WO2018149881A1 - Procédé à basse température selon fischer-tropsch - Google Patents

Procédé à basse température selon fischer-tropsch Download PDF

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Publication number
WO2018149881A1
WO2018149881A1 PCT/EP2018/053689 EP2018053689W WO2018149881A1 WO 2018149881 A1 WO2018149881 A1 WO 2018149881A1 EP 2018053689 W EP2018053689 W EP 2018053689W WO 2018149881 A1 WO2018149881 A1 WO 2018149881A1
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Prior art keywords
synthesis gas
bank
reaction
reactor
catalyst
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PCT/EP2018/053689
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German (de)
English (en)
Inventor
Brendon Patrick Hausberger
Simon Thornhill Holland
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Advanced Liquid Fuel UG (haftungsbeschränkt)
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Publication of WO2018149881A1 publication Critical patent/WO2018149881A1/fr

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    • 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
    • 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

Definitions

  • the invention relates to a process for the production of hydrocarbons from synthesis gas by means of low-temperature Fischer Tropsch method, wherein synthesis gas is reacted in a reactor cascade banking system with a minimum of three banks and an apparatus for carrying out such methods, comprising a reactor bank system having at least three Banks wherein each bank is equipped with multi-tube fixed catalyst reactors, heat exchangers and multi-stage separation units to separate the reaction products.
  • the heterogeneous Fischer-Tropsch process has been classified into a high-temperature Fischer-Tropsch (HTFT) process or a low-temperature Fischer-Tropsch (LTFT) process.
  • HTFT high-temperature Fischer-Tropsch
  • LTFT low-temperature Fischer-Tropsch
  • the HTFT process can be described as a two-phase Fischer-Tropsch process. It is usually carried out at a temperature of 250 ° C to 400 ° C and the catalyst used is usually an iron-based catalyst. In general, the process is carried out commercially in a fluidized bed reactor.
  • the LTFT process can be described as a three-phase Fischer-Tropsch process. It is usually carried out at a temperature of 180 ° C to 250 ° C and the catalyst used is usually either a cobalt-based or an iron-based catalyst. Under the process conditions, hydrocarbonaceous products result in the form of liquids and gases. Thus, this process can be described as a three-phase process wherein the reactants are in the gas phase, at least some of the products are in the liquid phase and the catalyst is in a solid phase in the reaction zones of the catalytic fixed beds of the reactor tubes. In general, this process is carried out commercially in fixed bed reactors.
  • Multi-tube fixed bed reactors which have been in use for several years, are operated by Sasol in their ARGE process and by Shell in the Shell Middle Distillate Synthesis (SMDS) single reactor recycle gas process or in combination with slurry reactors.
  • Sasol uses the multi-tube fixed bed reactors in simple application only in conjunction with the Synthol operation. Comparing fixed bed to Synthol process results shows that the conversion to hydrocarbons is higher in the Synthol unit and the CO: H 2 ratio is also higher. Since the ARGE fixed-bed reactor favors the formation of straight-chain paraffins, a higher production of diesel and wax fractions can be achieved than with the Synthol operating unit become.
  • the ARGE fixed bed reactor products have a lower gasoline octane number but a higher diesel cetane number relative to the synthol process.
  • the SMDS procedure consists of three stages:
  • the synthesis gas is converted into long-chain paraffins.
  • the reaction mechanism follows the known Schultz-Flory polymerization kinetics, which are characterized by the likelihood of chain growth (a). Chain termination (L-a) are marked. There is always a regular molecular weight distribution in the whole product and a high alpha value, which corresponds to a high average molecular weight of the paraffinic product. Typically, the products present themselves as two alpha model distributions with a fraction around the carbon number 10.
  • the paraffinic hydrocarbons produced by the FT reaction are always very linear. This implies that the synthesis reaction can be considered as a stepwise addition of a methyl segment to the end of an existing chain. Since atoms of the alkyl chain at the opposite end are hardly able to influence this reaction, it is plausible that the relative probabilities of chain growth and chain termination are independent of the length of the alkyl chain.
