WO2001083641A2 - Winter diesel fuel production from a fischer-tropsch wax - Google Patents
Winter diesel fuel production from a fischer-tropsch wax Download PDFInfo
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- WO2001083641A2 WO2001083641A2 PCT/US2001/009903 US0109903W WO0183641A2 WO 2001083641 A2 WO2001083641 A2 WO 2001083641A2 US 0109903 W US0109903 W US 0109903W WO 0183641 A2 WO0183641 A2 WO 0183641A2
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Classifications
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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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
Definitions
- This invention relates to the production of fuels from waxy, paraffinic hydrocarbons produced by the reaction of CO and hydrogen, via the Fischer- Tropsch hydrocarbon synthesis process.
- this invention relates to a diesel fuel and a process for its production, useful as a winter diesel fuel derived from wax containing Fischer-Tropsch feeds utilizing a multi-zone isomerization process to yield diesel fuels having both excellent low temperature properties and emissions performance.
- diesel fuels Upon combustion in a vehicular diesel engine, diesel fuels are known to emit undesirable pollutants, for example; solid particulate matter (PM) e.g., soot, as well as gaseous pollutants, e.g., unburned hydrocarbons (HC), carbon monoxide (CO), and nitrogen oxides (NOx).
- PM solid particulate matter
- gaseous pollutants e.g., unburned hydrocarbons (HC), carbon monoxide (CO), and nitrogen oxides (NOx).
- HC unburned hydrocarbons
- CO carbon monoxide
- NOx nitrogen oxides
- winter diesel fuels need exceptional low temperature flow properties, Accordingly, there have been numerous government and industry efforts to design winter fuels for use in the mogas/diesel markets to address the winter emissions quandary.
- the current results are winter diesel fuels which are traditionally blended with, or consist essentially of kerosene and are characterized by improved cold flow properties.
- Fischer-Tropsch fuels are well known as high cetane number fuels.
- these fuels due to the highly paraffinic nature of Fischer-Tropsch fuels, these fuels generally possess mediocre to poor cold flow properties, i.e., cloud point and cold filter plugging point.
- the heaviest paraffin molecules tend to crystallize as wax particles and precipitate above certain temperatures, resulting in high freeze point and/or cloud point. This makes it difficult or even impossible to use such products in many environments. Improving the cold flow properties of these fuels generally leads to decreasing the cetane number as is the case with conventional fuels.
- a novel process for the production of a fuel, useful as a winter diesel fuel, derived from Fischer-Tropsch products, which meets cold flow standards while simultaneously providing superior emissions performance comprises separating the paraffinic, wax containing Fischer-Tropsch product into a 300° F+ distillate fraction and upgrading the fraction via hydroisomerization and selective catalytic dewaxing to produce a diesel fuel with excellent low temperature properties and reduced emissions.
- a 300° F+ (149° C+) fraction derived from the Fischer- Tropsch process is passed into a first reaction zone, of two sequential isomerization reaction zones in a single reaction stage, the first reaction zone comprising a first catalyst containing a suitable hydroisomerization catalyst, to form a first zone effluent.
- a portion of the liquid product from the first zone effluent preferably the entire liquid product from the first zone effluent, is passed into a second reaction zone, comprising a second catalyst having a catalytic dewaxing functionality, to form a second zone effluent.
- the second reaction zone may contain a mixture or composite comprising both catalytic dewaxing and hydroisomerization catalysts.
- the first and second zones may be in the same or separate reaction vessels and preferably both zones are contained in the same reaction vessel. Further, the first and/or second reaction zone may comprise one or more catalyst beds.
- the second zone effluent comprises an isomerized hydrocarbon product and can be fractionated into desired liquid product fractions, e.g., a 320-700° F boiling fraction.
- 300° F+ fraction is meant the fraction of the hydrocarbons synthesized by the Fischer-Tropsch process and boiling above a nominal 300° F boiling point. At least a portion of the product of the second reaction zone is recovered to produce a middle distillate boiling in the diesel fuel range, i.e., a 320-700° F boiling fraction.
- the process is conducted in the absence of intermediate hydrotreating, and produces products with excellent cold flow characteristics, i.e., cloud and freeze point, superior smoke point and better than expected emissions characteristics.
