AU2004280647B2 - Process for the production of multipurpose energy sources and multipurpose energy sources produced by said process - Google Patents

Description

WO 2005/035695 PCT/ZA2004/000125 Process for the Production of Multipurpose Energy Sources and Multipurpose Energy Sources Produced by Said Process Field of the Invention 5 The invention relates to the production of multipurpose hydrocarbonaceous energy sources and to multipurpose hydrocarbonaceous fuels. Background to the Invention 10 In this specification, the term "multipurpose hydrocarbonaceous energy sources" is abbreviated to MES and is used in both the singular and the plural. An MES usable in gas turbines, compression ignition (CI) engines, including 15 Homogeneous Charge Compression Ignition (HCCI) systems or fuel cells is an attractive option for many energy users, especially for those operating in remote stranded locations where a single form of supply of energy is required and simplified logistics are necessary. These entities include users in many classes of human activity. 20 US patent 6,475,375, discloses the process for the production of a synthetic naphtha fuel usable in CI engines. This patent, however, does not contemplate the use of such a fuel as an MES having broader application other than use thereof in a Cl engine. Thus, the disclosure in this patent does not provide any indication of how the problems associated with the production of an MES may be overcome or what characteristics or 25 properties such an MES should have. A synthetic multi-purpose fuel useful as a fuel cell fuel, diesel engine fuel, gas turbine engine fuel and furnace or boiler fuel are disclosed in PCT WO 01/59034. The multi purpose fuel produced ranged from C9 to C22. 30 The inventor has now identified a need and a process for at least partially satisfying such an MES need.