  • the carbon number distribution of the FT product can therefore be described quite accurately, as a single parameter, by a simple statistical model (Anderson Flory-Schultz [AFS] distribution). This value appears to depend on the catalyst and the reaction conditions. In a few hundred formulations under different operating conditions it was confirmed that the carbon number distributions are in close agreement with the AFS chains of growth kinetics. The detected values vary between 0.70 and 0.95.
  • the FT method can either yield large amounts of gaseous hydrocarbons such as methane or products that have a very broad carbon number distribution.
  • gaseous hydrocarbons such as methane or products that have a very broad carbon number distribution.
  • methane can be produced with 100% selectivity.
  • the synthesis part of the SMDS process has been developed to produce strictly long-chain hydrocarbon wax.
  • the FT reactions are carried out commercially via an iron-based catalyst (for example from Sasol) or via a cobalt-based catalyst (SMDS) in a reactor which resembles a tubular heat exchanger packed with the catalyst in the tubes.
  • SMDS cobalt-based catalyst
  • WO 2002008163 A1 discloses a process for optimizing the Fischer-Tropsch synthesis of hydrocarbons in the distillate fuel and lubricating oil ranges, proposes a syngas conversion to higher molecular weight products, which the reaction of synthesis gas with a cobalt / ruthenium Fischer-Tropsch catalyst in the presence an olefin isomerization catalyst under suitable reaction conditions to form the desired reaction products.
  • US 2015/021 1766 A1 discloses a device for the synthesis of Fischer-Tropsch products containing 3 banks equipped with multitubereaktoren of equal number, with catalyst beds and at least one serially connected crackers per bank to existing (solid) paraffin wax in lower (liquid ) To split hydrocarbons.
  • the device used is adapted to a process tailored to the feed of a starting material of biomaterial. The process processes gas mixtures with (high) nitrogen contents of 50% and greater. Within the process, no water recycling takes place from the reaction mixture.
  • US 20040192989 A1 discloses a process for the production of hydrocarbons by means of a multi-tube reactor containing at least 100 tubes containing a catalyst, each tube being between 2 m and 5 m high and in thermal contact with a cooling fluid. Supplied to each tube is hydrogen and carbon monoxide at a linear gas surface velocity of less than about 60 cm / s; and a conversion of the gas feed stream to hydrocarbons on the catalyst, the yield in each tube being greater than 100 kg hydrocarbons / h / (m 3 reaction zone). Each tube can have an inner diameter of more than 2 cm.
  • the catalyst is active for Fischer-Tropsch synthesis and contains cobalt or iron.
  • the maximum difference in radial mean temperature between two points along the reactor in the axial direction is less than 15 ° C, preferably less than 10 ° C.
  • the catalyst loading or intrinsic activity along the length of the reactor may vary. Reaction water or hydrocarbon deposition during a linear reactor arrangement is not installed. Usually, the process heat is dissipated through the tube walls of the tubes of such reactors via boiling water under pressure. Due to the interaction between the generation of process heat and heat dissipation through the tube walls, axial and radial temperature profiles are created. The maximum conversion rates are generated in regions of axial temperature peaks. This means that most of the conversion is achieved in the first three to four meters of 10 m to 12 m long catalytic fixed beds.
  • the invention has for its object to provide methods and apparatus in which a maximum conversion of hydrocarbons is achieved at a controllable high selectivity.
  • the sales should be evenly distributed over the pipe lengths in the reactor, the maximum system availability and the production costs are minimal.
  • This object is achieved by providing a Fischer-Tropsch process, wherein in a, at least partially, linear multi-tube fixed bed reactor arrangement comprising catalysts comprising iron and, optionally, cobalt, synthesis gas (syngas) with hydrogen and carbon monoxide in a non-recycling Passage conversion is reacted.
