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
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1022—Fischer-Tropsch products
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/40—Characteristics of the process deviating from typical ways of processing
  • C10G2300/4012—Pressure

Definitions

• the present invention relates to a method to start a process for producing normally gaseous, normally liquid, and optionally normally solid hydrocarbons from a hydrocarbonaceous feedstock.
• the present invention relates to a method to start an integrated, highly efficient, low cost process providing operational flexibility for the production of hydrocarbons, in particular at remote locations as well a ⁇ at off-shore platforms .
• Various processes are known for the conversion of (gaseous) hydrocarbonaceous feedstocks, especially methane, natural gas and/or associated gs.s, into liquid products, especially methanol and liquid hydrocarbons, particularly paraffinic hydrocarbons. In this respect, reference is often made to remote locations and/or offshore locations, where no direct use of the gas is possible.
• WO 02/060841 relates to an integrated process for producing hydrocarbon products and energy in which FT steam (that is, steam produced by heat exchange between the reaction medium in a Fischer-Tropsch reaction and water) is superheated via a further heat exchange step against hot flue gas produced in a gas turbine generator.
• FT steam that is, steam produced by heat exchange between the reaction medium in a Fischer-Tropsch reaction and water
• the Fischer-Tropsch process is one process used for the conversion of hydrocarbonaceous feedstocks into gaseous, liquid and/or solid hydrocarbons.
• the feedstock is converted in a first step into a mixture of hydrogen and carbon monoxide (often referred to as synthesis gas or syngas) .
• the syngas is then converted in a second step over a suitable catalyst at elevated temperature and pressure into paraffinic carbons ranging from methane to high molecular weight molecules comprisir.g up to 200 carbon atoms, or, under particular circumstances even more.
• the Fischer-Tropsch reaction is very exothermic with the reaction temperature usually being controlled by indirect heat exchange of the reaction medium with water, the water being converted to saturated st.eam (called FT steam) .
• the Fischer-Tropsch process also produces a light product stream (also referred to as off gas, or t.ail gas) comprising unconverted synthesis gas, light hydrocarbon products (C1-C4 hydrocarbons, C2-C4 olefins and some oxygenates) as well as some carbon dioxide and inerts such as nitrogen and argon.
• a light product stream also referred to as off gas, or t.ail gas
• normally gaseous hydrocarbons are e.g. hydrocarbons which are gaseous at ambient conditions (20 0 C, 1 bar) . Examples are saturated C1-C4 hydrocarbons.
• Normally liquid hydrocarbons are liquid at ambient conditions (20 0 C, 1 bar) .
• Examples are saturated C ⁇ -n-Ci5, as well as C5-i-C]_g compounds. Normally solid hydrocarbons are solid at ambient conditions (20 0 C, 1 bar) . Examples are saturated n-C]_5 and higher normal hydrocarbons, as well as most i-C2o ⁇ compounds .
• FT steam has a pressure in the range of from 15 to
• MP steam is (usually) FT steam which is further heated in the range of 20-150 0 C, preferably 50-120 0 C, more preferably 70-90 0 C, above the FT steam temperature, such that it is unsaturated FT steam having a pressure in the range of from 15 to 40 bar and a temperature of from 220 0 C to 400 0 C, preferably in the range 250 °C-370 0 C, more preferably in the range 280 0 C-330 C C; and
• HP steam has a pressure in the range of from 55 to 150 bar and is preferably superheated with respect to MP steam by 10-100 0 C, preferably by about EO 0 C, such as being in the range 230 °C-500 0 C, preferably in the range 260 °C-470 0 C, more preferably in the range 280 0 C-40 0 C, and even more preferably in the range 330 °C-380 0 C.
• the present invention provides a method to start up a process for the production of normally gaseous, normally liquid, and optionally normally solid hydrocarbon products from a hydrocarbonaceous feedstock comprising the steps of (1) producing high pressure (HP) steam, preferably HP superheated steam, by means of at least one gas turbine generator and optionally one or more boilers fed with a hydrocarbonaceous feedstock;
• HP high pressure
• step 5 converting the synthesis gas produced according to step 5 exothermally to a range of normally gaseous, normally liquid, and optionally normally solid hydrocarbon products in a Fischer-Tropsch reaction;
• step 6 controlling the reaction temperature of step 6 by indirect heat exchange of the reaction medium with water, the water being converted to saturated st.eam (FT steam) ;
• step 6 separating the hydrocarbon products: produced in step 6 into a light product stream (comprising any unconverted syngas and at least part of t.he normally gaseous hydrocarbon products) and a heavy product stream (comprising the normally liquid and optionally normally solid hydrocarbon products) ;
• the gas turbine generator (s) and/or the boiler (s) of step 1 includes one or more gas turbine heat recovery steam generators (HRSG) .