WO 2005/035695 PCT/ZA2004/000125 The Fischer-Tropsch (FT) process is a well known process in which carbon monoxide and hydrogen are reacted over an iron, cobalt, nickel or ruthenium containing catalyst to produce a mixture of straight and branched chain hydrocarbons ranging from methane to waxes with molecular masses above 1400 and smaller amounts of 5 oxygenates. The feed for the FT process may be derived from coal, natural gas, biomass or heavy oil streams. The term Gas-to-Liquid (GTL) process refers to schemes based on natural gas, which is mainly methane, to obtain the synthesis gas, and its subsequent conversion using in most instances an FT process. The quality of the GTL FT synthetic products is essentially the same obtainable from the FT process 10 here defined once the synthesis conditions and the product work-up are defined. The complete process can include gas reforming which converts natural gas to synthesis gas (H 2 and CO) using well-established reforming technology. Alternatively, synthesis gas can also be produced by gasification of coal or suitable 15 hydrocarbonaceous feedstocks like petroleum based heavy fuel oils. The synthesis gas is then converted into synthetic hydrocarbons. The process can be effected using, among others, a fixed-bed tubular reactor or a three-phase slurry reactor. FT products include waxy hydrocarbons, light liquid hydrocarbons, a small amount of unconverted synthesis gas and a water-rich stream. The waxy hydrocarbon stream and, almost 20 always, the light liquid hydrocarbons are then upgraded in the third step to synthetic fuels such as diesel, kerosene and naphtha. Heavy species are hydrocracked and olefins and oxygenates are hydrogenated to form a final product that is highly paraffinic. Hydrocracking and hydrogenation processes belong to the group sometimes generally named hydroconversion processes. 25 Summary of the Invention According to a first aspect of the invention, there is provided a multipurpose carbonaceous energy source (MES fuel), said energy source selected from: 30 - a substantially C5 to C9 cut having an H:C molar ratio from 2.26 to 2.32; - a substantially C5 to C9 cut blended with a substantially C9 to C14 cut, said blend having an H:C molar ratio from 2.18 to 2.24; WO 2005/035695 PCT/ZA2004/000125 - a substantially C5 to C9 cut blended with a substantially C9 to C14 cut and a substantially C14 to C22 cut, said blend having an H:C ratio from 2.12 to 2.18; and - a substantially C5 to C9 cut blended with a substantially C14 to C22 cut, said 5 blend having an H:C molar ratio from 2.13 to 2.19. The MES fuel options as defined in this invention are summarised in Table 1. Table 1: MES Fuels 10 Fuel Carbon Number Range H:C CO2 Emissions MES Cut A Cut B Cut C Ratio Cut C5-C9 C9-C14 C14-C22 Molar g C0 2 /g fuel 1 C5-C9 X 2.29 3.080 2 C5-C14 X X 2.20 3.098 3 C5-C22 X X X 2.14 3.111 4 C1- 22 X X 2.17 3.105 The MES fuel may, when combusted, have a C02 emission below 3.115 g C02/g fuel combusted. 15 One or more of the C5 to C9, C9 to C14, and C14 to C22 cuts may be synthetic in origin. One or more of the C5 to C9, C9 to C14, and C14 to C22 cuts may be Fischer-Tropsch 20 process in origin. The MES Fuel may be a partially or totally synthetic fuel. The MES Fuel may be a Fischer-Tropsch process derived fuel. 25 According to a second aspect of the invention, there is provided a process for the production of synthetic multipurpose carbonaceous energy source (MES fuels), said process including the steps of: '2, WO 2005/035695 PCT/ZA2004/000125 a) oxidising a carbonaceous material to form a synthesis gas; b) reacting said synthesis gas under Fischer-Tropsch reaction conditions to form Fischer-Tropsch reaction products; c) fractionating the Fischer-Tropsch reaction products to form one or more MES 5 blending components selected from the group including: A. a C5 to C9 cut; B. a C9 to C14 cut; and C. a C14 to C22 cut; and d) using said blending components in the production of the MES, provided that 10 where at least one of the blending components is a blending component in the C9 to C14 or in the C14 to C22 boiling range then at least two blending components are used in the production of the MES, one of which is the C5 to C9 cut. 15 The C5 to C9 cut may be a light hydrocarbon blend, typically in the 35-1600C distillation range. The C9 to C14 cut may be a medium hydrocarbon blend, typically in the 155-250'C distillation range. 20 The C14 to C22 cut may be a heavy hydrocarbon blend, typically in the 245-3600C distillation range. To obtain the MES fuels of Table 1, the blending components A, B and C, as described 25 above, may be blended in a volumetric ratio of A:B:C of: 1.0:0.0:0.0 for MES 1 and 1.2:1.0:0.0 for MES 2 1.8:1.0:2.3 for MES 3 30 1.0:0.0:2.1 for MES 4 to 1.0:1.2:0.0 for MES 2 1.0:1.2:1.8 for MES 3 1.0:0.0:1.5 for MES 4 WO 2005/035695 PCT/ZA2004/000125 To obtain the MES fuels of Table 1, the blending components A, B and C may be blended in a volumetric ratio of A:B:C, wherein: A may be from 1 to 2; 5 B may be from 0 to 1.5; and C may be from 0 to 2.5. One or more of the blending components may be hydroconverted. 10 Thus, the MES may be a blend of both hydroconverted and unhydroconverted blending components. The MES may be a product of one or more of only unhydroconverted blending components. 15 The MES may be a product of one or more only hydroconverted blending components. The Fischer-Tropsch process of step b) may be the Sasol Slurry Phase Distillate TM process. 20 The carbonaceous material of step a) may be a natural gas stream, a natural gas derivatives stream, a petroleum gas stream, a petroleum gas derivatives stream, a coal stream, a waste hydrocarbons stream, a biomass stream, and in general any carbonaceous material stream. 25 Optionally, hydrogen may be separated from the synthesis gas either during or after step a). This hydrogen may be used in the hydroconversion of FT primary products, namely FT 30 condensate and FT wax. Table 2 below gives a typical composition of the FT condensate and FT wax fractions.

