Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
  • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
  • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
  • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
  • C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
  • C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/74—Iron group metals
  • B01J23/75—Cobalt
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/889—Manganese, technetium or rhenium
  • B01J23/8892—Manganese
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J35/00—Catalysts, in general, characterised by their form or physical properties
  • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
  • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
  • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
  • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00

Definitions

• the present invention relates to a shaped catalyst or catalyst precursor, containing a catalytically active component or a precursor therefor, the component selected from elements of Group VIII of the Periodic Table of the Elements, supported on a carrier, the catalyst or catalyst precursor optionally containing one or more elements or compounds from Groups IIA, IIIB, IVB, VB, VIB, VIIB or Group VIII of the Periodic Table of the Elements.
• the catalyst or catalyst precursor of the invention is very useful in mass-transfer or diffusion limited reactions, such as the Fischer-Tropsch hydrocarbon synthesis process.
• the invention further relates to a process to prepare the catalyst or catalyst precursor from a shapeable dough, to the die-plate used for the preparation of an extruded catalyst or catalyst precursor, to the use of the catalyst, as well as to the hydrocarbons prepared by using the catalyst.
• the invention further relates to a process to prepare fuels and base oils, by hydrogenation, hydroisomerisation and/or hydrocracking of the aforementioned hydrocarbons.
• BACKGROUND OF THE INVENTION Shaped catalysts or catalyst precursors are known in the art and have been described, for example in European Patent EP-0, 127, 220.
• Catalysts used in the Fischer-Tropsch synthesis often comprise one or more metals from Group VIII of the
• Periodic Table of the Elements optionally in combination with one or more metal oxides and/or other metals as promoters .
• a highly efficient catalyst is one which exhibits not only a high level of activity for the conversion of carbon monoxide and hydrogen to hydrocarbons, but also a high degree of selectivity to higher molecular hydrocarbons, in particular C5 hydrocarbons and larger, henceforth referred to as "C5+ hydrocarbons".
• C5+ hydrocarbons Preferably, the degree of branching in the C5+ hydrocarbons should be low. It is taught in the prior art that the efficiency of a catalyst in general increases as the size of the catalyst particle decreases. Further, catalysts should show a high stability, i.e. deactivation should be very low.
• the Fischer-Tropsch synthesis may be carried out using a variety of reaction regimes, for example a fluidised bed regime or a slurry bed regime.
• a major consideration in the design of the process is the pressure drop through the catalyst bed. It is most desirable that the pressure drop should be as low as possible.
• it is well reported in the art that, for a given shape of catalyst particles, as the size of the catalyst particles in a fixed bed is reduced, there is a corresponding increase in pressure drop through the catalyst bed.
• the catalyst particles should be sufficiently strong to avoid undesired attrition and/or breakage.
• the bulk crush strength should be (very) high, as beds are used in commercial reactors of up to 15 meters high.
• the strength of the catalyst particles plays an important part. This is an additional complication in designing further improved catalyst particles.
• a still further complicating element is the manufacturing process of catalyst particles.
• a catalyst or catalyst precursor comprising a Group VIII element and optionally a promoter selected from the elements of Group IIA, Group IIIB, Group IVB, Group VB, Group VIB or Group VIIB of the Periodic Table of the Elements which catalyst displays a high activity and selectivity in the Fischer-Tropic synthesis process, while keeping the pressure drop in the fixed bed as low as possible and displaying a high crush strength.
• the stability should be very high.
• the catalyst particles may be in the form of cylinders; hollow cylinders, for example cylinders having a central hollow space which has a radius of between 0.1 and 0.4 of the radius of the cylinder; straight or rifled (twisted) trilobes; or one of the other forms disclosed in US-4, 028, 221. Trilobe extrudates are said to be preferred.
• EP-0,218,147 discloses a helical lobed, polylobal extrudate particle having the outline shape of three or four strands helically wound about the axis of extrusion along the length of the particle and its use as a catalyst or catalyst support, in particular as a catalyst or catalyst support in hydrotreating operations.
