through ILSAC GF-1 to GF-5 specifications. These improvements were influenced by changes in base oil chemistry, development of new friction modifiers and their treat levels, and the total additive package consisting of various other components. However, the improvements are incremental and further fuel consumption reduction opportunities are becoming more challenging. Polyalkylene glycol (PAG) based engine oils are being explored as a step forward for significant fuel consumption reduction. Although PAG fluids are used in many industrial applications, its application as an engine oil has been explored in a limited way. The objective of this project is to deep dive in exploring the applicability of PAG technology in engine oil, understanding the benefits, and limitations, elucidating the mechanism(s) for friction benefits, if any, and finally recommending how to address any limitations. The project was designed in four steps, starting with selection of lubricant technology, followed by friction and wear evaluations in laboratory bench tests which are relatively simple and inexpensive and also served as a screener for further evaluation. Selected formulations were chosen for more complex engine component level tests i.e., motored valvetrain friction and wear, piston ring friction using a motored single cylinder, and motored engine tests. A couple of formulations were further selected based on component level tests for engine dyno tests i.e., Sequence VID (ASTM D6709) for fuel economy, Sequence IVA (ASTM D6891) for valvetrain wear, and Sequence VG (ASTM D6593) for sludge and varnish protection. These are some of the industry standard tests required for qualifying engine oils. Out of these tests, a single PAG oil was selected for chassis roll dynamometer tests for fuel economy and emission measurements using FTP (Federal Test Procedure) metro/highway cycles. Five different PAG chemistries were selected by varying the starting alcohol, the oxide monomers (ethylene oxide, propylene oxide, or butylene oxide), capped or uncapped, homopolymer or random copolymer. All formulations contained a proprietary additive package and one which contained additional antiwear and friction modifier additives. Laboratory bench tests (Pin-on-Disk, High Frequency Reciprocating Rig (HFRR), Block-on-Ring, Mini-Traction Machine (MTM) identified formulations having friction, wear, and load carrying characteristics similar to or better than baseline GF-5 SAE 5W-20 oil. Motored valvetrain and motored piston ring friction tests showed nearly 50% friction reduction for some of the PAG formulations compared to GF-5 SAE 5W-20 oil. Motored engine tests showed up to 15% friction benefit over GF-5 SAE 5W-20 oil. It was observed that friction benefits are more related to PAG base oil chemistry than their lower viscosity compared to GF-5 SAE 5W-20 oil. Analysis of wear surfaces from laboratory bench tests and bucket tappets from motored valvetrain tests confirmed the presence of PAG molecules. The adsorption of these polar molecules is believed to be reason for friction reduction. However, the wear surfaces also had thin tribo-film derived from additive components. The tribo-film consisting of phosphates, sulfides, and molybdenum disulfide (when molybdenum additive was present) were observed for both GF-5 SAE 5W-20 and PAG fluids. However, when using PAG fluids, motored valvetrain tests showed high initial wear, which is believed to be due to delay in protective tribo-film formation. After the initial wear, the wear rate of PAG fluids was comparable to GF-5 SAE 5W-20 oil. The PAG oil containing additional antiwear and friction reducing additives showed low initial wear as expected. However, when this oil was evaluated in Sequence IVA test, it showed initially low wear comparable to GF-5 oil but wear accelerated with oil aging indicating rapid deterioration of additive components. ASTM Sequence VG test showed good sludge protection capability but failed to meet varnish rating for GF-5 requirement. Chassis roll dynamometer tests with PAG oil 15-1 showed about 1% fuel economy benefit over GF-5 SAE 5W-20 oil in EPA city cycles only and when the oil was slightly aged (500 miles). No fuel economy benefits could be observed in combined EPA metro/highway cycles. Also, no fuel economy benefit could be observed with continued (500- 10000 miles) oil aging. However, the emission level was comparable to the reference oil and was within EPA limits. Analysis of the PAG oil following tests showed low iron content although additive components were significantly degraded. The results indicate that PAG fluids have significant friction reduction potential but there are challenges with wear and varnish protection capabilities. These limitations are primarily because the selected additive components were chosen to provide a fluid with no metal content that forms little or no sulphated ash. Significant development work is needed to identify additive components compatible with PAG chemistry including their solubility in PAG oil. Miscibility of PAG fluids with mineral base oil is another challenge for oil change service. There is PAG chemistry (oil soluble PAG, OSP) which is soluble in mineral oils but the formulation explored in this investigation did not show significant friction reduction in motored engine tests. Again, highlighting the need for additive development for specific PAG chemistry. The thermal oxidation behavior of these oils has not been explored in this investigation and needs attention.