  • synthesis gas syngas
  • linear is to be understood as meaning that the reactor cascades are arranged in series and connected in a fluid-conducting manner. Rather, the condensable product components are separated on discharge from a cascade and the non-separated synthesis gas for further implementation in another cascade and not in the cascade back in which they a.
  • the production costs are reduced by up to 30%, since, inter alia, there is no cycle compaction, which also has the advantage that the individual cascades or banks in which the starting materials or intermediates are reacted are preferably set up independently of one another, ie in particular have different process parameters, such as temperature, pressure and cycle time.
  • the invention includes a process for the production of hydrocarbons from synthesis gas by means of low temperature processes, wherein the synthesis gas in a reactor bank system with a minimum of three banks (multi-tube fixed bed reactors) passed and at reaction temperatures between 180 to 350 ° C and a pressure between 1, 5 MPa operated to 5.0 MPa and is reacted in the presence of catalysts having a H 2 / CO ratio between 1, 9 and 2.3.
  • the process is operated in a single linear pass of the starting material, wherein usually three series-connected reactor cascades are used with simultaneous water separation and product removal.
  • the synthesis gas is first introduced into the bank 1, then subjected to the simultaneous deposition of the reaction water and the synthesized crude oil (Sythetic crude, Syncrudes reaction product) and unreacted synthesis gas is introduced into the bank 2 and again freed from the water and Syncrude (reaction product) and unreacted synthesis gas to the third and last bank, freed from water and Syncrude again and unreacted synthesis gas is treated in such a way that over 80% of the carbon (carbon conversion to CO base) are implemented.
  • Synesized crude oil Synthetic crude, Syncrudes reaction product
  • unreacted synthesis gas is introduced into the bank 2 and again freed from the water and Syncrude (reaction product) and unreacted synthesis gas to the third and last bank, freed from water and Syncrude again and unreacted synthesis gas is treated in such a way that over 80% of the carbon (carbon conversion to CO base) are implemented.
  • a process wherein the performance is in the form of a high-performance once-through low-temperature Fischer Tropsch Syncrude synthesis, ie a linear low-temperature Fischer-Tropsch process, d. H.
  • the heat removal from the reactor cascades takes place by generating steam in natural circulation, wherein the pressure is between 2.0 and 4.0 MPa and thereby highest yields are achieved.
  • a variant of the method is to realize the reaction at 20 to 40 bar with an H 2 / CO ratio between 1, 9 and 2.3 and with less than 30 percent by volume of inert gases.
  • a further variant provides that the gas stream between the reactor banks 1 and 2 and 2 and 3 is compressed with compressors and that in addition to minimizing the product inhibition by intermediate deposition of reaction water and synthesis gas, the process parameters temperature and catalyst properties for each reactor individually be set to achieve the required process overall selectivity and catalyst age-related changes in the production cycle, how the product quality can be compensated, adjusted or corrected.
  • reaction temperature by means of support of iron / cobalt catalysts between 180-350 ° C, preferably at 220 ° C to 240 ° C, and that the process at a pressure of 1, 5 MPa to 5, 0 MPa, preferably 2.0 MPa to 4.0 MPa.
  • reaction water and (intermediate) syncrude (reaction product) takes place from each reactor tank.
  • the simultaneous water and Syncrude deposition has the effect that the life of the catalysts used is significantly increased and this circumstance leads to a cost reduction.
  • Reaction water in high concentrations in the reaction gas leads significantly to a faster inactivation of the catalysts used.
  • the process according to the invention can advantageously be used for the processing of educts which contain a nitrogen content of up to 30%, in particular of 20% or less.