• the helical shape of the catalyst is said to reduce the pressure drop across fixed bed reactors through which liquid and/or gas reactants are passed. In this way, smaller catalyst particles can be employed in a' given reactor design to meet the pressure drop requirements.
• the shape of quadrulobe-type catalysts is important, in particular with respect to a phenomenon known as pressure drop. From the experimental evidence provided it appears that asymmetric quadrulobes suffer less from pressure drop than the closely related symmetrical quadrulobes. The asymmetrically shaped particles are described in
• EP-0,220,933 by way of each pair of protrusions being separated by a channel which is narrower than the protrusions to prevent entry thereinto by the protrusions of an adjacent particle. It is taught in EP-0,220,933 that the shape of the particles prevents them from
• the present invention therefore relates to a shaped catalyst or catalyst precursor containing a catalytically active component or a precursor therefor, the component selected from elements of Group VIII of the Periodic Table of the Elements, supported on a carrier, which catalyst or catalyst precursor is an elongated shaped particle comprising three protrusions each extending from and attached to a central position, wherein the central position is aligned along the longitudinal axis of the particle, the cross-section of the particle occupying the space encompassed by the outer edges of six circles around a central circle, each of the six circles touching two neighbouring circles whilst three alternating circles are equidistant to the central circle and may be attached to the central circle, minus the space occupied by the three remaining outer circles and including the six interstitial regions.
• the catalyst particles according to the present invention have a larger surface- to-volume ratio than corresponding conventional "trilobal" particles of similar size and suffer substantially less from pressure drop than such corresponding conventional "trilobal” particles, due to higher voidage.
• a good C5+ selectivity and a good stability is obtained.
• An additional advantage is that the selectivity for linear (unbranched) products is increased.
• the particle ' s are sufficiently strong and can easily be made by extrusion.
• the shaped catalyst particles can be formed of any suitable material provided it is capable of being processed in such a way that their intended shape is obtained. Methods of preparing such shapes include pressing, extruding or otherwise forcing a granular or powdered catalyst or catalyst precursor material into various shapes under certain conditions, which will ensure that the particle retains the resulting shape, both during reaction as well as during regeneration.
• the catalysts of the present invention comprise, as the catalytically active component, a metal from Group VIII of the Periodic Table of the Elements.
• a metal from Group VIII of the Periodic Table of the Elements particularly catalytically active metals include ruthenium, iron, cobalt and nickel, more preferably cobalt. Combinations of two or more components are also possible.
• a Fischer-Tropsch catalyst is used, which yields substantial quantities of paraffins, more preferably substantially unbranched paraffins.
• a most suitable catalyst composition for this purpose includes a cobalt- containing Fischer-Tropsch catalyst.
• Such catalysts are described in the literature, see e.g. AU 698392 and WO 99/34917.
• Preferred hydrocarbonaceous feeds for the preparation of synthesis gas are natural gas or associated gas. As these feedstocks usually result in synthesis gas having H2/CO ratio's of close to 2, cobalt is a very good Fischer-Tropsch catalyst as the user ratio for this type of catalysts is also about 2.
• the catalytically active metal is preferably supported on a porous carrier.
• the porous carrier may be selected from any of the suitable refractory metal oxides or silicates or combinations thereof known in the art.
• Particular examples of preferred porous carriers include silica, alumina, titania, zirconia, ceria, gallia and mixtures thereof, especially silica, alumina and titania, especially Ti ⁇ 2-
• the amount of catalytically active metal on the carrier for optimum performance is preferably in the range of from 3 to 300 pbw per 100 pbw of carrier material, more preferably from 10 to 80 pbw, especially from 20 to 60 pbw.
• the catalyst may also comprise one or more metals or metal oxides as promoters.
• Suitable metal oxide promoters may be selected from Groups IIA, IIIB, IVB, VB, VIB or Group VIIB of the Periodic Table of the Elements, or the actinides and lanthanides.
