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01739 The influence of conveying distance on low velocity pneumatic conveying of fly ash
02 Liquid fuels (transport,
in the presence of small amounts assumed to he the seed of carbon promote the wax formation.
00101730
of 1-olefins. chain
The propagation
added I-olefins are of C, monomer to
Production of fuels from petroleum refining wastes
Starzak, M. Pol. PL 174,.572 (Cl. CiOGl/OO), 31 Aug 1998, Appl. 304,548, 2 Aug 1994. 3. (In Polish) Production of fuels from petroleum refining waste residues, hy neutralization of their acid content, using lime and chalk and emulsification of hydrocarbons by using nonionic and/or anionic emulsifiers is examined in this paper. Lime is added as a powder in the presence of ethanolamine and 4S-50% sodium hydroxide solution (at a ratio of 1 : (0.1-3)) (10-300) wt parts/l00 wt parts lime. Chalk is used at a lime/chalk ratio of l:(O.l-3). Then, the emulsifier (l-5% aqueous solution) lo-70 wt parts/l00 wt parts residue is added. Optionally, less than 2000 wt parts fuel oil is added to 100 wt parts residue. The resultant temperature of the fuel is stable and remains the same during storage and transportation. The calorific value is greater than 25 MJikg. and viscosity at 80” is 100 mm-/s.
00/01731
Production of lubricant base oils
Richter, F. Eur. Pat. Appl. EP 921.184 (Cl. CIOMI 11106) 9 Jun 1999, ZA Appl. 1998/9,528, 19 Ott 1998:. 14. The process of lubricant base oil production involves hydrotreating a feedstock comprising a Fischer-Tropsch wax and a petroleum-based waxy distillate. A range of hydrogenated products are produced during this procedure and waxy products can he recovered from them.
00/01732
Refining and blending of aviation turbine fuels
White, R. D. Drug Chern. Fbosicol, 1999. 22, (I). 143-153. Aviation turbine fuels (jet fuels) are similar to other petroleum products that have a boiling range of 300-550’F. Kerosene and number one grades of fuel oil. gas turbine oil and diesel fuel share many similar physical and chemical properties with jet fuel. The extrapolation of toxicology data on one material should provide information on the other products due to their similarity. Refineries in the USA manufacture jet fuel to meet industry standard specifications. Civilian aircraft primarily use Jet A or Jet A-l fuel as defined by ASTM D 1655. Military aircraft use JP-5 or JP-8 fuel as defined by MIL-T-5624R or MIL-T-83133D respectively. The f.p. and flash point are the principle differences between the finished fuels. Common refinery processes that produce jet fuel include distillation, caustic treatment, hydrocracking and hydrotreating. Each of these refining processes may be the final stage in the production of jet fuel. Occasionally, the blending of two or more of these refinery process streams are required to produce jet fuel that meets the desired specifications. Chemical additives allowed for use in jet fuel are also defined in the product specifications. In order to meet the specific storage or flight condition requirements of the customer, the customer has to put additives into the fuel as opposed to the refinery doing it on production.
Selective production of Cs hydrocarbons from syngas In a dual reactor using Co-Ni/ZrO, and S04*-Er02 catalysts
OOlO1733
Malyala, R. V. I/it/. E/IR. Cheni. Rc\.. 1999. 38. (4). 1323-1334. A sulfated zirconia (Sod’-/Zr02) solid acid catalyst in a dual fixed-bed microreaction system, was used to modify the product stream from the Fischer-Tropsch (FT) reaction over Co-Ni/ZrO? catalyst. Although the operating conditions for the first reactor containing the FT catalyst was fixed at 523 K and I atm, the effects of operating variables, such as a second *-/ZrO, catalyst ratio. and weight reactor temperature. the Co-Ni/ZrOz:S04 hourly space velocity (WHSV) on the steady-state-product distribution were analysed. A high selectivity (33 wt%) to total CJ hydrocarbons was achieved when the second reactor was operated at 423 K. with a catalyst ratio of l:l.5 and at a WHSV of 15 hh’. in comparison to a maximum selectivity of 14 wt% obtained using a single reactor with a Co-NiiZrOz catalyst, this selectivity was substantially higher. Catalyst characterization using temperature-programmed desorption of NH3 and ‘H-MAS NMR demonstrated that this high selectivity toward total Cq hydrocarbons was a result of catalyst. However, the rapid catalyst the strong acidity of the SO 4*-/ZrOa deactivation was attributed to coke deposition on the SOn--lZrOl catalyst. External and intraparticle mass transfer effects were negligible under these experimental conditions. Based on the product distribution in a dualreaction system, a reaction pathway was proposed.