• HRSG gas turbine heat recovery steam generators
• a HRSG is a steam generator known in the art, and is commorLly a downstream part of a gas turbine generator or a boiler. It can be separate or integral with a generator or boiler.
• the heat recovery comprises several heat exchangers, e.g. a heater to convert water into saturated steam, a superheater to convert saturated steam into unsaturated steam and an economiser, to heat up boiler feed water to its boiling point.
• one or more duct burners are present to increase the steam product.ivity.
• the high pressure (HP) steam is at a pressure between 55 and 150 bar and at a temperature of 330 to 380 0 C and/or the medium pressure (MP) steam is at a temperature of 280 to 330 0 C.
• the process according to the invention has the advantage of providing considerable flexibility at the start up of a process for the production of hydrocarbons products from a hydrocarbonaceous feedstock where downstream energy and steam (FT steam) are not available at the time of start up.
• the present invention allows more flexibility in the design of a hydrocarbcn synthesis plant.
• the cooling system of a hydrocarbon synthesis plant will produce saturated steam.
• a very generally used cooling system is a thermo-syphon system in which hot boiler feed water is introduced at a low level in a reactor. Eart of the water is converted into steam, and at the top cf the reactor a mixture of steam and water is transferred, to the so called steam drum. Steam is removed from the steam drum, and the water, together with make-up boiler feed water, is returned to the reactor. The saturated, steam thus produced needs to be heated as quickly a ⁇ possible to avoid condensation in the lines.
• the saturated steam needs to be converted into unsaturated steam at a location close to the hydrocarbon synthesis reactor.
• a steam/ steam heat exchanger which is fed with high pressure:, preferably superheated, steam.
• high pressure preferably superheated
• gas turbines make it possible to locate the gas turbines at a more suitable location, generally being separate or distal to the reactor, and still heat the saturated hydrocarbon conversion steam close to the hydrocarbon synthesis reactor. This still overcomes the problems caused by the formation of (large amounts of) condensate in the reactor exit lines or pipes.
• the gas turbine generator (s) and any boiler (s) run at full capacity.
• the generator operation may be reduced to (and maintained at) a much lower steam production level in the event that it should be necessary to re-engage it in order to generate more steam.
• a natural gas fired boiler (s) is used for the start up of the process for producing hydrocarbon products from a hydrocarbonaceous feedstock, it can help provide the necessary steam for the generation of power to start the overall process.
• the boiler may be maintained in .hot standby mode for emergency situations and still operate at low cost.
• the boiler may be fired with any suitable fuel source, for example Fischer-Tropsch off gas instead of natural gas.
• a boiler cannot generate electricity, and thus is less flexible.
• the gas turbine generator of step 9 is preferably that at least one gas turbine generator of step 1.
• the heat exchange in step (vi) is done in a condensing mode to maximise the efficiency of the total process.
• the present invention also provides an integrated process for producing normally gaseous, normally liquid, and optionally normally solid hydrocarbon products and energy comprising the steps of:
• step (i) converting a hydrocarbonaceous feedstock into syngas ;
• step (iia) converting in a Fischer Tropsch reaction at least part of the syngas of step (i) exothermically to normally gaseous, normally liquid, and optionally normally solid hydrocarbon products;
• step (iii) separating the reaction products produced in step (iia) into a heavy product stream (comprising the normally liquid and optionally normally gaseous hydrocarbon products) and a light product stream (comprising any unconverted syngas and at least part of the normally gaseous hydrocarbon products);
• step (iv) cooling and/or feeding fuel to one or more gas turbine generators and burning it to forir hot flue gas and energy; (v) producing high pressure (HP) , preferably superheated, steam by heat exchange of water against the hot flue gas from step (iv) ; and
• step (vi) cooling and/or condensing at leanst part of the HP (superheated) steam from step (v) in s heat exchanger against at least part of the FT steam from step (iib) to form MP steam.
• part of the HP superheated steam from step (v) may be depressurised (reduced in pressure) to produce medium pressure (MP) steam.
• the e.bove step (vi) is carried out in a condensing steam mode:.
• the condensed steam (or condensate) may be re-used as boiler feed water.
• the gas turbine generator (s) of step (iv) includes one or more gas turbine heat recovery steam generators (HRSG) .
• HRSG is a steam generator known in the art, and is commonly a downstream part of a gas turbine generator. It can be separate or integral with a generator.