• oxides of magnesium, calcium, strontium, barium, scandium, yttrium, lanthanum, titanium, zirconium, hafnium, cerium, thorium, uranium, vanadium, chromium and manganese are very suitable promoters.
• Particularly preferred metal oxide promoters for the catalyst used to prepare heavy paraffins are manganese, vanadium and zirconium oxide.
• Suitable metal promoters may be selected from Groups VIIB or VIII of the Periodic Table of the Elements. Rhenium, silver and Group VIII noble metals are particularly suitable, with platinum and palladium being especially preferred.
• the amount of promoter present in the catalyst is suitably in the range of from 0.01 to 100 pbw, preferably 0.1 to 40, more preferably 1 to 20 pbw, per 100 pbw of carrier.
• the most preferred promoters are selected from vanadium, manganese, rhenium, zirconium and platinum in view of their ability to produce long chain n-paraffins.
• the catalytically active metal and the promoter may be deposited on the carrier material by any suitable treatment, such as impregnation, mixing/kneading and mixing/extrusion.
• the loaded carrier is typically subjected to calcination.
• the effect of the calcination treatment is to remove crystal water, to decompose organic compounds and to convert inorganic compounds to their respective oxides.
• the resulting catalyst may be activated by contacting the catalyst with hydrogen or a hydrogen- containing gas, typically at temperatures of about 200 to 350 °C.
• Fischer-Tropsch catalysts comprise kneading/mulling, followed by extrusion, drying/calcination and activation.
• the suitable material for the shaped catalyst particles should be processed in such a way that their intended shape is obtained.
• a processing method is an extrusion process, wherein a shapeable dough, preferably comprising one or more sources for one or more of the catalytically active elements, and optionally one or more sources for one or more of the promoters and the finely divided refractory oxide or refractory oxide precursor is mulled together with a suitable solvent. The mulled mixture is then extruded through an orifice in a die-plate. The resulting extrudates are dried. If necessary, (additional) catalytic element sources and/or promoters may be applied to the extrudates by impregnation.
• the solvent for inclusion in the mixture may be any of the suitable solvents known in the art.
• suitable solvents include water; alcohols, such as methanol, ethanol and propanol; ketones, such as acetone; aldehydes, such as propanal; and aromatic solvents, such as toluene.
• a most convenient and preferred solvent is water, optionally in combination with methanol.
• die-plates enable the formation of the intended shape of the catalyst particles.
• Die- plates are well known in the art and can be made from metal or polymer material, especially a thermoplastic material .
• Preferred catalyst particles according to the present invention have a cross-section in which the three alternating circles (forming part of the outer circles) have diameters in the range between 0.74 and 1.3 times the diameter of the central circle, preferably between 0.87 and 1.15 times the diameter of the central circle. More preferred catalyst particles according to the present invention are those having a cross-section in which the three alternating circles have the same diameter as the central circle.
• the distance between the three alternating circles and the central circle is the same. This distance is preferably less than half the diameter of the central circle, more preferably less than a quarter of the diameter of the central circle, with most preference given to particles having a cross-section in which the three alternating circles are attached to the central circle.
• the three alternating circles do not overlap with the central circle. In case of any overlap, the overlap of each alternating circle and the central circle will be less than 5% of the area of the central circle, preferably less than 2%, more preferably less than 1%.
• the term “equidistant” as used herein refers to the circumstance that the distance between the centre of the central circle to the centre of one of the outer circles is equal to the distance between the centre of the central circle to the centre of either one of the other remaining outer circles.
• the term “equidistant” may comprise deviations up to 20% of the distance, preferably up to 10%, more preferably up to 5%. In the most preferred embodiment there is no deviation.
• the circumference of the preferred shaped particles according to the present invention is such that it does not contain sharp corners, which can also be expressed as the derivative of the cross-section being continuous.
• the diameter of the particles is defined as the distance between the tangent line that touches two protrusions and a line parallel to this tangent line that touches the third protrusion. It is indicated as d nom in Figure 1. In the case that the three alternating circles have one or two different diameters, d nom is the sum of the three measured diameters divided by three.