  • Another aspect of the invention relates to an apparatus for carrying out the process of the invention, in particular a low temperature Fischer Tropsch process for the conversion of synthesis gas to hydrocarbons, containing a reactor bank system with at least 3 banks, wherein each bank is at least equipped with multi-tube fixed catalyst bed Reactors, heat exchangers and multi-stage separation units for a separation of water of reaction, Syncrude and unreacted synthesis gas and a conduit system for reintroduction or recycling of synthesis gas in the upstream bank or unreacted synthesis gas the input synthesis gas or a thermal utilization (eg ) is supplied.
  • a reactor bank system with at least 3 banks, wherein each bank is at least equipped with multi-tube fixed catalyst bed Reactors, heat exchangers and multi-stage separation units for a separation of water of reaction, Syncrude and unreacted synthesis gas and a conduit system for reintroduction or recycling of synthesis gas in the upstream bank or unreacted synthesis gas the input synthesis gas or a thermal utilization (eg
  • the apparatus for carrying out the process according to the invention for the conversion of synthesis gas into hydrocarbons comprising a series-connected reactor cascade banking system with at least 3 banks, wherein each bank is at least equipped with multi-tube fixed catalyst bed reactors, heat exchangers and Mehrphasendekanter for a separation of water of reaction, Syncrude and unreacted synthesis gas and a Piping system for feeding or recycling synthesis gas into the upstream bank by means of compressors.
  • the heat removal from the reactors is preferably carried out by steam generation in natural circulation.
  • the apparatus comprises a reactor bank system having at least 3 banks.
  • Bank 1 is preferably equipped with 8-15 multi-tube fixed catalyst reactors, heat exchangers and multi-stage separation units
  • Bank 2 is equipped with 5-9 multi-tube fixed catalyst reactors, heat exchangers and multi-stage separation units and / or bench 3 equipped with 3 - 6 multi-tube fixed catalyst reactors, heat exchangers and multi-stage separation units, and a piping system for reintroduction or recycle of syngas into bank 1.
  • a device according to the invention contains multi-tube fixed catalyst reactors containing tubes.
  • the device according to the invention contains 3 banks, of which these multi-reactors are equipped with catalyst beds, with banks 2 and 3 having a reduced number of fixed-bed reactors with respect to the upstream bank.
  • the device according to the invention does not require any cracker (s) and is designed so that a simultaneous separation of reaction water and Syncrude takes place in the process.
  • the apparatus thus contains in particular a reactor bank system with a minimum of three banks, including bank 1 with multi-tube fixed bed reactors with tubes designed for optimum heat exchange (tubes) with catalyst beds, in particular consisting of preferably classic LTFT catalysts supplied with a purified Compressor-boosted syngas stream connected to Bank 2 with reduced number of individual fixed-bed reactors with tubes designed for optimal heat exchange with FT catalyst beds, through which unreacted process syngas from Bank 1 reactors separated by multiphase decanter for simultaneous deposition of one part the reaction water and the synthesized syncrude from the process gas stream and the passage of the unreacted separated process syngas of the reactors of Bank 2 on the following multi-phase decanter with the function of a second partial separation of residual syngas, reaction W asser and Syncrude and the forwarding of the residual syngas to the last reactors with further reduced number of bank 3 and subsequent final separation of water and syncrude via multiphase decanter, so that over 80% of the CO in the feed to bank 1 passes through the exit of bank 3 in
  • the present invention includes apparatus and methods of at least three reactor banks for ONCE THROUGH NT FISCHER TROPSCH (OT-NT-FT) PROCESS suitable for crude oil (Syncrude) production, wherein the achievement of high yields is aimed at various liquid fuels from optimized product selectivity distributions and it can be described as in the examples.
  • the heat removal from the reactors takes place by steam generation in natural circulation.
  • the reactor tubes, with an inner diameter of 40-60 mm, are filled with a catalyst bed.