• the fuel for the gas turbine generator may be any suitable combustible substance known in the art, including a hydrocarbonaceous feedstock or at least part, possibly all, of the light product steam produced according to step (iii) .
• step (vi) is done in a condensing mode to maximise efficiency.
• Figure 1 is a schematic diagram of a Fischer-Tropsch process and some supporting utilities for producing hydrocarbons from a hydrocarbonaceous feedstock using the claimed start up method.
• the hydrocarbon production process begins with the conversion of a hydrocarbonaceous feedstock into syngas (i) by means of catalytic reforming, auto thermal reforming, partial oxidation and/or combinations thereof in the appropriate apparatus fed by a hydrocarbonaceous feedstock such as natural gas, coal or biomass and, where necessary, oxygen and/or steam.
• a hydrocarbonaceous feedstock such as natural gas, coal or biomass and, where necessary, oxygen and/or steam.
• the syngas is converted (ii) exothermically at elevated temperatures and pressures in the presence of a suitable Fischer-Tropsch catalyst to a range of hydrocarbon products.
• the reaction temperature may be controlled by indirect heat exchange of the reaction medium with water (indicated in Figure 1 as boiler feedwater (BFW) ) which is converted into steam (herein after referred to as FT steam) .
• BFW boiler feedwater
• the Fischer-Tropsch products are converted (iii) into a heavy product stream which is drawn off, and a light product stream (or off-gas) .
• a major part of the light gas is recycled to the syngas production process.
• an optimum carbon efficiency is obtained.
• 20 - 90% of the light product is recycled, especially 40 - 80%.
• At least part of the light product stream is fed to a combustion chamber of a gas turbine generator (iv) , and/or the burners of a HRSG, to form combusted gas, which is subsequently combusted through an expansion chamber to form hot flue gas while at the same time generating electricity or driving a compressor (for example for powering an ASU) .
• Boiler feedwater is heated by heat exchange against the hot flue gas to produce HP superheated steam in a series of heat exchangers, in Figure 1 designated (va) , (vb) and (vc) .
• (va) may be an economiser, (vb) an evaporator and (vc) a superheater.
• the HP steam is condensed in a heat exchanger against at least part of the FT steam produced by heat exchange with the FT reaction medium in order to superheat the FT steam. Thereafter, at least part of the superheated FT steam is fed to steam turbines to generate electricity and/or mechanical power.
• turbines driven by the superheated FT steam may be used to drive compressors in steps (i) , (ii) and/or (iii) .
• a hydrocarbonaceous feed (ix) may be used to feed a fired heater in the production of HP superheated steam ( (v) above) .
• part of the superheated HP steam may be depressurised to MP steam (x) where insufficient FT steam from step (iii) is available.
• the depressurising step may be carried out via an appropriate valve .
• hydrocarbonaceous feed may be fed (xi) to the gas turbines in case of insufficient light product stream from step (iii) is available.
• start up energy in the form of a hydrocarbonaceous feedstock for example natural gas
• the start up method of the invention is controlled and safe not only under fresh start conditions, but also under restart conditions.
• the start up method of the invention also provides flexibility for quick response to changing conditions, in particular via step (x) whereby HP steam is converted to MP steam to provide elect.rical or mechanical power for other components wit.hin the system.
• the present invention facilitates a FT process in which FT steam is heated by indirect heat exchange (step (vi) ) to produce MP steam.
• the reaction temperature in the FT reactor is control Led by heat exchange with water being converted to saturated FT steam.
• the FT steam is primarily used as feed for a steam turbine (iv) which thereby generates electrical and/or mechanical energy. However, in order to prevent excessive condensation in the steam turbines the FT steam needs to be superheated. According to the invention, the FT steam is superheated by indirect heat exchange by means of condensation of HP steam (see step (vi) ) .
• the superheated temperature of the HP steam is such that the temperature after isoenthalpic depressurisation of the HP steam to the FT steam pressure, is equal to or higher than the temperature of the superheated FT steam.
• step (vi) involves cooling or condensing HP steam against saturated FT steam as opposed to a heat exchange process which involves heat trarsfer from flue gas to the FT steam stream.
• the superheated HP steam is produced in a heat recovery steam generator utilising hot flue gas.
• the hot flue gas in turn originates from the expansion chamber of a gas turbine generator and/or from a burner integrated within the heat recovery steam generator.
• HP pressure and superheat temperature may be made in orde r to ensure that the heat recovery steam generator operates under conditions suitable to provide energy to superheat the FT steam during steady state operations, as well as to provide MP steam in the situation where insufficient or no FT steam is available (for example at start up) .
