WO2000020535A1 - Procede de production de distillats moyens et distillats moyens produits par ce procede - Google Patents

Procede de production de distillats moyens et distillats moyens produits par ce procede Download PDF

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Publication number
WO2000020535A1
WO2000020535A1 PCT/ZA1999/000096 ZA9900096W WO0020535A1 WO 2000020535 A1 WO2000020535 A1 WO 2000020535A1 ZA 9900096 W ZA9900096 W ZA 9900096W WO 0020535 A1 WO0020535 A1 WO 0020535A1
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WO
WIPO (PCT)
Prior art keywords
middle distillate
fraction
isoparaffins
synthetic middle
synthetic
Prior art date
Application number
PCT/ZA1999/000096
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English (en)
Inventor
Robert De Haan
Luis Pablo Dancuart
Mark Jan Prins
Ewald Watermeyer De Wet
Original Assignee
Sasol Technology (Pty) Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sasol Technology (Pty) Ltd filed Critical Sasol Technology (Pty) Ltd
Priority to AU63001/99A priority Critical patent/AU765274B2/en
Priority to EP99950311A priority patent/EP1129155A1/fr
Priority to JP2000574637A priority patent/JP3824490B2/ja
Priority to US09/787,668 priority patent/US7217852B1/en
Publication of WO2000020535A1 publication Critical patent/WO2000020535A1/fr
Priority to US10/712,169 priority patent/US7294253B2/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition

Definitions

  • This invention relates to middle distillates having good cold flow properties, such as the Cold Filter Plugging Point (CFPP) measured in accordance with the IP method 309, and a high Cetane number, as well as to a process for production of such distillates. More particularly, this invention relates to middle distillates produced from a mainly paraffinic synthetic crude which is produced by the reaction of CO and H 2 , typically by the Fischer-Tropsch (FT) process.
  • CFPP Cold Filter Plugging Point
  • Waxy products of a FT hydrocarbon synthesis process particularly the products of a cobalt and/or iron based catalytic process, contain a high proportion of normal paraffins.
  • Primary FT products provide notoriously poor cold flow properties, making such products difficult to use where cold flow properties are vital, e.g. diesel fuels, lube oil bases and jet fuel.
  • cold flow properties of a middle distillate such as jet fuel
  • Hydrocracking produces smaller amounts of gases and light products, which reduce the yield of valuable distillates.
  • the middle distillate fuel described in this invention is produced from a highly paraffinic synthetic crude (syncrude) obtained from synthesis gas (syngas) through a reaction like the FT reaction.
  • the FT primary products cover a broad range of hydrocarbons from methane to species with molecular masses above 1400; including mainly paraffinic hydrocarbons and much smaller quantities of other species such as olefins, and oxygenates.
  • a process for the production of a middle distillate or distillate blend such as diesel, having a high Cetane number as well as good cold flow properties.
  • the synthetic middle distillate cut may comprise more than 50% isoparaffins. wherein the isoparaffins are predominantly methyl and/or ethyl and/or propyl branched.
  • the gradient of an isoparaffins to n-paraffins mass ratio profile of the synthetic middle distillate cut may increase from about 1: 1 for C s to 8.54: 1 for C 1 5 and decrease again to about 3: 1 for C ]8 .
  • a fraction of the synthetic middle distillate cut in the Cjo to Cj 8 carbon number range has a higher ratio of isoparaffins to n-paraffins than a Cs to Co fraction of the synthetic middle distillate cut.
  • the isoparaffins to n-paraffins mass ratio of the do to C 18 fraction may be between 1: 1 and 9: 1.
  • the isoparaffins to n-paraffins mass ratio may be 8.54:1 for a C 1 5 fraction of the synthetic middle distillate cut.
  • a Cjo to C 2 fraction of the middle distillate cut may have a narrow mass ratio range of isoparaffins to n-paraffins of between 3.3: 1 and 5: 1, generally between 4: 1 and 4.9: 1.
  • the mass ratio of isoparaffins to n-paraffins may be adjusted by controlling the blend ratio of hydrocracked to straight run components of the synthetic middle distillate cut.
  • the isoparaffins to n-paraffins mass ratio of the do to 8 fraction having 30% straight run component may be between 1 : 1 and 2:5: 1.
  • the isoparaffins to n-paraffins mass ratio of the do to d s fraction having 20% straight run component mav be between 1.5: 1 and 3:5: 1.
  • the isoparaffins to n-paraffins mass ratio of the Cio to Cj S fraction having 10% straight run component may be between 2 3 1 and 4 3 1
  • the isoparaffins to n-paraffins mass ratio of the do to Cj g fraction having substantially only a hydrocracked component may be between 4 1 and 9 1
  • At least some of the isoparaffins may be methyl branched At least some of the isoparaffins may be dimethyl branched At least 30% (mass) of the isoparaffins are typically mono-methyl branched
  • isoparaffins may however be ethyl branched
  • a synthetic middle distillate cut having a Cetane number above 70 and a CFPP. in accordance with IP 309. of below -20°C. said distillate having an isoparaffinic content substantially as described above
  • the synthetic middle distillate cut is a FT product
  • the invention extends to a diesel fuel composition including from 10% to 100% of a middle distillate cut as desc ⁇ bed above
  • the diesel fuel composition may include from 0 to 90% of one or more other diesel fuel
  • the diesel fuel composition may include at least 20% of the middle distillate cut, the composition having a Cetane number greater than 47 and a CFPP, in accordance with IP 309, below -22°C
  • the diesel fuel composition may include at least 30% of the middle distillate cut. the composition having a Cetane number greater than 50 and a CFPP, in accordance with IP 309, below -22°C
  • the diesel fuel composition may mlcude at least 50% of the middle distillate cut, the composition having a Cetane number greater than 52 and a CFPP, in accordance with IP 309, below -25°C
  • the diesel fuel composition may include at least 70% of the middle distillate cut, the composition having a Cetane number greater than 60 and a cold flow plug point, in accordance with IP 309, below -30°C
  • the diesel fuel composition may further include from 0 to 10% additives
  • the additives may include a lubricity improver
  • the lubricity improver may comprise from 0 to 0 5% of the composition, typically from 0 00001% to 0 05% of the composition In some embodiments, the lubricity improver comp ⁇ ses from 0 008% to 0 02% of the composition
  • the diesel fuel composition may include, as the other diesel, a crude oil derived diesel, such as US 2-D grade (low sulphur No 2-D grade for diesel fuel oil as specified in ASTM D 975-94) and/or CARB (California Air Resources Board 1993 specification) diesel fuel
  • a process for producing a synthetic middle distillate having a Cetane number higher than 70 including (a) separating the products obtained from synthesis gas via the FT synthesis reaction into one or more heavier fraction and one or more lighter fraction, (b) catalytically processing the heavier fraction under conditions which yield mainly middle distillates,