- Such distillate products can be used as diesel fuels or as blending components therefor.
- this isomerized product of the second zone effluent produces a fuel having a T95 (the temperature at which most all the material has boiled off, leaving only 5% remaining in the distillation pot) greater than or equal to 240° C (464° F) but less than or equal to 350° C (662° F), preferably a T95 greater than or equal to 245° C (473° F) but less than or equal to 340° C (644° F), more preferably a T95 greater than or equal to 245° C (473° F) but less than or equal to 335° C (635° F) and having a cold filter plugging point as determined by IP-309 below about -35° C, more preferably below about -40° C and contains:
- paraffins at least 90+ wt%, preferably at least 95+ wt , more preferable at least 99+ wt%
- cetane number > 65, preferably > 70, more preferably > 75
- the invention comprises a Fischer-Tropsch hydrocarbon synthesis process, in which a synthesis gas comprising a mixture of H 2 and CO, react in the presence of a suitable Fischer-Tropsch hydrocarbon synthesis catalyst, to form a hydrocarbon product wherein a 300° F + distillate fraction and hydrogen or a hydrogen containing gas is passed into a first reaction zone, having a first catalyst comprising a suitable hydroisomerization catalyst to form a first zone effluent and the total liquid product from the first zone effluent is passed into a second reaction zone having a second catalyst containing either a catalytic dewaxing catalyst, a hydroisomerization catalyst or a mixture thereof, to form a second zone effluent comprising an isomerized hydrocarbon product.
- a synthesis gas comprising a mixture of H 2 and CO
- a middle distillate fuel, useful as a diesel fuel is recovered from the hydrocarbon product of the second reaction zone.
- good yields of distillate fuels with excellent cold flow properties are produced from wax containing paraffins derived from the Fischer- Tropsch process to produce a full boiling range diesel fuel, preferably a 320-700° F fraction, with the unique combination of high cetane number, very low cloud and cold filter plugging point (CFPP) performance and full boiling range cut exhibiting superior emissions performance.
- CFPP cold filter plugging point
- all or part of the hydrocarbon product recovered from the second reaction zone can be combined or blended and used as a winter diesel fuel.
- the product of this invention can be used in relative minor amounts, e.g., 10% or more, for significantly improving the final blended diesel product.
- Figure 1 is an illustration of the experimental reactor used to produce the comparative test fuels of this invention as described in the examples.
- the Fischer-Tropsch process is well known to those skilled in the art, see for example, U.S. Patent Nos. 5,348,982 and 5,545,674 herein incorporated by reference.
- the Fischer-Tropsch process involves the reaction of a synthesis gas feed comprising hydrogen and carbon monoxide fed into a hydrocarbon synthesis reactor in the presence of a Fischer-Tropsch catalyst, generally a supported or unsupported Group VIII, non-noble metal e.g., Fe, Ni, Ru, Co and with or without a promoter e.g., ruthenium, rhenium and zirconium.
- a Fischer-Tropsch catalyst generally a supported or unsupported Group VIII, non-noble metal e.g., Fe, Ni, Ru, Co and with or without a promoter e.g., ruthenium, rhenium and zirconium.
- These processes include fixed bed, fluid bed and slurry hydrocarbon synthesis.
- a preferred Fischer-Tropsch process is one that utilizes a non-shifting catalyst, such as cobalt or ruthenium or mixtures thereof, preferably cobalt, and preferably a promoted cobalt, the promoter being zirconium or rhenium, preferably rhenium.
- a non-shifting catalyst such as cobalt or ruthenium or mixtures thereof, preferably cobalt, and preferably a promoted cobalt, the promoter being zirconium or rhenium, preferably rhenium.
- Such catalysts are well known and a preferred catalyst is described in U.S. Patent No. 4,568,663 as well as European Patent 0266 898.
- the synthesis gas feed used in the process comprises a mixture of H 2 and CO wherein H2:CO are present in a ratio of at least about 1.7, preferably at least about 1.75, more preferably 1.75 to 2.5.
- the high proportion of normal paraffins in the product produced by the Fischer-Tropsch process must be converted from wax containing hydrocarbon feeds into more useable products, such as transportation fuels.