WO 2005/035695 PCT/ZA2004/000125 Table 2: Typical Fischer-Tropsch product after separation into two fractions (vol% distilled) FT Condensate FT Wax (< 270*C fraction) (> 270*C fraction) C5-1600C 44 3 160-2700C 43 4 270-3700C 13 25 370-5000C 40 > 5000 C 28 5 In one embodiment of the invention, the hydroconverted products are fractionated in a common distillation unit where at least three blending components are recovered: (1) a light hydrocarbon blend, typically in the 35-1600C ASTM D86 distillation range, 10 i.e. C5 to C9; (2) a medium hydrocarbon blend, typically in the 155-250*C ASTM D86 distillation range, i.e. C9 to C14; and (3) a heavy hydrocarbon blend, typically in the 245-360*C ASTM D86 distillation range, i.e. C14 to C22. 15 However, in other embodiments, the FT condensate and FT wax are blended together before being fractionated into the blending components. In some embodiments the FT condensate is transferred directly to the products fractionator without any hydroconversion stage. 20 When processing using this approach, the MES products benefit from the synergy of the composition and quality of the wax and condensate fractions. MES fuels meet the fuel requirements of many classes of energy conversion systems 25 including gas turbines, Cl engines, including HCCI systems and fuel cells. The MES compositions may have the following properties which make it suitable for fuel cells, gas turbine engine and Cl engines (as shown in Table 3): 30 High Cetane Number: Fuels with a high cetane number ignite quicker and hence exhibit a milder uncontrolled combustion because the quantity of fuel involved is less. A WO 2005/035695 PCT/ZA2004/000125 reduction of the uncontrolled combustion implies an extension of the controlled combustion, which results in better air/fuel mixing and more complete combustion with lower NOx emissions and better cold start ability. The shorter ignition delay implies lower rates of pressure rise and lower peak temperatures and less mechanical stress. 5 The cetane number of the MES compositions was determined according to ASTM D613 test method and an Ignition Quality Tester (IQT - ASTM D6890). Near Zero-Sulphur Content: The sulphur content was determined according to the 10 ASTM D5453 test method. The less than 1 ppm sulphur present in the MES compositions not only make the components suitable for a fuel cell reformer catalyst, but also contribute to the lower exhaust emission in engines, such as Cl engines. The less than 1 ppm sulphur present in the MES composition either ensure compatible with certain exhaust catalyst devises or give improved compatibility with other. 15 Good Cold Flow Properties: Cold Filter Plugging Point (CFPP) is the lowest temperature at which the fuel can pass through a standard test filter under standard conditions (requires more than 1 minute for 20 ml to pass through a 45-pm filter). This test is done accordingly to the Institute of Petroleum IP 309 method or equivalent. 20 Inadequate cold flow performance will lead to difficulties with starting and blockage of Cl engine fuel filters under cold weather conditions. Freezing point is one of the physical properties used to quantitatively characterise gas turbine engine fuel fluidity. The low freezing point, determined in accordance with the 25 automated ASTM 5901 test method, or equivalent, can be attributed to the more than 60 mass% iso-paraffins present in MES compositions. Excellent Thermal and Oxidation Stability: The thermal stability of the MES compositions was determined according to the Octel F21-61 test method where a 30 visual rating was used to describe the relative stability. The FT products lead to significantly less carbon deposition on the fuel cell reformer catalyst than would be expected from a conventional diesel type feedstock under comparative reaction conditions.