  • the first bank (1) is equipped with multi-tube fixed bed reactors (6,7,8). Pure syngas (4) in a ratio of H 2 / CO of 1.9 to 2.3 is preferably applied in the upper part of the individual reaction tubes with optimized tube diameters and optimum heat exchanger properties in the individual reactors by compressors (5) with reaction pressure generation. At the reactor ends, the synthesized hydrocarbons (22, intermediate syncrude A) and the reaction water (23) produced are separated by decanters (10, 1, 12). Unreacted process gas (21) from Bank 1 is then passed, without additional pressure increase, to the number two reduced multi-tube fixed bed tubular reactors (13,14) of Bank two (2) and traverse the fixed catalyst beds.
  • the number of reactors or the total number of tubes of bank 2 is reduced depending on gas flow and pressure loss. Also from Bank 2, from the reactor ends, the synthesized hydrocarbons (22, intermediate-mycrude B)) and the generated reaction water (23) are separated by a multiphase decanter. The unreacted process gas (21) from the reactors of Bank 2 is now in turn passed without additional pressure increase on the multi-tube fixed bed reactors Bank 3. The number of reactors (18) or the total tube (tube) number of the bank three (3) is reduced depending on the gas flow and pressure losses. Reaction water (23) and intermediate syncrude C (22) are separated via a decanter. The unreacted small residual process gas volume (21) can be found in the primary syngas stream (4) are recycled or used for the operation of a gas turbine.
  • the procedure ONCE THROUGH is realized by the adjustment of each individual reactor geometry of the reactors of the reactor banks and on the individual process parameters pressure, temperature and tube characteristics of the individual reactors as well as the application of different conversion catalysts with specific selectivity. It offers superior flexibility over conventional methods. For continuous operation, reactors (9, 15, 19) are kept in standby to ensure catalyst replacement or maintenance on the reactors without plant downtime. Increased plant availability and cost savings result from this technical measure.
  • the first bank (1) is equipped with multi-tube fixed bed reactors (5,6,7). Pure syngas (4) is applied in a ratio of H 2 / CO of 1.9 to 2.3, preferably in the upper part of the individual reaction tubes with optimized tube diameters and optimum heat exchanger properties in the individual reactors by compressors (5) with reaction pressure generation. At the reactor ends, the synthesized hydrocarbons (22, intermediate syncrude A) and the reaction water (23) produced are separated by decanters (10, 1, 12). Unreacted process gas (21) from Bank 1 is then passed, without additional pressure increase, to the number two reduced multi-tube fixed bed tubular reactors (13,14) of Bank two (2) and traverse the fixed catalyst beds.
  • the number of reactors or the total number of tubes of bank 2 is reduced depending on gas flow and pressure loss. Also from Bank 2, from the reactor ends, the synthesized hydrocarbons (22, intermediate-mycrude B)) and the generated reaction water (23) are separated by a multiphase decanter. The unreacted process gas (21) from the reactors of Bank 2 is now in turn passed without additional pressure increase on the multi-tube fixed bed reactors Bank 3. The number of reactors (18) or the total tube (tube) number of the bank three (3) is reduced depending on the gas flow and pressure losses. Reaction water (23) and intermediate syncrude C (22) are separated via a decanter. The unreacted low residual process gas volume (21) can be recycled to the primary syngas stream (4) or used for operation of a gas turbine.
  • the ONCE THROUGH process is governed by the setting of each individual reactor geometry of the reactors of the reactor banks and on the individual Process parameters pressure, temperature and tube characteristics of the individual reactors and the application of different conversion catalysts realized with specific selectivity. It offers superior flexibility over conventional methods. For continuous operation, reactors (9, 15, 19) are kept in standby to ensure catalyst replacement or maintenance on the reactors without plant downtime.
  • the OT-NT-FT system requires a synthesis gas pressure between 20 and 40 bar with a H 2 / CO ratio between 1, 9 and 2.3 and with less than 30 percent by volume of inert gases.
  • the OT-NT-FT system requires an unchanged synthesis gas pressure of between 20 and 40 bar compared to the 10,000 bpd OT-NT-FT system with a H 2 / CO ratio of between 1, 9 and 2 , 3 and with less than 30% by volume of inert gases.