• the three protrusions and the central position together form the cross-section of the catalyst or catalyst precursor.
• the main part of each protrusion is formed by one of the (remaining) alternating circles.
• the main part of the central protrusion is formed by the central circle.
• the interstitial areas are divided between the central position and the protrusion by a line perpendicular to the line connecting the centre point of the central circle and the centre part of the alternating circle.
• the perpendicular line crosses the connecting line (solid line) at a point exactly in the middle between the two centre points (see figure 2).
• between 10% and 100% of the number of particles produced preferably have a nominal diameter with a deviation of less than 5% of the shape as defined in the present invention.
• at least 50% of the catalyst particles have a nominal diameter with a deviation of less than 5% of the shape as defined in the present invention.
• catalyst particles according to the present invention which also contain one or more holes along the length of the particles.
• the particles can contain one or more holes in the area formed by the central cylinder (the central circle in the cross-section given in Figure 1) and/or one or more holes in one or more of the alternating cylinders (the alternating circles in the cross-section given in Figure 1) .
• the presence of one or a number of holes causes an increase of the surface to volume ratio which in principle allows exposure of more catalytic sites and, in any case, more exposure to incoming charges which may work advantageously from a catalytic point of view. Since it becomes increasingly difficult to produce hollow particles as their size becomes smaller it is preferred to use porous particles without holes when smaller sizes are desired for certain purposes.
• the voidage of the catalyst particles according to the present invention is well above 50% (voidage being defined as the volume fraction of the open space present in a bed of particles outside the particles present, i.e. the volume of the pores inside the particles are not included in the voidage) .
• the particles used in the experiment to be described hereinafter had a voidage of typically 58% which is substantially above that of the comparative "trilobal" particle, the voidage of which amounted to just over 43%.
• the voidage of a bed of catalyst particles according to the invention is suitably between 45 and 80%, preferably between 50 and 70%, more preferably between 55 and 65%.
• the catalyst particles according to the present invention can be described as having a length/diameter ratio (L/D) of at least 1.
• the particles according to the present invention can have a L/D in the range between 1 and 25.
• the particles according to the present invention have a L/D in the range between 1.5 and 20, more preferably in the range between 2 and 10.
• the particles used in the experiment to be described hereinafter had a L/D of about 2.5.
• the length of the particles in accordance with the present invention is suitably in the range between 1 and 25 mm, preferably in the range between 2 and 20 mm, depending on the type of application envisaged.
• the catalytic conversion process may be performed under conventional synthesis conditions known in the art. Typically, the catalytic conversion may be effected at a temperature in the range of from 150 to 300 °C, preferably from 180 to 260 °C. Typical total pressures for the catalytic conversion process are in the range of from 1 to 200 bar absolute, more preferably from 10 to 70 bar absolute. In the catalytic conversion process especially more than 75 wt% of C5+, preferably more than
• the amount of products comprising one or more tertiary substituted carbon atoms is at least 20% less compared to a conversion process with similar reaction conditions, where a conventional trilobal catalyst is used.
• the amount of heavy wax (C20+) ma Y De U P to 60 wt%, sometimes up to 70 wt%, and sometimes even up till 85 wt%.
• a cobalt catalyst is used, a low H2/CO ratio is used (especially 1.7, or even lower) and a low temperature is used (190-230 °C) .
• the Fischer-Tropsch hydrocarbons stream comprises at least 35 wt% C30+, preferably 40 wt%, more preferably 50 wt%.
• the Fischer-Tropsch process may be a slurry FT process, especially an ebulated bed process or a fixed bed FT process, especially a multitubular fixed bed process. It has been found that the beds containing particles according to the invention have - in a random packing - a much higher voidage than beds containing the corresponding conventional trilobes when packed using the well known "sock loading" technique.
• the voidage obtained when using the conventional trilobal shape amounts up to about 45% whereas use of the particles according to the present invention produces a voidage of at least 55% which makes such particles attractive for low pressure drop applications, for instance the Fischer-Tropsch synthesis process.