• operation of an integrated FT process requires flexibility between external energy sources (such as natural gas) and light FT products (off-gas) on the fuel side, and optimal flexibility between FT steam and MP steam production on the steam side for reliable operation and start up/shut down reasons.
• the present invention provides such operational flexibility.
• the means for providing additional heat or heating serves to assist the provision of steam by the heating or superheating of water by the exhaust flue gases.
• the additional heat or heating could be provided by any suitable means, including one or more burners, such as duct burners known in the art.
• the means is located in a suitable position, for example, in the direct vicinity of the heat exchangers.
• the means may be powered by any suitable fuel source, including for example, the fuel source (s) (such as syngas) used for the gas turbine or other parts of the hydrocarbon synthesis plant.
• Such means may be operable at different conditions, e.g. temperature, at different locations.
• the means for compressing and optionally separating an oxygen containing gas is suitably one or more air separation units known in the art.
• the hydrocarbonaceous feed stock is suitably methane, natural gas, associated gas or a mixture of
• the feed comprises mainly, i.e. more than 90 v/v%, especially more than 94%,
• C ] __4 hydrocarbons especially comprises cLt least 60 v/v percent methane, preferably at least 75%, more preferably
• hydrocarbons mentioned in the present description are suitably 04.24 hydrocarbons, especially 05.20 hydrocarbons, more especially C 6-16 hydrocarbons, or mixtures thereof. These hydrocarbons or mixtures thereof are liquid at temperatures between 5 and 30 C (1 bar) , especially at about 20 0 C (1 bar) , and usually are paraffinic of nature, while up to 24 wt%, preferably up to 12 wt%, of either olefins or oxygenated compounds may be present.
• normally gaseous hydrocarbons normally liquid hydrocarbons and optionally normally solid hydrocarbons are obtained. It is often preferred to obtain a large fraction of normally solid hydrocarbons. These solid hydrocarbons may be obtained up to 85 wt% based on total hydrocarbons, usually between 50 and 75 wt%.
• the partial oxidation and/or reforming of gaseous feedstocks, producing mixtures of especially carbon monoxide and hydrogen, can take place according to various established processes. These processes include the Shell Gasification Process. A comprehensive survey of this process can be found in the Oil and Gas Journal, September 6, 1971, pp 86-90.
• the oxygen containing gas used in cor.version of hydrocarbonaceous feed into syngas may be; air (containing about 21 vol. percent of oxygen), oxygen enriched air, suitably containing up to 70 percent, or substantially pure air, containing typically at least 95 vol.%, usually at least 98 vol.%, oxygen.
• Oxygen or oxygen enriched air may be produced via cryogenic techniques, but could also be produced by a membrane based process, e.g. the process as described in WO 93/06041.
• At least initially the boiler provides a power source for driving at least one air compressor or separator of the air compression/separating unit.
• carbon dioxide and/or steam may be introduced into the partial oxidation process or combined partial oxidation and reforming process.
• the partial oxidation process is defined as including partial oxidation, non- catalytic and catalytic, with or without a flame and with or with out steam and/or carbon dioxide injection.
• the percentage of hydrocarbonaceous feed which is converted in the first step of the process of the invention is suitably 50-99% by weight and preferably 80-98% by weight, more preferably 85-96% by weight.
• the gaseous mixture comprising predominantly hydrogen, carbon monoxide and optionally nitrogen, is contacted with a suitable catalyst in the catalytic conversion stage, in which the hydrocarbons are formed.
• a suitable catalyst in the catalytic conversion stage, in which the hydrocarbons are formed.
• at least 70 v/v% of the syngas is contacted with the catalyst, preferably at least 80%, mere preferably at least 90%, still more preferably all the syngas.
• step (ii) represents a Fischer-Tropsch synthesis reaction in which case conversion of the mixture comprising hydrogen and carbon monoxide into hydrocarbons utilises a catalyst known in the art and usually referred to as a Fischer-Tropsch catalyst.
• Catalysts for use in the Fischer-Tropsch hydrocarbon synthesis process frequently comprise, as the catalytically active component, a metal from Group VIII of 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) .
• Particular catalytically active metals include ruthenium, iron, cobalt and nickel. Cobalt is a preferred catalytically active metal.
• 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 and titania.
• the amount of catalytically active metal on the carrier 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. (pbw - parts by weight) .
• the catalyst may also comprise one or more metals or metal oxides as promoters.
