Classifications

• • 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
  • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
• • 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
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
  • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
• • 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
  • C10G2/34—Apparatus, reactors
  • C10G2/341—Apparatus, reactors with stationary catalyst bed
• • 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
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00628—Controlling the composition of the reactive mixture
  • B01J2208/00637—Means for stopping or slowing down the reaction
• • 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
  • B01J23/847—Vanadium, niobium or tantalum or polonium
  • B01J23/8472—Vanadium
• • 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

Definitions

• the present invention relates to a Fischer-Tropsch process, in particular to a process for carrying out a high-speed stop in a Fischer-Tropsch process carried out in a fixed bed reactor.
• the Fischer-Tropsch process can be used for the conversion of hydrocarbonaceous feed stocks into normally liquid and/or solid hydrocarbons (0 0 C, 1 bar) .
• the feed stock e.g. natural gas, associated gas, coal-bed methane, residual oil fractions, biomass and/or coal
• This mixture is often referred to as synthesis gas or syngas.
• the synthesis gas is fed into a reactor where it is converted over a suitable catalyst at elevated temperature and pressure into paraffinic compounds ranging from methane to high molecular weight modules comprising up to 200 carbon atoms, or, under particular circumstances, even more.
• Fischer-Tropsch reactor systems include fixed bed reactors, especially multi-tubular fixed bed reactors, fluidised bed reactors, such as entrained fluidised bed reactors and fixed fluidised bed reactors, and slurry bed reactors such as three-phase slurry bubble columns and ebullated bed reactors.
• the Fischer-Tropsch reaction is very exothermic and temperature sensitive. In consequence, careful temperature control is required to maintain optimum operation conditions and desired hydrocarbon product selectivity. The fact that the reaction is very exothermic also has the consequence that when temperature control is not adequate, the reactor temperature can increase very quickly, which carries the risk of a reactor runaway, which may result in local deactivation of the catalyst.
• a reactor runaway is a most undesirable phenomenon, as it may result in catalyst deactivation which necessitates untimely replacement of the catalyst, causing reactor downtime and additional catalyst cost. Therefore, there is need for a process for carrying out a high-speed stop in a Fischer-Tropsch reactor.
• a high-speed stop may, for example, be required when the temperature in the Fischer-Tropsch reactor increases to an unacceptable value either locally or over the entire reactor, when there is an interruption in the gas flow, or in the case of other unforeseen circumstances.
• the present invention pertains to a process for carrying out a high-speed stop in a Fischer- Tropsch process which comprises providing a feed to a fixed bed reactor comprising a Fischer-Tropsch catalyst, the reactor being at reaction temperature and pressure, and withdrawing an effluent from the reactor, characterised in that the high-speed stop is effected by blocking provision of feed to the reactor and simultaneously blocking the withdrawal of effluent from the reactor.
• the feed provided to the fixed bed reactor comprises CO and H2.
• the effluent can be a single gaseous phase, a multi-phase effluent or two or more effluent streams with one or more being mainly gaseous and one or more being mainly liquid phase. In this invention, all effluent streams are stopped.
• the word effluent when used in the context of blocking the effluent, encompasses all effluent streams.
• the word feed when used in the context of blocking the feed, encompasses all feed streams.
• the feed can be a single gaseous feed stream or two or more gas feed streams, or a multi-phase feed or two or more feed streams with one or more being mainly gaseous and one or more being mainly liquid phase.
• the feed stream provided to the reactor, or the combination of feed streams provided to the reactor comprises at least CO and H2.
• all feed streams are stopped, and no new feed streams are fed to the reactor.
• no feed is provided to the reactor any more, not even a feed stream that does not comprise CO or H2.
• the invention thus concerns a process for carrying out a high-speed stop in a Fischer-Tropsch process which comprises providing a feed to a fixed bed reactor comprising a Fischer-Tropsch catalyst, the reactor being at reaction temperature and pressure, and withdrawing an effluent from the reactor, whereby the feed comprises CO and H2, characterised in that the high-speed stop is effected by blocking provision of any feed stream to the reactor and simultaneously blocking the withdrawal of any effluent stream from the reactor.
• the reactor When the reactor has been blocked, the reactor is cooled.
• the end temperature of the cooling step depends on the desired further action. In general, the reactor will be cooled to a temperature between ambient and 200 0 C. Where the reactor is cooled with a view to immediate restarting of the reactor, it will generally be cooled to a temperature in the range of 100-190 0 C, in particular to a value of 160-180 0 C.
• the cooling speed will depend on the size of the reactor and further circumstances. For example, it may be in the range of 10-100 0 C per hour.