- conversion is accomplished primarily by hydrogen treatments involving hydrotreating, hydroisomerization, and hydrocracking in which a suitable fraction of the product is contacted with a suitable catalyst in the presence of hydrogen to isomerize the fraction by converting the molecular structure of at least a portion of the hydrocarbon material from normal paraffins to branched iso-paraffins to form the desired product, as is known to those skilled in the art.
- the feedstock for this invention can be described as a wax containing Fischer-Tropsch product, and this product can contain C5+ materials, preferably C10+, more preferably
- a wax containing paraffin feed stock derived from the Fischer-Tropsch process is separated, usually by fractionation, into a 300° F+ distillate fraction.
- the feed also comprises more than 90% paraffinic hydrocarbons, most of which are normal paraffins.
- the feed preferably has negligible amounts of sulfur and nitrogen compounds with less than 2000 wppm, preferably less than 1000 wppm and more preferably less than 500 wppm of oxygen in the form of oxygenates.
- the 300° F+ Fischer-Tropsch derived fraction is then upgraded via a single stage isomerization process, i.e., the liquid product of the first reaction zone is passed directly into the second reaction zone, comprising hydroisomerization followed by selective catalytic dewaxing.
- the single stage reduces product loss and avoids the need for two parallel reactions stages.
- the 300° F+ distillate fraction is passed into a first reaction zone, comprising a hydroisomerization catalyst to form a first zone effluent wherein at least a portion of the liquid product of the first zone effluent is passed into a second reaction zone, comprising a catalyst having a catalytic dewaxing function, to form a second zone effluent comprising a hydroisomerized hydrocarbon product.
- a first reaction zone comprising a hydroisomerization catalyst to form a first zone effluent wherein at least a portion of the liquid product of the first zone effluent is passed into a second reaction zone, comprising a catalyst having a catalytic dewaxing function, to form a second zone effluent comprising a hydroisomerized hydrocarbon product.
- the entire liquid product existing under the conditions of the first reaction zone pass directly into the second reaction zone.
- the first zone effluent may also comprise light gases and naphtha which pass into the second reaction zone.
- the light gas and/or naphtha fractions may be separated before the first zone effluent is transferred to the second reaction zone. Further, additional hydrogen or other quench gases may be injected before passing the effluent of the first zone into the second reaction zone.
- the Fischer-Tropsch derived wax containing feed is subjected to hydroisomerization in the first reaction zone in the presence of hydrogen, or a hydrogen containing gas, to convert a portion of the normal paraffins to isoparaffins.
- the degree of hydroisomerization is measured by the amount of boiling point conversion, i.e., the amount of 700° F+ hydrocarbons converted to 700° F- hydrocarbons.
- At least a portion of the liquid product from the first zone effluent is passed into a second reaction zone containing a dewaxing catalyst, a hydroisomerization catalyst or a mixture thereof, designed to minimize boiling point conversion while improving cold flow/cloud point properties by reacting at least a portion of the remaining n- paraffins contained in the first zone effluent to further isomerize the n-paraffins to isoparaffins or crack larger chain paraffins to smaller chain paraffins which are, in turn, isomerized to iso-paraffins or selectively crack the n-paraffins.
- the dewaxing reaction within the second reaction zone is conducted until a cold filter plugging point for the second zone effluent at or below about -35° C, more preferably below -40° C is achieved.
- the dewaxing reaction may be conducted until a cloud point for the second zone effluent at or below about -35° C, more preferably below -40° C is achieved.
- a hydrocarbon product is recovered from the second zone effluent having a T95 greater than or equal to 240° C (464° F) but less than or equal to 350° C (662° F), preferably a T95 greater than or equal to 245° C (473° F) but less than or equal to 340° C (644° F), more preferably a T95 greater than or equal to 245° C (473° F) but less than or equal to 335° C (635° F).
- the cold flow and emission properties of the resulting distillate fuel are excellent, making the product useful as a winter diesel fuel.
- Hydroisomerization and hydrocracking are well known processes for upgrading hydrocarbon synthesis products and the conditions employed can vary widely. Accordingly, applicants' isomerization process may be employed in either a single stage or dual reactor system depending on the desired catalysts utilized for each reaction zone.