Separation of Fischer-Tropsch wax from Catalyst using near-critical fluid extraction: Analysis of process feasibility
00101734
Biales, J. M. Oier,er F~‘l,cl.v.1999. 13. (3). 667-677. An analysis of the technical feasibility of a near-critical fluid extraction (NCE) process for the recovery of heavy normal paraffins from a FischerTropsch slurry reactor. Process simulations were performed using the ASPEN PLUS program, considering 100 individual compounds from CL to n-hexane, n-heptane, and n-octane C,,,,,. Four light solvents: n-pentane, were evaluated. These four compounds are major products of the F-T reaction. Most of the analysis was concentrated in two regions: (1) high solvent/product ratios (ca. 20/l), such that product could he recovered by temperature-retrograde condensation; and, (2) low solvent/product ratios (approximately 311). The latter region appeared to require higher extraction but had several attractive temperatures and higher slurry flow-rates, features such as lower vapour flow-rates. lower solvent makeup rates and
refining,
quality,
storage)
lower energy requirements. The product from the NCE process never had a solvent with a concentration low enough for the process to he self-sufficient in the solvent, when the flow-sheet contained one product recovery unit. However, with multiple recovery units, self-sufficiency was obtained. It appears that the NCE process is feasible and has many attractive features, 00/01735 Stability and handling of Sasol semi-synthetic jet fuel Roets, P. Proc. Irrt. Cork/: Srrrh. Hur~tll. Liy. FIW/.Y. 6th 1097. 1998, 2. 7X9804. Various methods, employing hydrogen treatment and polymerization can he used to produce jet fuel with very high thermal stability. negligible levels of sulfur and aromatics. In the 1980s research was carried out on both shale- and coal-derived jet fuel and from the results, two drawbacks to the potential commercial use of these fuels were identified. These were the fuel’s poor lubricity properties and the shrinkage of seals previously wetted by crude oil-derived fuels. Additional concerns expressed at the time were the fuel’s additive response and its capacitance, or dielectric constant. when used in density correlations. In order to produce a more acceptable fuel for use in commercial aircraft operating out of Johanneshurg international airport, Sasol will blend a synthetic jet fuel component with crude oilderived jet fuel to increase the blend’s aromatic content. The properties of the synthetic jet fuel component and the semi-synthetic jet fuel blend are discussed in this paper. Finally biocide additive efficacy in the synthetic fuels was detected.
00101736 Status and prospects of gas-to-liquids processes Senden, M. M. G. and Punt, A. D. Pwpr. - .4n1. C/tori. Sot.. Dir. PC,/ Chen1.. 1999, 44. (1). 10-12. The Shell middle distillate synthesis process, which uses the FischerTropsch process in the conversion of natural gas into middle distillate is characterized.
OOlO1737 Steady-state and dynamic behavior of the fixed-bed catalytic reactor for Fischer-Tropsch synthesis Liu, Q. Sh;roir Htrtrgoiig Coo&ig .Yvrviw Xw/xw. I YY9. I?. ( I ). I4 2 1 (In Chinese) A two-dimensional heterogeneous model is used to simulate a FischerTropsch synthesis fixed-bed reactors. The numerical calculation methods of the model equations are also analysed and the method to solve the FischerTropsch synthesis fixed-bed reactor model equations is detected. The purposes of this paper is to assess the steady state and dynamic behaviour of the F-T fixed-bed catalytic reactor. The operation conditions of the reactor steady state hehaviour are investigated. Reactor dynamic behaviour for step changes in the feed temperature. fluid rate and the wall temperature are also studied.