  • step (c) separatmg the middle distillate product of step (b) from a light product fraction and a heavier product fraction which are also produced in step (b), and
  • step (d) blending the middle distillate fraction obtained in step (c) with at least a portion of the one or more lighter fraction of step (a), or products thereof
  • step (b) may be a hydroprocessing step, for example, hydrocracking
  • the process for producing a synthetic middle distillate may include one or more additional step of fractionating at least some of the one or more lighter fraction of step (a), or products thereof, p ⁇ or to step (d)
  • the process for producing a synthetic middle distillate may mclude the additional step of hydrotreatmg at least some of the one or more light fraction of step (a), or products thereof, p ⁇ or to step (d)
  • the one or more heavier fraction of step (a) may have a boiling point above about 270°C. however, it may be above 300°C
  • the one or more lighter fraction may have a boiling point in the range C 5 to the boiling point of the heavier fraction, typically in the range 160°C to 270°C
  • step (d) may boil in the range 100°C to 400°C
  • the product of step (d) may boil in the range 160°C to 370°C
  • the product of step (d) may be a diesel fuel
  • the product of step (d) may have a CFPP below -20°C. typically below -30°C. and even below -
  • the product of step (d) may be obtained by mixing the middle distillate fraction obtained in step (c) with at least a portion of the one or more lighter fraction of step (a), or products thereof, m a volume ratio of between 1 1 and 9 1, typically 2 1 and 6 1, and in one embodiment, in a volume ratio of 84 16
  • the invention extends further to a process for the production of middle distillate fuels from FT pnmary products, comprising predominantly long chain linear paraffins
  • the waxy product from the FT process is separated into at least two fractions, a heavier and at least one lighter fraction
  • the lighter fraction may be subjected to mild catalytic hydrogenation to remove hetero-atomic compounds such as oxygen and to saturate olefins, thereby producing matenal useful as naphtha, solvents, diesel and/or blending components therefor
  • the heavier fraction may be catalytically hydroprocessed without p ⁇ or hydrotreatmg to produce products with good cold flow characteristics
  • This hydroprocessed heavier fraction could be blended with all or part of the hydrogenated and/or unhydrogenated light fraction to obtain, after fractionation, naphtha and a diesel fuel characterised by a high Cetane number
  • the catalysts suitable for the hydroprocessmg steps are commercially available and can be selected towards an improved quality of the desired final product
  • This invention desc ⁇ bes the conversion of primary FT products mto naphtha and middle distillates, for example, diesel having a high Cetane number in excess of 70, while also having good cold flow properties, as described above
  • the FT process is used indust ⁇ ally to convert synthesis gas, derived from coal, natural gas, biomass or heavy oil streams, mto hydrocarbons ranging from methane to species with molecular masses above 1400
  • Preferred reactors for the production of heavier hydrocarbons are slurry bed or tubular fixed bed reactors, while operating conditions are preferably in the range of 160°C - 280°C. in some cases 210- 260°C. and 18 - 50 Bar, in some cases 20-30 bar
  • FT products can be converted into a range of final products, such as middle distillates, gasoline, solvents, lube oil bases, etc
  • Such conversion which usually consists of a range of processes such as hydrocracking, hydrotreatment and distillation, can be termed a FT work-up process
  • the FT work-up process of this invention uses a feed stream consisting of C 5 and higher hydrocarbons derived from a FT process This feed is separated mto at least two individual fractions, a heavier and at least one lighter fraction The cut point between the two fractions is preferably less than 300°C and typically around 270°C
  • the >270°C fraction also referred to as wax, contains a considerable amount of hydrocarbon material, which boils higher than the normal diesel range. If we consider a typical diesel boiling range of 160- 370°C, it means that all material heavier than 370°C needs to be converted into lighter materials by means of a catalytic process often refe ⁇ ed to as hydroprocessing, for example, hydrocracking. Catalysts for this step are of the bifunctional type; i.e. they contain sites active for cracking and for hydrogenation. Catalytic metals active for hydrogenation include group VIII noble metals, such as platinum or palladium, or a sulphided Group VIII base metals, e.g.
  • nickel, cobalt which may or may not include a sulphided Group NI metal, e.g. molybdenum.
  • the support for the metals can be any refractory oxide, such as silica, alumina, titania, zirconia, vanadia and other Group III, IN, NA and VI oxides, alone or in combination with other refractory oxides.
  • the support can partly or totally consist of zeolite.
  • the preferred support is amorphous silica- alumina.
  • Process conditions for hydrocracking can be varied over a wide range and are usually laboriously chosen after extensive experimentation to optimize the yield of middle distillates. In this regard, it is important to note that, as in many chemical reactions, there is a trade-off between conversion and selectivity. A very high conversion will result in a high yield of gases and low yield of distillate fuels. It is therefore important to painstakingly tune the process conditions in order to limit the conversion of >370°C hydrocarbons. Table 2 gives a list of the preferred conditions. Table 2: Process conditions for hydrocracking