• the catalyst particles described herein can also be formed as helical lobed particles.
• helical lobed particles refers to an elongated shaped particle comprising three protrusions each extending from and attached to a central position, the central position being aligned along a longitudinal axis, the particle having a cross-section occupying the space encompassed by the outer edges of six circles around a central circle, each of the six circles bordering two neighbouring circles whilst three alternating circles are equidistant to the central circle and may be attached to the central circle, minus the space occupied by the three remaining outer circles and including the six interstitial regions, which protrusions extend along and are helically wound about the longitudinal axis of the particle.
• helical lobed particles By employing helical lobed particles, a larger diameter helical lobed catalyst particle can be employed to achieve a given selectivity than is necessary when employing straight lobed particles, resulting in a greater reduction in pressure drop across the catalyst bed than expected from the prior art.
• helical lobed particles for a given design of fixed bed with a predetermined pressure drop, by employing the helical lobed particles in the Fischer-Tropsch process a substantially higher selectivity can be achieved than with the appropriate straight lobed particles necessary to meet the pressure drop requirements.
• Trilobe-shaped catalyst particles were prepared as follows. A mixture was prepared containing 143 g commercially available titania powder (P25 ex. Degussa) , 66 g commercially available Co (OH) 2 powder, 10.3 g n(Ac)2-4H2 ⁇ and 38 g water. The mixture was kneaded for
• the mixture was shaped using a Bonnot extruder.
• the resulting extrudates were dried and calcined.
• the resulting extrudates contained 20 wt% Co and 1 wt% Mn.
• the resulting catalyst particles had a trilobal shape having a nominal diameter of 1.7 mm (Catalyst A) .
• a mixture was prepared containing 143 g commercially available titania powder (P25 ex. Degussa), 66 g commercially available Co (OH) 2 powder, 10.3 g n(Ac)2-4H2 ⁇ and 38 g water. The mixture was kneaded for
• the mixture was shaped using a Bonnot extruder equipped with an appropriate dieplate to obtain the desired shape as desired in claim 1.
• the resulting extrudates were dried and calcined.
• the resulting catalyst particles contained 20 wt% Co and 1 wt% Mn and had shapes as defined in claim 1 with nominal diameters of 1.7 mm (Catalyst B) , 1.5 mm (Catalyst C) , 1.3 mm (Catalyst D) and 1.0 mm (Catalyst E) respectively.
• Example III Example III
• Catalysts A and B were tested in a process for the preparation of hydrocarbons.
• the catalysts were reduced in-situ for 24 hours with a mixture of nitrogen and hydrogen gas. During reduction the relative amount of hydrogen in the mixture was gradually increased from 0% to 100%.
• the water concentration in the off-gas was kept below 3000 ppmv.
• catalyst B gives a better performance than catalyst A with respect to C5+ selectivity in the Fischer-Tropsch process.
• the performance of catalyst B is better even though the amount of active material per volume reactor is smaller for catalyst B than for catalyst A, due to the higher voidage.
• the specific shape of the catalyst B particles enables a better use of the expensive catalyst material .
• Catalysts A, C, D and E were tested in a process for the preparation of hydrocarbons.
• the catalysts were reduced in-situ for 24 hours with a mixture of nitrogen and hydrogen gas. During reduction the relative amount of hydrogen in the mixture was gradually increased from 0% to 100%.
• the water concentration in the off-gas was kept below 3000 ppmv. Following reduction the pressure was increased to
• the reaction was carried out with a mixture of hydrogen and carbon monoxide.
• the reaction temperature is expressed as the weighted average bed temperature (WABT) in °C.
• the results are set out in Table II.
• catalysts C, D and E give a better performance than catalyst A in the Fischer-Tropsch process.
• the performance of catalysts C, D and E is better even though the amount of active material per volume reactor is smaller for catalysts C, D and E than for catalyst A, due to the higher voidage.
• the specific shape of catalyst C, D and E particles enables a better use of the expensive catalyst material.

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