OW01738 The effect of boron on the catalyst reducibility and actlvlty of Co/T102 Fischer-Tropsch catalysts Li, J. and Coville, N. J. A&. Corrrl.. A. 1999. 181. (I). 201 -208. The techniques DRIFTS, XRD, LRS TGA and a fixed bed flow reactor were used to investigate the effect of boron (as H2BOJ) on the CO hydrogenation ability of Co/TiOz catalysts. The introduction of boron (O.OZlS%) into a 10 wt% CofliOa catalyst decreased the Co30s crystallite size (26-16 nm) in the oxidic catalysts (calcined at 300°C) and decreased the uptake of hydrogen (0.35-0.9 mL/g cat) in the reduced catalyst. The presence of boron made the reduction of the Co/TiO: catalyst more difficult. The CO conversion and overall hydrogenation rate decreased with decreasing ease of reducibility and decreasing cobalt dispersion caused by boron. Turnover frequency (approximately 20x IO-? s--‘), however. remained constant throughout and was independent of the extent of reduction and dispersion of the catalysts. This provides further evidence of the structure-insensitivity of supported Co Fischer-Tropsch catalysts. The addition of small amounts of boron (~0.1%) do, however, result in an increase in o less CHI production and an increase in the olefiniparaffin ratio.
OOlO1739 The influence of conveying distance on low velocity pneumatic conveying of fly ash Agarwal, V. K. Powder Hand. Prow.u. 1999. Ii. (I). 57-60. In order to convey fly ash through a 130 metres long pipeline over a wide variety of conveying conditions, an extensive experimental investigation was performed. A pressure minimum point emerged at very low conveying velocities. The full hatch of material could not be conveyed through the pipeline at these velocities. An analysis of the low velocity results for the conveying of the fly ash is included to illustrate the relationships obtained, and to demonstrate that the optimum conveying air velocity is not always the lowest achievable velocity with fly ash.
OWO1740 Thermodynamic analysis of phase states of products of Fischer-Tropsch synthesis Ermakova, A. Z/i. Prikl. Khim. l.S.-P~~t~rhr,~). 1998. 71, (I I). 1776-1782 (In RussiaN) The phase transition states of Fischer-Tropsch synthesis products are thermodynamically analysed in this paper. The Redlich-Kwong-Soave equation of state is used for the basis of the study. It is used to calculate the Gibbs energy, entropy and enthalpy of phase transitions. which are necessary for designing the reactor.
Fuel and Energy Abstracts
July 2000
199
in the presence of small amounts assumed to he the seed of carbon promote the wax formation.
00101730
of 1-olefins. chain
The propagation
added I-olefins are of C, monomer to
Production of fuels from petroleum refining wastes
Starzak, M. Pol. PL 174,.572 (Cl. CiOGl/OO), 31 Aug 1998, Appl. 304,548, 2 Aug 1994. 3. (In Polish) Production of fuels from petroleum refining waste residues, hy neutralization of their acid content, using lime and chalk and emulsification of hydrocarbons by using nonionic and/or anionic emulsifiers is examined in this paper. Lime is added as a powder in the presence of ethanolamine and 4S-50% sodium hydroxide solution (at a ratio of 1 : (0.1-3)) (10-300) wt parts/l00 wt parts lime. Chalk is used at a lime/chalk ratio of l:(O.l-3). Then, the emulsifier (l-5% aqueous solution) lo-70 wt parts/l00 wt parts residue is added. Optionally, less than 2000 wt parts fuel oil is added to 100 wt parts residue. The resultant temperature of the fuel is stable and remains the same during storage and transportation. The calorific value is greater than 25 MJikg. and viscosity at 80” is 100 mm-/s.
00/01731
Production of lubricant base oils
Richter, F. Eur. Pat. Appl. EP 921.184 (Cl. CIOMI 11106) 9 Jun 1999, ZA Appl. 1998/9,528, 19 Ott 1998:. 14. The process of lubricant base oil production involves hydrotreating a feedstock comprising a Fischer-Tropsch wax and a petroleum-based waxy distillate. A range of hydrogenated products are produced during this procedure and waxy products can he recovered from them.