  • hydrotreating is a well-known industrial process, catalyzed by any catalyst having a hydrogenation function, e.g. Group VIII noble metal or sulphided base metal or Group VI metals, or combinations thereof.
  • Preferred supports are alumina and silica.
  • Table 3 gives typical operating conditions for the hydrotreating process.
  • hydrotreated fraction may be fractionated into paraffinic materials useful as solvents
  • the applicant has now surprisingly found that the hydrotreated fraction may be directly blended with the products obtained from hydrocracking the wax.
  • hydroisomerise the material contained in the condensate stream
  • isomerisation leads to the formation of branched isomers, which leads to Cetane ratings less than that of the co ⁇ esponding normal paraffins.
  • Important parameters for a FT work-up process are maximization of product yield, product quality and cost. While the proposed process scheme is simple and therefore cost-effective, it produces High Performance Diesel, having a Cetane number >70, and naphtha in good yield. In fact, the process of this invention is able to produce a diesel of hitherto unmatched quality, which is characterized by a unique combination of both high Cetane number and excellent cold flow properties. This is believed to be related to a low degree of isomerisation in the 160-270°C fraction of the diesel and contrary to this, a high degree of isomerisation in the 270-370°C fraction of the diesel.
  • the total amount of isomers in the light boiling range of the diesel (160-270°C fraction) and the heavier range of the diesel (270°C-370°C) are shown in the following table 4.
  • the relatively high percentage of normal paraffins in the light boiling range contributes to the high Cetane number of the diesel fuel, without affecting the cold flow properties.
  • branching is of utmost importance because the linear hydrocarbons in this range provide very poor cold flow properties and in some cases, may even crystallize. Therefore, the amount of iso-paraffins in this range is maximised during hydroprocessing under the process conditions described herein.
  • the basic process is outlined m the attached Figure 1
  • the synthesis gas (syngas), a mixture of Hydrogen and Carbon monoxide, enters the FT reactor 1 where the synthesis gas is converted to hydrocarbons by the FT reaction
  • a lighter FT fraction is recovered in line 7, and may or may not pass through fractionator 2 and hydrotreater 3
  • the product 9 from the hydrotreater may be separated in fractionator 4 or, alternatively, mixed ith hydrocracker products 16 sent to a common fractionator 6
  • a waxy FT fraction is recovered in line 13 and sent to hydrocracker 5 If fractionation 2 is considered the bottoms cut 12 are be sent to hydrocracker 5
  • the products 16, on their own or mixed with the lighter fraction 9a. are separated in fractionator 6
  • a light product fraction, naphtha 19 is obtained from fractionator 6 or by blending equivalent fractions 10 and 17. This is a C 5 -160°C fraction useful as naphtha.
  • a somewhat heavier cut, synthetic diesel 20 is obtainable in a similar way from fractionator 6 or by blending equivalent fractions 11 and 18. This cut is recovered as a 160-370°C fraction useful as diesel.
  • the heavy unconverted material 21 from fractionator 6 is recycled to extinction to hydrocracker 5.
  • the residue may be used for production of synthetic lube oil bases.
  • a small amount of Cj-C gases are also separated in fractionator 6.
  • a commercially available hydrocracking catalyst was used for hydrocracking of a non-hydrotreated FT hydrocarbon fraction with an initial boiling point of about 280°C.
  • the active metals on the catalyst comprised cobalt and molybdenum, while the support was amorphous silica-alumina.
  • Operating conditions were temperatures between 375 and 385°C, pressure of 70 bar and hydrogen flow rate of 1500 m 3 n /m 3 feed.
  • the experiment was carried out in a pilot plant reactor. The conversion of >370°C material to lighter material ranged between 65 and 80%. Diesel component A is obtained after fractionation of the reactor products. The properties of this diesel component are given in table 1.
  • the active metals on the catalyst comprised molybdenum and cobalt, while the support was alumina.
  • the process conditions were temperatures around 250°C, pressure of 68 bar and hydrogen flow rate of 1070 mVm 3 feed.
  • the test was carried in a commercial scale fixed bed reactor. Diesel components B and C were obtained after fractionation of respectively the reactor feed and reactor product. The properties of these diesel components are given in table 6. Table 6: Diesel Blending Components
  • Blend I The diesel fraction obtained from hydrocracking a heavy FT material (component A) was blended with a hydrogenated lighter FT material (component B) in a volume ratio of 84: 16.
  • the properties of the final blend, called Blend I, are given in table 7.
  • Blend I may be used on its own. but also as a blending feedstock.
  • Blend II The diesel fraction obtained from hydrocracking a heavy FT material (component A) was directly blended with a lighter non-hydrogenated FT material (component C) in a volume ratio of 84: 16.
  • the properties of the final blend, called Blend II. are given in table 7 Similar to example 3, Blend II may be used on its own, but also as a blending feedstock. In addition to a high Cetane numbers, above 70, and excellent cold flow properties, with CFPP substantially better than -20°C. Blend II contains alcohols and smaller quantities of other oxygenates, the level of which depend on the blending ratio used to prepare the blend.
  • the diesel Blend I of Example 3 was blended with US 2-D grade diesel having desired Cetane number and CFPP properties, as shown in Table 8 and charts 1 and 2 below, were obtained.
  • Chart 2 Cetane Number of Applicants Diesel and Blends Thereof.