- hydroisomerization and catalytic dewaxing are conducted in a single stage, fixed bed reactor comprising a first and second reaction zone wherein a hydroisomerization catalyst and catalytic dewaxing catalyst operate to convert 10-80% of the 700° F+ materials to 700° F- materials and selectively dewax the feed to achieve a cold filter plugging point below about -35° C.
- the first reaction zone preferably comprises a first catalyst layer containing a hydroisomerization catalyst while the second reaction zone comprises a second catalyst layer containing a catalytic dewaxing catalyst or preferably containing a mixture of hydroisomerization and catalytic dewaxing catalysts.
- each reaction zone may contain one or more catalyst beds comprising one or more catalysts in order to incorporate interstage quench or liquid redistribution between beds. Catalyst activity for each reaction zone will normally be dependent upon variations in operating conditions.
- hydroisomerization and catalytic dewaxing catalysts which have similar activity for the conversion and cracking of the n- paraffin containing hydrocarbon feeds under analogous operating conditions, i.e., similar or overlapping reaction conditions such as temperature and pressure.
- activity balance may be achieved by varying the degree and concentration of each of the catalysts in a single reactor or the degree and concentration of a catalyst within a particular reaction zone or catalyst bed.
- a dual reactor system may be employed to conduct hydroisomerization and catalytic dewaxing in separate reactors, connected in series, such that the total liquid product of the first reactor flows directly into the reaction zone of the second reactor.
- the preferred reactor conditions, i.e., temperature and pressure for each reactor may depend on the catalysts employed in each reactor.
- hydroisomerization is achieved by reacting the wax containing feed with hydrogen in the presence of a suitable hydoisomerization catalyst. While many catalysts may be satisfactory for this step, some catalysts perform better than others and are preferred.
- a suitable hydoisomerization catalyst comprises one or more Group VIII noble or non- noble metal components, and depending on the reaction conditions, one or more non-noble metals such as Co, Ni and Fe, which may or may not also include Group VIB metal (e.g., Mo, W) oxide promoters, supported on an acidic metal oxide support to give the catalyst both a hydrogenation and dehydrogenation function for activating the hydrocarbons and an acid function for isomerization.
- Group VIB metal e.g., Mo, W
- noble metals reduce hydrogenolysis, particularly at lower temperatures and will therefore be preferred for some applications.
- Preferred noble metals are Pt and Pd.
- the catalyst may also contain a Group IB metal, such as copper, as a hydrogenolysis suppressant.
- the cracking and hydrogenation activity of the catalyst is determined by its specific composition.
- the metal Groups referred to herein are those found in the Sargent- Welch Periodic Table of the Elements, copyright 1968.
- the acidic support for the hydroisomerization catalyst is preferably an amorphous silica-alumina where the silica is present in amounts of less than about 30 wt %, preferably 5-30 wt %, more preferably 10-20 wt %.
- the silica-alumina support may contain amounts of a binder for maintaining catalyst integrity during high temperature, high pressure processes.
- Typical binders include silica, alumina, Group IVA metal oxides, e.g., zirconia, titania, various types of clays, magnesia, etc., and mixtures of the foregoing, preferably alumina, silica, or zirconia, most preferably alumina. Binders, when present in the catalyst composition, make up about 5-50% by weight of the support, preferably 5-35% by weight, more preferably 20-30% by weight.
- Characteristics of the support preferably include surface areas of 200-500 m 2 /gm (BET method), preferably about 250-400 m 2 /gm; and pore volume of less than 1 ml/gm as determined by water adsorption, preferably in the range of about 0.35 to 0.8 m/gm, e.g., 0. 57 ml/gm.
- the metals may be incorporated onto the support by any suitable method, and the incipient wetness technique is preferred. Suitable metal solutions may be used, such as nickel nitrate, copper nitrate or other aqueous soluble salts.
- the metals are co-impregnated onto the support allowing for intimate contact between the Group VIII metal and the Group IB metal, for example, the formation of bimetallic clusters.
- the impregnated support is then dried, e.g., over night at about 100°- 150° C, followed by calcination in air at temperatures ranging from about 200°-550° C, preferably 350°-550° C, so that there is no excessive loss of surface area or pore volume.
- the Group IB metal is usually present in lesser amounts and may range from about a 1:2 to about a 1:20 ratio respecting the Group VIII metal.