00/01732
Refining and blending of aviation turbine fuels
White, R. D. Drug Chern. Fbosicol, 1999. 22, (I). 143-153. Aviation turbine fuels (jet fuels) are similar to other petroleum products that have a boiling range of 300-550’F. Kerosene and number one grades of fuel oil. gas turbine oil and diesel fuel share many similar physical and chemical properties with jet fuel. The extrapolation of toxicology data on one material should provide information on the other products due to their similarity. Refineries in the USA manufacture jet fuel to meet industry standard specifications. Civilian aircraft primarily use Jet A or Jet A-l fuel as defined by ASTM D 1655. Military aircraft use JP-5 or JP-8 fuel as defined by MIL-T-5624R or MIL-T-83133D respectively. The f.p. and flash point are the principle differences between the finished fuels. Common refinery processes that produce jet fuel include distillation, caustic treatment, hydrocracking and hydrotreating. Each of these refining processes may be the final stage in the production of jet fuel. Occasionally, the blending of two or more of these refinery process streams are required to produce jet fuel that meets the desired specifications. Chemical additives allowed for use in jet fuel are also defined in the product specifications. In order to meet the specific storage or flight condition requirements of the customer, the customer has to put additives into the fuel as opposed to the refinery doing it on production.
Selective production of Cs hydrocarbons from syngas In a dual reactor using Co-Ni/ZrO, and S04*-Er02 catalysts
OOlO1733
Malyala, R. V. I/it/. E/IR. Cheni. Rc\.. 1999. 38. (4). 1323-1334. A sulfated zirconia (Sod’-/Zr02) solid acid catalyst in a dual fixed-bed microreaction system, was used to modify the product stream from the Fischer-Tropsch (FT) reaction over Co-Ni/ZrO? catalyst. Although the operating conditions for the first reactor containing the FT catalyst was fixed at 523 K and I atm, the effects of operating variables, such as a second *-/ZrO, catalyst ratio. and weight reactor temperature. the Co-Ni/ZrOz:S04 hourly space velocity (WHSV) on the steady-state-product distribution were analysed. A high selectivity (33 wt%) to total CJ hydrocarbons was achieved when the second reactor was operated at 423 K. with a catalyst ratio of l:l.5 and at a WHSV of 15 hh’. in comparison to a maximum selectivity of 14 wt% obtained using a single reactor with a Co-NiiZrOz catalyst, this selectivity was substantially higher. Catalyst characterization using temperature-programmed desorption of NH3 and ‘H-MAS NMR demonstrated that this high selectivity toward total Cq hydrocarbons was a result of catalyst. However, the rapid catalyst the strong acidity of the SO 4*-/ZrOa deactivation was attributed to coke deposition on the SOn--lZrOl catalyst. External and intraparticle mass transfer effects were negligible under these experimental conditions. Based on the product distribution in a dualreaction system, a reaction pathway was proposed.
Separation of Fischer-Tropsch wax from Catalyst using near-critical fluid extraction: Analysis of process feasibility
00101734
Biales, J. M. Oier,er F~‘l,cl.v.1999. 13. (3). 667-677. An analysis of the technical feasibility of a near-critical fluid extraction (NCE) process for the recovery of heavy normal paraffins from a FischerTropsch slurry reactor. Process simulations were performed using the ASPEN PLUS program, considering 100 individual compounds from CL to n-hexane, n-heptane, and n-octane C,,,,,. Four light solvents: n-pentane, were evaluated. These four compounds are major products of the F-T reaction. Most of the analysis was concentrated in two regions: (1) high solvent/product ratios (ca. 20/l), such that product could he recovered by temperature-retrograde condensation; and, (2) low solvent/product ratios (approximately 311). The latter region appeared to require higher extraction but had several attractive temperatures and higher slurry flow-rates, features such as lower vapour flow-rates. lower solvent makeup rates and
refining,
quality,
storage)
lower energy requirements. The product from the NCE process never had a solvent with a concentration low enough for the process to he self-sufficient in the solvent, when the flow-sheet contained one product recovery unit. However, with multiple recovery units, self-sufficiency was obtained. It appears that the NCE process is feasible and has many attractive features, 00/01735 Stability and handling of Sasol semi-synthetic jet fuel Roets, P. Proc. Irrt. Cork/: Srrrh. Hur~tll. Liy. FIW/.Y. 6th 1097. 1998, 2. 7X9804. Various methods, employing hydrogen treatment and polymerization can he used to produce jet fuel with very high thermal stability. negligible levels of sulfur and aromatics. In the 1980s research was carried out on both shale- and coal-derived jet fuel and from the results, two drawbacks to the potential commercial use of these fuels were identified. These were the fuel’s poor lubricity properties and the shrinkage of seals previously wetted by crude oil-derived fuels. Additional concerns expressed at the time were the fuel’s additive response and its capacitance, or dielectric constant. when used in density correlations. In order to produce a more acceptable fuel for use in commercial aircraft operating out of Johanneshurg international airport, Sasol will blend a synthetic jet fuel component with crude oilderived jet fuel to increase the blend’s aromatic content. The properties of the synthetic jet fuel component and the semi-synthetic jet fuel blend are discussed in this paper. Finally biocide additive efficacy in the synthetic fuels was detected.