• Suitable metal oxide promoters may be selected from Groups HA, IHB, IVB, VB and VIB of the (same) Periodic Table, or the actinides and lanthanides .
• oxides of magnesium, calcium, strontium, barium, scandium, yttrium, lanthanum, cerium, titanium, zirconium, hafnium, thorium, uranium, vanadium, chromium and manganese are most suitable promoters.
• Particularly preferred metal oxide promoters for the catalyst used to prepare the waxes for use in the present invention are manganese and zirconium oxide.
• Suitable metal promoters may be selected from Groups VIIB or VIII of the (same) Periodic Table.
• Rhenium 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 1OC pbw, preferably 0.1 to 40, more preferably 1 to 20 pbw, per 100 pbw of carrier.
• the catalytically active metal and th ⁇ promoter, if present, may be deposited on the carrier material by any suitable treatment, such as impregnation, kneading and extrusion.
• the loaded carrier is typically subjected to calcination at a temperature of generally from 350 to 750 0 C, preferably a temperature in the range of from 450 to 550 0 C.
• the effect of the calcination treatment is to remove crystal water, to decompose volatile decomposition products and to convert organic and 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 200 to 350 0 C.
• 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 100 to 600 0 C, preferably from 150 to 350 0 C, more preferably from 180 to 270 0 C, and most preferably from 200 to 250 0 C. Typical total pressures for the catalytic conversion process are in the range of from 1 to 2OC bar absolute, more preferably from 10 to 70 bar absolute. In the catalytic conversion process mainly (at least 70 wt%, preferably 90 wt% of C5+ hydrocarbons are formed.
• a Fischer-Tropsch catalyst which yields substantial quantities of paraffins, more preferably substantially unbranched paraffins.
• a part may boil above the boiling point range of the: so-called middle distillates, to normally solid hydrocarbons.
• a most suitable catalyst for this purpose is a cobalt- containing Fischer-Tropsch catalyst.
• middle distillates is a reference to hydrocarbon mixtures of which the boiling point range corresponds substantially to that of kerosene and gas oil fractions obtained in a conventional atmospheric distillation of crude mineral oil.
• the boiling point range of middle distillates generally lies within the range of 150 to 360 0 C.
• the higher boiling range paraffinic hydrocarbons may be isolated and subjected to a catalytic hydrocracking step, which is known per se in the art, to yield the desired middle distillates.
• the catalytic hydro-cracking is carried out by contacting the paraffinic hydrocarbons at elevated temperature and pressure and in the presence of hydrogen with a catalyst containing one or more metals having hydrogenation activity, and supported on a carrier.
• Suitable hydro- cracking catalysts include catalysts comprising metals selected from Groups VIB and VIII of the Periodic Table of Elements.
• the hydrocrackirg catalysts contain one or more noble metals from Group VIII.
• Preferred noble metals are platinum, palladium, rhodium, ruthenium, iridium and osmium. Most preferred catalysts for use in the hydrocracking stage are those comprising platinum.
• the amount of catalytically active metal present in the hydrocracking catalyst may vary with..n wide limits and is typically in the range of from 0.05 to 5 parts by weight per 100 parts by weight of the carrier material.
• Suitable conditions for the catalytic: hydrocracking are known in the art. Typically, the hydrocracking is effected at a temperature in the range of from 175 to 400 0 C. Typical hydrogen partial pressures applied in the hydrocracking process are in the range of from 10 to 250 bar.
• the FT process (step (ii) ) may be operated in a single pass mode ("once through") or in a recycle mode.
• the process may be carried out in one or more reactors, either parallel or in series.
• the preference will be to use only one reactor.
• Slurry bed reactors, ebulliating bed reactors and fixed bed reactors may be used, the fixed bed reactor being the preferred option.
• the product of the hydrocarbon synthesis and consequent hydrocracking suitably comprises mainly normally liquid hydrocarbons, beside water and normally gaseous hydrocarbons.
• the catalyst and the process conditions in such a way that especially normally liquid hydrocarbons are obtained, the product obtained (“syncrude”) may transported in the liquid form or be mixed with any stream of crude oil without creating any problems as to solidification and or crystallization of the mixture. It is observed in this respect that the production of heavy hydrocarbons, comprising large amounts of solid wax, are less suitable for mixing with crude oil while transport in the liquid form has to be done at elevated temperatures, which is Less desired.

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• Organic Chemistry (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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• 2006
  • 2006-07-14 EP EP06764177A patent/EP1904422A1/en not_active Withdrawn
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  • 2006-07-14 WO PCT/EP2006/064266 patent/WO2007009951A1/en active Application Filing
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