- Catalytic dewaxing has as its objective, the removal of a portion of the remaining straight chain n-paraffins which contribute to undesirably high cloud point while minimizing the cracking of the branched chain iso-paraffins formed during hydroisomerization.
- this step removes the n-paraffins by either selectively breaking the n-paraffins into small molecules, lower-boiling liquids or converting some of the remaining n-paraffins to isoparaffins, while leaving the more branched chain iso-paraffins in the process stream.
- Catalytic dewaxing processes commonly employ zeolite dewaxing catalysts with a high degree of shape selectivity so that only linear (or almost liner) paraffins can enter the internal structure of the zeolite where they undergo cracking to effect their removal.
- Some preferred dewaxing catalysts include SAPO-11, SAPO-41, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-57, SSZ-31, SSZ-32, SSZ-41, SSZ- 43 and ferrierite.
- the catalyst(s) contained in the second reaction zone having a catalytic dewaxing functionality may comprise a catalytic dewaxing catalyst, a mixture of a catalytic dewaxing catalyst and a hydroisomerization catalyst or a composite containing a catalytic dewaxing and hydroisomerization catalyst component.
- layered catalyst beds comprising catalytic dewaxing catalyst and/or hydroisomerization catalysts may be employed in the second reaction zone.
- the dewaxing catalyst comprises a composite pellet comprising both a hydroisomerization catalyst and catalytic dewaxing catalyst.
- the dewaxing component of the catalytic dewaxing catalyst comprises a 10-member ring unidirectional, inorganic oxide, molecular sieve having generally oval 1-D pores having a minor axis between about 4.2 A and about 4.8 A and a major axis between about 5.4 A and about 7.0 A as determined by X-ray crystallography.
- the molecular sieve is preferably impregnated with from 0.1 to 5 wt %, more preferably about 0.1 to 3 wt % of at least one Group VIII metal, preferably a noble Group VIII metal, most preferably platinum or palladium.
- the isomerization component of the composite catalyst can be any of the typical isomerization catalysts, such as those comprising a refractory metal oxide support base (e.g., alumina, sinca-alumina, zirconia, titanium, etc.) on which has been deposited a catalytically active metal selected from the group consisting of Group VI B, Group VII B, Group VIII metals and mixtures thereof, preferably Group VIII, more preferably noble Group VIII, most preferably Pt or Pd and optionally including a promoter or dopant such as halogen, phosphorus, boron, yttria, magnesia, etc. preferably halogen, yttria or magnesia, most preferably fluorine.
- a refractory metal oxide support base e.g., alumina, sinca-alumina, zirconia, titanium, etc.
- a catalytically active metal selected from the group consisting of Group VI B, Group VII B, Group VIII metals and mixtures
- the catalytically active metals are present in the range 0.1 to 5 wt %, preferably 0.1 to 3 wt %, more preferably 0.1 to 2 wt %, most preferably 0.1 to 1 wt %.
- the promoters and dopants are used to control the acidity of the isomerization catalyst.
- acidity is imparted to the catalyst by addition of a halogen, preferably fluorine.
- a halogen preferably fluorine
- it is present in an amount in the range 0.1 to 10 wt %, preferably 0.1 to 3 wt %, more preferably 0.1 to 2 wt % most preferably 0.5 to 1.5 wt %.
- acidity can be controlled by adjusting the ratio of silica to alumina or by adding a dopant such as yttria or magnesia which reduces the acidity of the silica-alumina base material as taught in U.S. Pat. No. 5,254,518.
- one or more isomerization catalysts can be pulverized and powdered, and mixed producing the second component of the composite pellet catalyst.
- the composite catalyst can contain the individual powdered components which make it up in a broad ratio.
- the components can be present in the ratio in the range 1:100 or more to 100 or more: 1, preferably 1:3 to 3:1.
- the multi-stage isomerization process was carried out in an isothermal sand bath (2) containing two 0.5 inch up-flow fixed bed reactors, Rl and R2, connected in series where the total liquid product of the first reactor (Rl) was fed directly into the reaction zone of the second reactor (R2).
- Rl contained 80 cc (44.7 gms) of a commercially available hydroisomerization catalyst comprising 0.5 wt% Pd on a silica-alumina support containing nominally 20 wt % alumina/80 wt% silica and 30 wt% alumina binder.