WO 2005/035695 PCT/ZA2004/000125 Oxygen stability is tested through the calculation of the amount of insolubles formed in the presence of oxygen. It measures the fuel's resistance to degradation by oxygen by the ASTM D2274 test method or equivalent. The MES compositions are stable in the presence of oxygen with the formation of insolubles of less than 0.2 mg/100ml. 5 High Hydrogen To Carbon Content: The highly paraffinic nature of the FT products and very low aromatic concentration contribute to the high H:C ratios of the MES compositions. 10 In Table 1, four illustrative MES formulations are shown which have been found compatible with their proposed use in gas turbines, Cl engines, including HCCI systems and fuel cells. The expected quality and estimated yields of the MES formulations of Table I are presented in Table 3. 15 The MES compositions may be suitable for use in fuel cells, gas turbine engine and Cl engines, including HCC systems as they contain FT reaction derived products which are highly saturated with less than 2 volume% olefins, have ultra-low levels of sulphur with an almost zero aromatic hydrocarbon content, high linearity, high hydrogen to carbon ratio, very good cold flow properties, and high cetane number. 20 Lower reformer temperatures in fuel cells are required with the use of FT naphtha, kerosene or diesel. The FT products lead to significantly less carbon deposition on the catalyst than would be expected from a conventional diesel type feedstock under comparative reaction conditions and produce more steam. The MES components have 25 good cold flow properties as well as a high cetane number because of the predominantly mono-, and to a lesser extent other, branched forms of the paraffins which make these components suitable for application in gas turbine engines, Cl engines, including HCCI systems and fuel cells. 30 The highly paraffinic related properties such as high H:C ratio, high cetane number and low density together with virtually zero-sulphur and very low aromatics content give the FT products their very good emission performance 8a A further aspect of the present invention provides use of a C5 to C9 cut of hydroconverted Fischer-Tropsch reaction products in a process for the preparation of an MES fuel usable in a compression ignition engine, or in a gas turbine, or in a fuel cell, the process including the steps of: 5 a) oxidising a carbonaceous material to form a synthesis gas; b) reacting said synthesis gas under Fischer-Tropsch reaction conditions to form Fischer-Tropsch reaction products; c) hydroconverting said products; d) fractionating the hydroconverted Fischer-Tropsch reaction products 10 to form at least a C5 to C9 cut as a blending component A and one or more blending components selected from the group including: B. C9 to C14 cut; and C. C14 to C22 cut; and e) using said blending components in the production of said MES fuel; 15 wherein the same said MES fuel produced by steps a) to e) is suitable for use in each of said compression ignition engine, said gas turbine; and said fuel cell fuel. The C5 to C9 cut may be a light hydrocarbon blend having a 35-160'C distillation range. The C9 to C14 may be a medium hydrocarbon blend having a 155-2500C 20 distillation range. The C14 to C22 cut may be a heavy hydrocarbon blend having a 245 3600C distillation range. Components B and C may both be present and the fuel produced by the use of blending components A, B, and C blended in a volumetric ratio of A:B:C 25 wherein: A may be from 1 to 2; B may be up to 1.5; and/or C may be up to 2.5. The Fischer-Tropsch process of step b) may be a slurry phase distillate 30 process. The carbonaceous material of step a) may be a natural gas stream, a natural gas derivatives stream, a petroleum gas stream, a petroleum gas 8b derivatives stream, a coal stream, a waste hydrocarbons stream, a biomass stream, and in general any carbonaceous material stream. The fuel may include a substantially C5 to C9 hydroconverted cut blended with a substantially C9 to C14 hydroconverted cut, which cuts may have the 5 Fischer-Tropsch process as their origin, said blend having an H:C molar ratio from 2.18 to 2.24. The fuel may include a substantially C5 to C9 hydroconverted cut blended with a substantially C9 to C14 hydroconverted cut and a substantially C14 to C22 hydroconverted cut, which cuts have the Fischer-Tropsch process as their origin, 10 said blend having an H:C ratio from 2.12 to 2.18. The fuel may include a substantially C5 to C9 hydroconverted cut blended with a substantially C14 to C22 hydroconverted cut, said blend having an H:C molar ratio from 2.13 to 2.19. The fuel may have an oxidation stability of equal or less than 0.2 15 mg/1OOml. The fuel when combusted may yield a C02 emission below 3.115 gCO 2 /g fuel combusted.