• the reactor may also be depressurised, before, during, or after cooling. If so desired, the reactor may be depressurised to a value of, say, below 15 bar, more specifically in the range of 1- 10 bar, for example in the range of 2-8 bar.
• the performance of a high-speed stop in a Fischer-Tropsch reactor is often accompanied by a raise in temperature, culminating in a process-side temperature peak. This is caused by a decrease in gas hourly space velocity which leads to an increased conversion, accompanied by increased heat formation, and simultaneously to a decrease in heat removal capacity.
• a high-speed stop according to the invention results in an increase in peak temperature which is substantially lower than the increase in peak temperature which is obtained when a high-speed stop is carried out by blocking the flow of feed to the reactor and depressurising the reactor via the bottom. It was also found that the procedure according to the invention does not result in substantial catalyst deactivation.
• the process according to the invention is suitable for fixed bed reactors.
• the reactor is a reactor tube, which has a ratio between length and diameter of at least 5, in particular at least 50. As an upper limit a ratio of at most 1000 may be mentioned .
• the reactor tube is a tube in a multitubular reactor, which comprises a plurality of reactor tubes at least partially surrounded by a heat transfer medium.
• the tubes in a multitubular reactor generally have a diameter in the range of 0.5-20 cm, more in particular in the range of 1 to 15 cm. They generally have a length in the range of 3 to 30 m.
• the number of tubes in a multitubular reactor is not critical to the present invention and may vary in wide ranges, for example in the range of 4 to 50 000, more in particular in the range of 100 to 40 000.
• Multitubular reactors and their use in Fischer- Tropsch processes are known in the art and require no further elucidation here.
• the catalyst is a particulate catalyst, that is, a catalyst in the form of particles.
• the shape of the catalyst may be regular or irregular.
• the dimensions are suitably 0.1-30 mm in all three directions, preferably 0.1-20 mm in all three directions, more in particular 0.1-6 mm.
• Suitable shapes are spheres and, in particular, extrudates.
• the extrudates suitably have a length between 0.5 and 30 mm, preferably between 1 and 6 mm.
• the extrudates may be cylindrical, polylobal, or have any other shape.
• Their effective diameter that is, the diameter of a sphere with the same outer surface over inner volume ratio, is suitably in the range of 0.1 to 10 mm, more in particular in the range of 0.2-6 mm.
• the process according to the invention is of particular interest for reactors comprising a catalyst with decreased diffusion limitation, in particular with an effective diameter of at most 2 mm, more in particular of at most 1.6 mm, still more in particular of at most 1.5 mm.
• Catalysts with a decreased diffusion limitation are for example described in WO2003/013725, WO2008/087149, WO2003/103833 , and WO2004/041430.
• the Fischer-Tropsch reaction is preferably carried out at a temperature in the range from 125 to 400 0 C, more preferably 175 to 300 0 C, most preferably 200 to
• the pressure preferably ranges from 5 to 150 bar, more preferably from 20 to 80 bar.
• the gaseous hourly space velocity may vary within wide ranges and is typically in the range from 500 to 10000 Nl/l/h, preferably in the range from 1500 to 4000 Nl/l/h.
• the hydrogen to CO ratio of the feed as it is fed to the catalyst bed generally is in the range of 0.5:1 to 2:1.
• Products of the Fischer-Tropsch synthesis may range from methane to heavy hydrocarbons.
• the production of methane is minimised and a substantial portion of the hydrocarbons produced have a carbon chain length of a least 5 carbon atoms.
• the amount of C5+ hydrocarbons is at least 60% by weight of the total product, more preferably, at least 70% by weight, even more preferably, at least 80% by weight, most preferably at least 85% by weight.
• the CO conversion of the overall process is preferably at least 50%.
• the products obtained via the process according to the invention can be processed through hydrocarbon conversion and separation processes known in the art to obtain specific hydrocarbon fractions. Suitable processes are for instance hydrocracking, hydroisomerisation, hydrogenation and catalytic dewaxing. Specific hydrocarbon fractions are for instance LPG, naphtha, detergent feedstock, solvents, drilling fluids, kerosene, gasoil, base oil and waxes.
• Fisher-Tropsch catalysts are known in the art. They typically comprise a Group VIII metal component, preferably cobalt, iron and/or ruthenium, more preferably cobalt. Typically, the catalysts comprise a catalyst carrier.
• the catalyst carrier is preferably porous, such as a porous inorganic refractory oxide, more preferably alumina, silica, titania, zirconia or combinations thereof. References to the Periodic Table and groups thereof used herein refer to the previous IUPAC version of the Periodic Table of Elements such as that described in the 68th Edition of the Handbook of Chemistry and Physics (CPC Press) .