- R2 contained a catalyst blend containing 29 cc (16.2 gms) of a commercially available dewaxing catalyst comprising 0.5 wt% Pt on an extrudate containing Theta-1 zeolite (TON) and 51 cc (27.5 gms) of the hydroisomerization catalyst contained in Rl. The extrudate was crashed and the -8, +20 mesh used to load a portion of the fixed bed reactor. There was no treatment or interstage stripping of the hydroisomerized product of Rl prior to feeding into R2.
- a 300° F+ Fischer-Tropsch derived wax containing feed (4) was run through Rl at conditions that resulted in about 50% conversion of the 700° F+ material to 700° F- and dewaxing was run through R2 to achieve a cloud point below about -35° C.
- the isothermal reactor conditions were as follows: 715 psig, 1650 SCF/Bbl hydrogen treat rate at 0.854 LHSV and a temperature of approximately 606° F.
- Fuel 1 comprised a 280-700° F nominal cut fuel whereas Fuel 2 comprised a 300-700° F nominal cut.
- the process employed in the example showed boiling range product distributions characterized by high selectivity to 300/700° F with low gas and naphtha production.
- Aromatics total % 0 0 27.9 26.7
- the recovered distillate has nil sulfur and nitrogen. Further, the process does not make aromatics and polyaromatics, or as usually operated, virtually no aromatics are produced. Accordingly, the concentration of sulfur, aromatics and polyaromatics for Fuels 1 and 2 were below the detectable limits of the test methods shown in Table 3.
- the tenth percentile minimum temperatures are listed in the ASTM Standard Specification for Diesel Fuel Oils D-975 in Figures X4.l-X4.12. These ambient air temperatures were derived from an analysis of historical hourly temperature readings recorded over a period of 15 to 21 years from 345 weather stations across the United States.
- the tenth percentile minimum ambient air temperature is defined as the lowest ambient air temperature which will not go lower on average more than 10% of the time. In other words, the daily minimum ambient air temperature would, on average, not be expected to go below the monthly tenth percentile minimum ambient air temperature more than three days for a 30 day month.
- the Fischer-Tropsch derived fuels of this invention have cloud points below -35° C, thereby qualifying as a winter diesel fuel.
- the Fischer-Tropsch fuels of the invention were compared with the conventional petroleum fuels.
- the fuels were evaluated with a Peugeot 405 Indirect Injection (IDI) light duty diesel engine.
- Regulated emissions were measured during hot-start transient cycles and emissions of hydrocarbons (HC), carbon monoxide (CO), nitrous oxide (NOx) and particulate matter (PM) were measured.
- HC hydrocarbons
- CO carbon monoxide
- NOx nitrous oxide
- PM particulate matter
- the light duty European test cycle is performed in two parts:
- this urban cycle represents inner city driving conditions after a cold start with a maximum speed of 50 km h
- EUDC the extra-urban driving cycle is typical of suburban and open road driving behavior and includes speeds up to 120 km/h. The data is based on the combined emissions of the ECE and EUDC cycles expressed in g/km. See SAE Papers 961073 and 961068.
- Fuel 4 was used as the reference and therefore run in triplicate; all others were run in duplicate.
- the data represents the average values from the combination of the ECE-EUDC test procedures ("combined ECE-EUDC" reporting method).
- Table 5 details the predicted changes for light duty (i.e., passenger car) diesel engines according to the well recognized European Program on Emissions, Fuels and Engine Technologies (EPEFE) study in Europe undertaken by the government, auto and oil companies to define the relationship between fuel properties and emissions based on variables in density, cetane number and T95.
- the left hand column indicates the two pollutants (particulate matter and nitrogen oxides) along with the changes in absolute emissions in g/Hp-hr and percent change (% increase(positive) or % decrease(negative)) for each of the four fuel characteristics shown at the top of the columns.
- the emission change (in g/Hp- hr and percent) is based on a deviation of one of the four fuel characteristics as shown in parenthesis. For example, if the T95 was lowered by 55° C, the particulate emissions would decrease by 6.9% while the NOx would increase by 4.6%.