WO 2005/035695 PCT/ZA2004/000125 Process Description This invention includes four possible processes for the production of MES components. 5 Two of them are based in the use of natural gas as feed and, the other two make use of any hydrocarbonaceous feedstock possible of been gasified. Therefore, feeds for the latter include coal, waste, biomass and heavy oil streams. The first process matter of this invention, presented in Figure 1, makes use of natural 10 gas 11 which is converted to synthesis gas at suitable process conditions in reformer 1. The reforming reaction makes use of oxygen 13 obtained from an air separation step 2 from atmospheric air 12. Water in the form of steam can also be used in the reforming process. 15 Syngas 14 from the reformer stage is converted in FT unit 3 to synthetic hydrocarbons including at least two liquid streams, as well as a gas stream and reaction water not shown. A portion of the syngas might be derived from the hydrogen separation plant 4 where a hydrogen rich stream 17 is produced for use in hydroconversion. Alternatively, hydrogen can be produced in an independent facility and transferred as stream 17. 20 The light synthetic hydrocarbons stream 15, sometimes named FT Condensate, includes paraffins, olefins and some oxygenates, mostly alcohols. This stream is transferred to hydrotreating unit 6 where olefins and oxygenates are hydrogenated into, mostly, the corresponding paraffin hydrocarbons. The process is completed at 25 conditions such that the average carbon number of the feed remains essentially unchanged in hydrotreated product 18. The heavy synthetic hydrocarbons 16, sometimes named FT Wax, has a similar chemical composition as that of the lighter stream 15; however, under normal 30 processing these species are solid at room temperature. This stream is transferred to the hydroconversion unit 5, preferably a hydrocracker system, where (1) olefins and oxygenates are hydrogenated to the corresponding paraffins which in turn and together with the original long chain paraffins (2) undergo cracking reactions resulting in a significant reduction of its average carbon number compared with that of the feed. The 35 resulting hydrocracked product 19 is a mixture of normal and iso-paraffins.

WO 2005/035695 PCT/ZA2004/000125 The combined hydroconverted products 18 and 19 are fractionated in distillation unit 7 resulting in at least four process streams. Stream 20 is a light hydrocarbon blend, typically in the 35-160'C ASTM D86 distillation range. Stream 21 is a medium 5 hydrocarbon blend, typically in the 155-250'C ASTM D86 distillation range. Stream 22 is a heavy hydrocarbon blend, typically in the 245-3600C ASTM D86 distillation range. Stream 23 includes unconverted species whose boiling points are above 3600C and is recycled to the hydrocracker to increase the production of the valuable species. The separation process also results in collecting a gas stream - not shown. 10 The MES products are produced using these streams on their own or in blends as shown in Table I above. An alternative second process scheme based on natural gas is presented in Figure 2. 15 From a process standpoint it differs from the one described before in that the light synthetic hydrocarbons 15 is not hydrotreated. Instead it is blended with the hydrocracked product 18. The resulting stream 19 is fractionated then in distillation unit 7 resulting in products 20-22 similar to those above described. However, while these products can be used in the same blends, they include some olefins and oxygenates in 20 their composition. Using alternative high molecular mass feedstocks this invention provides the process scheme shown in Figure 3. This concept makes use of coal, biomass or heavy oil which in the form of stream 11 is converted to synthesis gas at suitable process 25 conditions in gasifier 1. The gasification process makes use of oxygen 13 obtained from an air separation step 2 from atmospheric air 12. Water in the form of steam can also be used in the process. This process is then substantially similar to the one discussed before with reference to Figure 1. However, and as an additional stream, some liquids are produced during the gasification process and separated as stream 24. 30 These might be recovered as a product or recycled to the gasifier to enhance production of the valuable streams. Other than this, process units and streams in Figure 3 correspond to those in Figure 1 and its associated process description WO 2005/035695 PCT/ZA2004/000125 Finally, and as an alternative to this concept, it is provided a fourth process scheme similar in essence to the second option discussed here above. As the one just discussed, this makes use of coal, biomass or heavy oil as feedstock and makes use of gasifier I as described in the previous paragraph. This process is then substantially 5 similar to the one discussed before with reference to Figure 2. However, and as an additional stream, some liquids are produced during the gasification process and separated as stream 24. These might be recovered as a product or recycled to the gasifier to enhance production of the valuable streams. Other than this, process units and streams in Figure 4 correspond to those in Figure 2 and its associated process 10 description.

