Commercial Deployment of Fischer–Tropsch Synthesis: The Coproduction Option

Shen, John Paul; Schmetz, Edward; Kawalkin, Gregory J.; Stiegel, Gary J.; Noceti, Richard P.; Winslow, J.; Kornosky, R.M.; Krastman, D.; Venkataraman, Venkat; Driscoll, Daniel J.; Cicero, D.C.; Haslebacher, William F.; Hsieh, B.C.B.; Jain, S.C.; Tennant, Jenny B.

doi:10.1023/b:toca.0000012983.86034.d1

Cited by 5 publications

(3 citation statements)

References 8 publications

Supporting

Mentioning

Contrasting

Order By: Relevance

“…The signal from long-chain HCs and graphite/coke phase is significantly smaller than for all other conditions at all temperatures. These observations are in line with the literature reporting a higher conversion rate of the reaction and slower carburization process. − …”

Section: Resultssupporting

confidence: 92%

In Situ Surface-Sensitive Investigation of Multiple Carbon Phases on Fe(110) in the Fischer–Tropsch Synthesis

et al. 2022

View full text Add to dashboard Cite

Carbide formation on iron-based catalysts is an integral and, arguably, the most important part of the Fischer− Tropsch synthesis process, converting CO and H 2 into synthetic fuels and numerous valuable chemicals. Here, we report an in situ surface-sensitive study of the effect of pressure, temperature, time, and gas feed composition on the growth dynamics of two distinct iron−carbon phases with the octahedral and trigonal prismatic coordination of carbon sites on an Fe(110) single crystal acting as a model catalyst. Using a combination of state-of-the-art X-ray photoelectron spectroscopy at an unprecedentedly high pressure, high-energy surface X-ray diffraction, mass spectrometry, and theoretical calculations, we reveal the details of iron surface carburization and product formation under semirealistic conditions. We provide a detailed insight into the state of the catalyst's surface in relation to the reaction.

show abstract

Section: Resultssupporting

confidence: 92%

In Situ Surface-Sensitive Investigation of Multiple Carbon Phases on Fe(110) in the Fischer–Tropsch Synthesis

et al. 2022

View full text Add to dashboard Cite

show abstract

“…Alkali metals have long been used as promoters for industrial catalysts to enhance activity, selectivity and stability. This includes Fischer-Tropsch, ethylene epoxidation and ammonia synthesis catalysts [51][52][53]. The potential of potassium doping, through simple impregnation, of Mn:Ce mixed oxide as CWO catalysts has therefore been explored with the following objectives (i) enhance mineralization selectivity while preserving high conversions by co-promoted catalysts; (ii) improve catalyst stability and longevity by slowing down formation of polymeric deposits [54,55].…”

Section: Catalyst Modification For Mitigating Deactivationmentioning

confidence: 99%

Catalytic wet oxidation: micro–meso–macro methodology from catalyst synthesis to reactor design

Larachi

2005

Top Catal

View full text Add to dashboard Cite

Compared to alternative mature wet oxidation technologies that have tremendously proliferated in industry, heterogeneously mediated catalytic wet oxidation (CWO) has achieved, thus far, poor commercial penetration. The two factors that are likely responsible for this situation are (i) the lack of efficient and robust catalysts that pass with success the acid-test for commercial exploitation remote from the aseptic academic conditions, (ii) and the lack of a comprehensive reactor design framework and methodology for scale-up, reactor selection and operation inherent to the multiphase nature of the CWO reactors. This synthetic review summarizes the recent research and development work conducted at Laval University on the CWO from both the perspectives of catalyst development and testing, and multiphase reactor simulations and selection. Specific emphasis was put, on the one hand, on the development brought to some manganese oxide-ceria composites against deactivation, and on the other hand, on the formulation of multidimensional unsteady-steady non-isothermal mass-energy transport/reaction models, embedding catalyst deactivation or not, for trickle bed reactors, packed bubble column reactors, three-phase fluidized beds and slurry bubble columns. A micro-Meso-macro scale methodology was adopted from the materials synthesis up to reactor selection in which the catalyst performance (conversion, selectivity, and deactivation), the intrinsic chemical kinetics, the fluid phase thermodynamics, the pellet scale transport, and the reactor scale physical phenomena (heat, mass transport and hydrodynamics) were integrated. As a result, several aspects relevant to reactor behaviour such as solvent evaporation due to CWO reaction exothermic effects, catalyst partial wetting and catalyst deactivation, and back-mixing effects were covered, and recommendations were formulated. NomenclatureA reactor cross-sectional area, m 2 C concentration, mol/m 3 or g/L C p isobaric specific heat capacity, J/kg/K D eff effective diffusivity, m 2 /s E activation energy, kJ/mol E z axial dispersion coefficient, m 2 /s H Henry constant, or bed height, m H j hidden layer transfer function, k rate constants, mol/min/kg cat. (equations (1)-Arrhenius pre-exponential factor, mol/min/kg cat. equation (9) ka ll liquid-liquid volumetric mass transfer coefficient. s )1 k l a gas-liquid volumetric mass transfer coefficient, s )1 ka sls liquid-solid mass transfer coefficient, s )1 K adsorption equilibrium constant, m 3 /mol L v water enthalpy of vaporization, J/mol [m c ] catalyst loading, kg cat./m 3 P pressure, atm r spherical co-ordinate at pellet scale, m r c chemical reaction rate, mol/m 3 /s S neural network output S M mineralization selectivity t time, min T absolute temperature, K U i neural network inputs U superficial velocity, m/s v molar volume, cm 3 /mol [W] carbonaceous deposit carbon concentration, mol C/m 3 solution x dissolved mole fraction X chemical conversion y gas mole fraction z longitudinal co-ordinate, mGreek a deactivation function, DH...

show abstract

“…For example, DOE has worked with Syntroleum Corporation and Marathon Oil Company to build an FTS pilot plant in Catoosa, OK for the production of 70 barrels per day (''BPD'') of ultra-clean transportation fuel from natural gas [4,5]. In addition, DOE has been supporting several programs focused on the development of FTS technology for the production of ultra-clean transportation fuels from synthesis gas derived from coal [6][7][8]. However, FTS technology is currently only economically viable at large scales [9].…”

Section: Introductionmentioning

confidence: 99%