- Table 6 was produced by combining the published results of Table 5, with the properties measured in Table 3 and the emissions results of Table 4. The resulting test data indicates the expected change in emissions as projected by the EPEFE equations versus the actual changes measured during emissions testing on each of the fuels listed in Table 3. Again, all results are referenced to Fuel 4 as the base fuel. TABLE 6
- Fuel 3 shows very close agreement with the predictions differing by only a slight amount with particulate emissions 2.4% ( “ 3.9%- " 1.5%) worse than expected and NOx 4.6% (1.2% - “ 4.3%) better than expected.
- the contrast from Fuel 4 is quite different and unexpected.
- the Fischer-Tropsch derived fuels of this invention exceeded the performance predicted for particulate emissions while at the same time dramatically decreasing NOx emissions. According to these projections, an improvement in particulate emissions is expected for Fuels 1 and 2 and the above data not only bears this prediction out but exceeds it.
- the EPEFE predictions also predict a slight increase in NOx.
- the smoke level was below the detectable amount.
Abstract
Description
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Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP01922779A EP1297098A2 (en) | 2000-05-02 | 2001-03-28 | Winter diesel fuel production from a fischer-tropsch wax |
CA2405660A CA2405660C (en) | 2000-05-02 | 2001-03-28 | Winter diesel fuel production from a fischer-tropsch wax |
AU4954301A AU4954301A (en) | 2000-05-02 | 2001-03-28 | Winter diesel fuel production from a fischer-tropsch wax |
JP2001580252A JP2003531948A (en) | 2000-05-02 | 2001-03-28 | Production of winter diesel fuel from Fischer-Tropsch wax |
BR0110424-1A BR0110424A (en) | 2000-05-02 | 2001-03-28 | Process for producing a fuel, fuel, and, Process for producing a fuel useful as a diesel fuel |
KR1020027014624A KR100786420B1 (en) | 2000-05-02 | 2001-03-28 | Winter diesel fuel production from a fischer-tropsch wax |
AU2001249543A AU2001249543B2 (en) | 2000-05-02 | 2001-03-28 | Winter diesel fuel production from a fischer-tropsch wax |
NO20025259A NO20025259L (en) | 2000-05-02 | 2002-11-01 | Winter diesel fuel made from Fischer-Tropsch wax |
AU2005229643A AU2005229643B2 (en) | 2000-05-02 | 2005-10-31 | Winter diesel fuel production from a fischer-tropsch wax |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US09/562,453 | 2000-05-02 | ||
US09/562,453 US6787022B1 (en) | 2000-05-02 | 2000-05-02 | Winter diesel fuel production from a fischer-tropsch wax |
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WO2001083641A2 true WO2001083641A2 (en) | 2001-11-08 |
WO2001083641A3 WO2001083641A3 (en) | 2002-09-06 |
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PCT/US2001/009903 WO2001083641A2 (en) | 2000-05-02 | 2001-03-28 | Winter diesel fuel production from a fischer-tropsch wax |
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US (1) | US6787022B1 (en) |
EP (1) | EP1297098A2 (en) |
JP (1) | JP2003531948A (en) |
KR (1) | KR100786420B1 (en) |
AR (1) | AR029910A1 (en) |
AU (2) | AU2001249543B2 (en) |
BR (1) | BR0110424A (en) |
CA (1) | CA2405660C (en) |
NO (1) | NO20025259L (en) |
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Also Published As
Publication number | Publication date |
---|---|
CA2405660C (en) | 2011-01-04 |
BR0110424A (en) | 2003-02-25 |
JP2003531948A (en) | 2003-10-28 |
TW589367B (en) | 2004-06-01 |
US6787022B1 (en) | 2004-09-07 |
ZA200208205B (en) | 2003-07-24 |
KR20030010613A (en) | 2003-02-05 |
WO2001083641A3 (en) | 2002-09-06 |
CA2405660A1 (en) | 2001-11-08 |
AR029910A1 (en) | 2003-07-23 |
NO20025259L (en) | 2003-01-02 |
AU4954301A (en) | 2001-11-12 |
NO20025259D0 (en) | 2002-11-01 |
KR100786420B1 (en) | 2007-12-17 |
EP1297098A2 (en) | 2003-04-02 |
AU2001249543B2 (en) | 2005-09-29 |
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