WO 2005/035695 PCT/ZA2004/000125 "J.i C 00 000 -t Cq C0 00 N CON 0 Xo w coc ' i 00 C) de co co) 't ) N 06 Ifl1 C0 6 cCY) 0 x N C) L )c )C -oJ M I--ov. C 1 C)C 0 C) c 0~ 0 0 0o x C', C0. - -C >~~0 a) I, vc AjCJ LOV .0 006 0 ) c- E oo CD CO~ = 0 ce) CO .~ L 0 0L - B L m 09 0 0~- 00 (L 0 CY c C)0 (U - C 0 aU 0-. 0 > @-0)( O S 2 :3 (0L-C' >-0,n0uC H 0>0 I- L 4-; - -5 . A 0 = L - o 12 Editorial note 2004280647 The following page has inadvertently been numbered page 12.

Claims (12)

1. Use of a C5 to C9 cut of hydroconverted Fischer-Tropsch reaction products in a process for the preparation of an MES fuel usable in a compression ignition engine, or in a gas turbine, or in a fuel cell, the process including the 5 steps of: a) oxidising a carbonaceous material to form a synthesis gas; b) reacting said synthesis gas under Fischer-Tropsch reaction conditions to form Fischer-Tropsch reaction products; c) hydroconverting said products; 10 d) fractionating the hydroconverted Fischer-Tropsch reaction products to form at least a C5 to C9 cut as a blending component A and one or more blending components selected from the group including: B. C9 to C14 cut; and C. C14 to C22 cut; and 15 e) using said blending components in the production of said MES fuel; wherein the same said MES fuel produced by steps a) to e) is suitable for use in each of said compression ignition engine, said gas turbine; and said fuel cell fuel.

2. Use as claimed in claim 1, wherein the C5 to C9 cut is a light hydrocarbon blend having a 35-1600C distillation range. 20

3. Use as claimed in claim 1, wherein the C9 to C14 is a medium hydrocarbon blend having a 155-250*C distillation range.

4. Use as claimed in claim 1, wherein the C14 to C22 cut is a heavy hydrocarbon blend having a 245-360*C distillation range.

5. Use as claimed in any one of claims 1 to 4, wherein components B and C 25 are both present and the fuel is produced by the use of blending components A, B, and C blended in a volumetric ratio of A:B:C wherein: A may be from 1 to 2; B may be up to 1.5; and/or C may be up to 2.5. 13

6. Use as claimed in any one of claims 1 to 5, wherein the Fischer-Tropsch process of step b) is a slurry phase distillate process.

7. Use as claimed in any one of claims 1 to 6, wherein the carbonaceous material of step a) is a natural gas stream, a natural gas derivatives stream, a 5 petroleum gas stream, a petroleum gas derivatives stream, a coal stream, a waste hydrocarbons stream, a biomass stream, and in general any carbonaceous material stream.

8. Use as claimed in any preceding claim, wherein the fuel includes a substantially C5 to C9 hydroconverted cut blended with a substantially C9 to C14 10 hydroconverted cut, which cuts have the Fischer-Tropsch process as their origin, said blend having an H:C molar ratio from 2.18 to 2.24.

9. Use as claimed in any of claims 1 to 7, wherein the fuel includes a substantially C5 to C9 hydroconverted cut blended with a substantially C9 to C14 hydroconverted cut and a substantially C14 to C22 hydroconverted cut, which 15 cuts have the Fischer-Tropsch process as their origin, said blend having an H:C ratio from 2.12 to 2.18.

10. Use as claimed in any of claims 1 to 7, wherein the fuel includes a substantially C5 to C9 hydroconverted cut blended with a substantially C14 to C22 hydroconverted cut, said blend having an H:C molar ratio from 2.13 to 2.19. 20

11. Use as claimed in any preceding claim, wherein the fuel has an oxidation stability of equal or less than 0.2 mg/1 00ml. 14

12. Use as claimed in any preceding claim, wherein the fuel when combusted yields a C02 emission below 3.115 gCO 2 /g fuel combusted. SASOL TECHNOLOGY (PTY) LTD WATERMARK PATENT & TRADE MARK ATTORNEYS P26997AU00