• the optimum amount of catalytically active metal present on the carrier depends inter alia on the specific catalytically active metal.
• the amount of cobalt present in the catalyst may range from 1 to 100 parts by weight per 100 parts by weight of carrier material, preferably from 10 to 50 parts by weight per 100 parts by weight of carrier material.
• the catalytically active metal may be present in the catalyst together with one or more metal promoters or co- catalysts.
• the promoters may be present as metals or as the metal oxide, depending upon the particular promoter concerned. Suitable promoters include oxides of metals from Groups IA, IB, IVB, VB, VIB and/or VIIB of the Periodic Table, oxides of the lanthanides and/or the actinides.
• the catalyst comprises at least one of an element in Group IVB, VB and/or VIIB of the Periodic Table, in particular titanium, zirconium, manganese and/or vanadium.
• the catalyst may comprise a metal promoter selected from Groups VIIB and/or VIII of the Periodic Table.
• Preferred metal promoters include rhenium, platinum and palladium.
• a most suitable catalyst comprises cobalt as the catalytically active metal and zirconium as a promoter.
• Another most suitable catalyst comprises cobalt as the catalytically active metal and manganese and/or vanadium as a promoter.
• the promoter if present in the catalyst, is typically present in an amount of from 0.1 to 60 parts by weight per 100 parts by weight of carrier material. It will however be appreciated that the optimum amount of promoter may vary for the respective elements which act as promoter. If the catalyst comprises cobalt as the catalytically active metal and manganese and/or vanadium as promoter, the cobalt : (manganese + vanadium) atomic ratio is advantageously at least 12:1.
• Example 1 Comparative example
• a Fischer-Tropsch process was operated at a temperature of about 210 0 C and a pressure of about 40 bar in a fixed-bed reactor containing a catalyst.
• a high-speed stop was carried out by blocking the flow of feed to the reactor, while maintaining a nitrogen feed at an LHSV of 50 Nl/l/h.
• the reactor was depressurised via the bottom to a pressure of 20 barg in 6 minutes, and then to a pressure of 6 barg in an additional 14 minutes.
• the reactor temperature was measured during the high-speed stop, and a peak temperature of +100 0 C above the maximum reaction temperature prior to the high-speed stop was measured.
• Example 2 Comparative example A Fischer-Tropsch process was operated at a temperature of about 222 ° C and a pressure of about 60 bar in a fixed-bed reactor containing a catalyst.
• a high-speed stop was carried out by blocking the flow of feed to the reactor.
• the reactor was depressurised via the bottom to a pressure of 20 barg in 6 minutes, and then to a pressure of 6 barg in an additional 14 minutes.
• the reactor temperature was measured during the high-speed stop, and a peak temperature of more than 300 0 C above the maximum reaction temperature prior to the high-speed stop was measured. Higher temperatures did occur during this runaway, but could not be measured.
• Example 3 Example according to the invention
• a Fischer-Tropsch process was operated at a temperature of about 210 0 C and a pressure of about 40 bar in a fixed-bed reactor containing a catalyst.
• a high-speed stop was carried out by blocking the flow of feed to the reactor and the flow of effluent from the reactor.
• the reactor was cooled at 20 °C/h to 160 0 C. It was then depressurised via the bottom to a pressure of 20 barg in 6 minutes, and then to a pressure of 6 barg in an additional 14 minutes.
• the reactor temperature was measured during the high-speed stop, and a peak temperature of + 23 0 C above the maximum reaction temperature prior to the high-speed stop was measured.
• Example 4 Example according to the invention
• a Fischer-Tropsch process was operated at a temperature of about 222 0 C and a pressure of about 60 bar in a fixed-bed reactor containing a catalyst.
• a high-speed stop was carried out by blocking the flow of feed to the reactor and the flow of effluent from the reactor.
• the reactor was cooled at 20 °C/h to 160 0 C. It was then depressurised via the bottom to a pressure of 20 barg in 6 minutes, and then to a pressure of 6 barg in an additional 14 minutes.
• the reactor temperature was measured during the high-speed stop, and a peak temperature of +25 0 C above the maximum reaction temperature prior to the high-speed stop was measured.
• Example l 210 0 C 40 bar N2 feed; +100 0 C comp depressurised via the bottom
• Example 2 222 0 C 60 bar blocked feed; >300°C above comp depressurised via the bottom
• Example 3 210 0 C 40 bar blocked feed; +23 0 C invention blocked effluent

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• 2009
  • 2009-12-14 BR BRPI0923094-7A patent/BRPI0923094B1/pt active IP Right Grant
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