  • the FT technology according to the invention is distinguished by a particularly high selectivity of the formation of middle distillates.
  • product proportions of the diesel / kerosene fraction in the FT crude product of 70% by mass and higher can be achieved.
  • the composition of the FT fuels produced (high aromatics content) is intrinsically close to the requirements of kerosene quality.
  • the kerosene produced by the FT technology of the present invention can be used as a drop-in-type synthetic aviation fuel without the elaborate post-treatment required in the application of the commercially available FT processes.
  • a special feature of the FT technology according to the invention is the innovative "once through" reactor concept. This concept dispenses with the recirculation of the unreacted synthesis gas, resulting in considerable cost savings (no recycle gas compression) and an intensification of the FT synthesis (no separation into product gas stream and recycle gas stream) achieved.
  • the FT process according to the invention is significantly better suited than the competitive Fischer-Tropsch processes for the production of tailor-made, specification-compliant aviation fuels.
  • a reduction of the production cost of synthetic kerosene by about 1/3 compared to the established methods of FT synthesis is possible.
  • the FT technology according to the invention is scalable over a wide range of system capacity. Therefore, this new process can be used both for large-scale refinery (plant capacity 105-106 t / a) and for decentralized use in smaller plants (plant capacity 102-103 t / year).
  • the FT process according to the invention represents a new, more efficient variant of the low-temperature FT synthesis. The synthesis is carried out at temperatures in the range from 220 to 240 ° C. and pressures of from 25 to 40 bar.
  • the heat removal from the tube bundle reactors is preferably carried out by steam generation in natural circulation.
  • the reactor tubes with an inner tube diameter of 40-50 cm, are filled with a catalyst bed, the catalyst used being crucial for the quality and yield of the FT product produced.
  • the condensable components (see Syncrude) are separated from the product mixture and the unreacted synthesis gas is fed to the next reactor stage.
  • the inventive technology differs significantly from the competing FT methods.
  • the "once through" reactor design eliminates the need for recirculating cycle gas, resulting in significant cost advantages (no recycle gas compressors and no
  • an advanced, specially adapted Fe-based catalyst is used. It is characterized by high degrees of conversion of the synthesis gas, with a particularly high selectivity of the formation of middle distillates. For the entire reactor cascade, sales of up to 80%, based on the supplied carbon, are achieved. With appropriate adjustment of the process conditions, a product content of glare-free kerosene of 70 wt .-% and higher can be achieved. In particular, the high kerosene yield represents a unique feature of the FT method according to the invention, usually the proportion of Kerosinfr forcing in the product spectrum of low-temperature FT synthesis is well below 50 wt .-%.
  • the proven 6 to 9-month catalyst lifetime for the iron-based catalysts is at least twice that of competing FT processes. Due to the longer service life, the somewhat higher production costs of the catalyst according to the invention are compensated.
  • Another advantage is that the iron catalysts used in the FT process according to the invention have a significantly higher activity compared to the water gas shift reaction, in comparison to cobalt catalysts, which are commonly used in the low-temperature FT synthesis. This circumstance qualifies the FT technology according to the invention especially for the material utilization of C02-rich synthesis gases.
  • An important advantage of the FT method according to the invention compared to the comparable variants of the low-temperature FT synthesis, consists in the high quality of the kerosene produced.
  • aviation fuels are subject to extreme physical and chemical properties (ASTM certification), reflecting the complex interplay of safety and material requirements.
  • ASTM certification the product of the FT synthesis according to the invention can be approved as aerospace fuel 50.
  • the FT content of the FT product is almost exclusively aliphatic saturated hydrocarbons, and in order to meet the specification requirements for aviation fuel, aromatics must be generated by suitable processes for processing the FT Syncrudes
  • Another option is to add blending components, for example, from the processing of tars from coal fixed-bed gasification, as well as conventional low-pressure conditioning Temperature FT method generated aviation fuels is relatively expensive.