Abstract

Cette invention concerne des distillats moyens ayant de bonnes propriétés d'écoulement à froid telles que la température limite de filtrabilité des gas-oil (TLF) mesurée selon la méthode 309IP, et un indice de cétane élevé, de même qu'un procédé de production de ces distillats. Plus particulièrement, cette invention concerne des distillats moyens produits à partir d'un pétrole de synthèse essentiellement paraffinique lequel est produit par la réaction de CO et de H2 typiquement selon le procédé Fischer-Tropsch (FT). Les distillats moyens de l'invention sont essentiellement isoparaffiniques, les isoparaffines étant ramifiées méthyle, éthyle et/ou propyle. L'invention concerne également une composition de carburant diesel contenant les distillats moyens de l'invention. L'invention concerne également un procédé de préparation des distillats moyens.
PCT/ZA1999/000096 1998-10-05 1999-09-17 Procede de production de distillats moyens et distillats moyens produits par ce procede WO2000020535A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU63001/99A AU765274B2 (en) 1998-10-05 1999-09-17 Process for producing middle distillates and middle distillates produced by that process
EP99950311A EP1129155A1 (fr) 1998-10-05 1999-09-17 Procede de production de distillats moyens et distillats moyens produits par ce procede
JP2000574637A JP3824490B2 (ja) 1998-10-05 1999-09-17 合成中間留出物留分
US09/787,668 US7217852B1 (en) 1998-10-05 1999-09-17 Process for producing middle distillates and middle distillates produced by that process
US10/712,169 US7294253B2 (en) 1998-10-05 2003-11-12 Process for producing middle distillates

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
ZA989038 1998-10-05
ZA98/9038 1998-10-05
US20976298A 1998-12-11 1998-12-11
US09/209,762 1998-12-11

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US09/787,668 A-371-Of-International US7217852B1 (en) 1998-10-05 1999-09-17 Process for producing middle distillates and middle distillates produced by that process
US10/712,169 Division US7294253B2 (en) 1998-10-05 2003-11-12 Process for producing middle distillates

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EP (1) EP1129155A1 (fr)
JP (2) JP3824490B2 (fr)
AU (1) AU765274B2 (fr)
MY (1) MY125273A (fr)
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JP2002526637A (ja) 2002-08-20
JP4261552B2 (ja) 2009-04-30
EP1129155A1 (fr) 2001-09-05
JP2006161056A (ja) 2006-06-22
MY125273A (en) 2006-07-31
AU765274B2 (en) 2003-09-11
JP3824490B2 (ja) 2006-09-20
AU6300199A (en) 2000-04-26

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