00101736 Status and prospects of gas-to-liquids processes Senden, M. M. G. and Punt, A. D. Pwpr. - .4n1. C/tori. Sot.. Dir. PC,/ Chen1.. 1999, 44. (1). 10-12. The Shell middle distillate synthesis process, which uses the FischerTropsch process in the conversion of natural gas into middle distillate is characterized.
OOlO1737 Steady-state and dynamic behavior of the fixed-bed catalytic reactor for Fischer-Tropsch synthesis Liu, Q. Sh;roir Htrtrgoiig Coo&ig .Yvrviw Xw/xw. I YY9. I?. ( I ). I4 2 1 (In Chinese) A two-dimensional heterogeneous model is used to simulate a FischerTropsch synthesis fixed-bed reactors. The numerical calculation methods of the model equations are also analysed and the method to solve the FischerTropsch synthesis fixed-bed reactor model equations is detected. The purposes of this paper is to assess the steady state and dynamic behaviour of the F-T fixed-bed catalytic reactor. The operation conditions of the reactor steady state hehaviour are investigated. Reactor dynamic behaviour for step changes in the feed temperature. fluid rate and the wall temperature are also studied.
OW01738 The effect of boron on the catalyst reducibility and actlvlty of Co/T102 Fischer-Tropsch catalysts Li, J. and Coville, N. J. A&. Corrrl.. A. 1999. 181. (I). 201 -208. The techniques DRIFTS, XRD, LRS TGA and a fixed bed flow reactor were used to investigate the effect of boron (as H2BOJ) on the CO hydrogenation ability of Co/TiOz catalysts. The introduction of boron (O.OZlS%) into a 10 wt% CofliOa catalyst decreased the Co30s crystallite size (26-16 nm) in the oxidic catalysts (calcined at 300°C) and decreased the uptake of hydrogen (0.35-0.9 mL/g cat) in the reduced catalyst. The presence of boron made the reduction of the Co/TiO: catalyst more difficult. The CO conversion and overall hydrogenation rate decreased with decreasing ease of reducibility and decreasing cobalt dispersion caused by boron. Turnover frequency (approximately 20x IO-? s--‘), however. remained constant throughout and was independent of the extent of reduction and dispersion of the catalysts. This provides further evidence of the structure-insensitivity of supported Co Fischer-Tropsch catalysts. The addition of small amounts of boron (~0.1%) do, however, result in an increase in o less CHI production and an increase in the olefiniparaffin ratio.
OOlO1739 The influence of conveying distance on low velocity pneumatic conveying of fly ash Agarwal, V. K. Powder Hand. Prow.u. 1999. Ii. (I). 57-60. In order to convey fly ash through a 130 metres long pipeline over a wide variety of conveying conditions, an extensive experimental investigation was performed. A pressure minimum point emerged at very low conveying velocities. The full hatch of material could not be conveyed through the pipeline at these velocities. An analysis of the low velocity results for the conveying of the fly ash is included to illustrate the relationships obtained, and to demonstrate that the optimum conveying air velocity is not always the lowest achievable velocity with fly ash.
OWO1740 Thermodynamic analysis of phase states of products of Fischer-Tropsch synthesis Ermakova, A. Z/i. Prikl. Khim. l.S.-P~~t~rhr,~). 1998. 71, (I I). 1776-1782 (In RussiaN) The phase transition states of Fischer-Tropsch synthesis products are thermodynamically analysed in this paper. The Redlich-Kwong-Soave equation of state is used for the basis of the study. It is used to calculate the Gibbs energy, entropy and enthalpy of phase transitions. which are necessary for designing the reactor.
Fuel and Energy Abstracts
July 2000
199