  • the synthetic FT kerosene according to the invention has a clear advantage in terms of particle emissions (reduction by 90%), SO emissions (reduction by 80%) and NOR emissions (reduction by 30%).
  • the newly developed Fe catalyst is the key of the technology of the present invention. It is characterized by high product selectivity, high shift activity (particularly important for C02-rich synthesis gases), low CH 4 formation rate, increased aromatics content in the FT product, long catalyst life and overall very low material costs. -> In combination with measure (c) Reduction of product production costs by approx. 1/3.

Abstract

La présente invention concerne un procédé pour produire des hydrocarbures à partir de gaz de synthèse au moyen d'un procédé à température de basse pression selon Fischer-Tropsch, ledit gaz de synthèse étant introduit dans un système de réservoirs à réacteurs en cascade ayant au moins trois réservoirs pour la réaction et un dispositif pour mettre en œuvre ce type de procédé, contenant un système de réservoirs à réacteurs ayant au moins trois réservoirs, dans lequel chaque réservoir est au moins équipé de réacteurs à lit catalytique fixe multitubes, d'échangeurs de chaleur et d'unités de séparation à plusieurs étages pour séparer les produits réactionnels.
PCT/EP2018/053689 2017-02-14 2018-02-14 Procédé à basse température selon fischer-tropsch WO2018149881A1 (fr)

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DE102017001627.5 2017-02-14
DE102017001627.5A DE102017001627A1 (de) 2017-02-14 2017-02-14 Vorrichtung und Verfahren zur Hochleistungs-OT-NT-FT-Synthese mit hohen Ausbeuten an FT-Produkten mit hoher Produktselektivität zur Aufbereitung zu flüssigen/festen industriellen Wachsen und zu flüssigen Kraftsstoffen(Kerosin/Diesel)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002008163A1 (fr) 2000-07-24 2002-01-31 Chevron U.S.A. Inc. Techniques permettant d'optimiser le procede fischer-tropsch de synthese d'hydrocarbures du type mazouts legers et/ou huiles de base lubrifiantes
US20040192989A1 (en) 2003-03-24 2004-09-30 Conocophillips Company Commercial fischer-tropsch reactor
US20120275975A1 (en) * 2011-04-01 2012-11-01 Ho Tae Lee Second stage fischer-tropsch reaction system to enhance the conversion of synthetic gas
US20150211766A1 (en) 2012-08-01 2015-07-30 Kobayashi Pharmaceutical Co., Ltd. Heating tool
WO2016138165A1 (fr) * 2015-02-25 2016-09-01 Sgc Energia S.A. (Formerly-Gi-Gasification International S.A.) Systèmes, procédés et appareils pour réacteurs de fischer-tropsch montés en cascade

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150217266A1 (en) 2012-09-07 2015-08-06 Afognak Native Corporation Systems and processes for producing liquid transportation fuels

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002008163A1 (fr) 2000-07-24 2002-01-31 Chevron U.S.A. Inc. Techniques permettant d'optimiser le procede fischer-tropsch de synthese d'hydrocarbures du type mazouts legers et/ou huiles de base lubrifiantes
US20040192989A1 (en) 2003-03-24 2004-09-30 Conocophillips Company Commercial fischer-tropsch reactor
US20120275975A1 (en) * 2011-04-01 2012-11-01 Ho Tae Lee Second stage fischer-tropsch reaction system to enhance the conversion of synthetic gas
US20150211766A1 (en) 2012-08-01 2015-07-30 Kobayashi Pharmaceutical Co., Ltd. Heating tool
WO2016138165A1 (fr) * 2015-02-25 2016-09-01 Sgc Energia S.A. (Formerly-Gi-Gasification International S.A.) Systèmes, procédés et appareils pour réacteurs de fischer-tropsch montés en cascade

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