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WO2016107860A1 - Procédé pour préparer une cire de paraffine - Google Patents

Procédé pour préparer une cire de paraffine Download PDF

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Publication number
WO2016107860A1
WO2016107860A1 PCT/EP2015/081328 EP2015081328W WO2016107860A1 WO 2016107860 A1 WO2016107860 A1 WO 2016107860A1 EP 2015081328 W EP2015081328 W EP 2015081328W WO 2016107860 A1 WO2016107860 A1 WO 2016107860A1
Authority
WO
WIPO (PCT)
Prior art keywords
fraction
wax
fischer
paraffin wax
congealing point
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2015/081328
Other languages
English (en)
Inventor
Arend Hoek
Antonius Adrianus Maria Roovers
Kaushik MAJUMDER
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Shell USA Inc
Original Assignee
Shell Internationale Research Maatschappij BV
Shell Oil Co
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 Shell Internationale Research Maatschappij BV, Shell Oil Co filed Critical Shell Internationale Research Maatschappij BV
Priority to CN201580071670.5A priority Critical patent/CN107109258A/zh
Priority to US15/542,940 priority patent/US20180002618A1/en
Priority to MYPI2017702307A priority patent/MY192547A/en
Priority to JP2017535343A priority patent/JP2018508600A/ja
Priority to SG11201705115XA priority patent/SG11201705115XA/en
Priority to CN202210121634.7A priority patent/CN114574243A/zh
Priority to EP15817899.6A priority patent/EP3240872A1/fr
Publication of WO2016107860A1 publication Critical patent/WO2016107860A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/36—Recovery of petroleum waxes from other compositions containing oil in minor proportions, from concentrates or from residues; De-oiling, sweating
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L91/00—Compositions of oils, fats or waxes; Compositions of derivatives thereof
    • C08L91/06—Waxes
    • C08L91/08—Mineral waxes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • 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
    • 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/42—Refining of petroleum waxes
    • C10G73/44—Refining of petroleum waxes in the presence of hydrogen or hydrogen-generating compounds
    • 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
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products

Definitions

  • the present invention provides a paraffin wax and a process to prepare said paraffin wax.
  • Paraffin wax may be obtained by various processes.
  • US 2,692,835 discloses a method for deriving paraffin wax from crude oil.
  • paraffin wax may be obtained using the so called Fischer-Tropsch process.
  • An example of such process is disclosed in WO 2002/102941, EP 1 498 469, WO 2004/009739 and WO 2013/064539.
  • WO 2000/11113 discloses a process to prepare
  • Fischer-Tropsch derived wax products by feeding a
  • Fischer-Tropsch derived paraffinic into a distillation column, followed by operating the distillation column to produce wax products, which wax products are withdrawn from the distillation column.
  • a problem of the process disclosed in WO 2000/11113 is that although this process delivers wax products, the wax products are not refined enough to be used in applications such as candles, hot melt adhesives, crayons, packaging, and PVC extrusion lubricants in an advantageous way.
  • an object of the present invention is to provide an efficient method for preparing refined paraffin wax product in a high yield.
  • One of the above or other objects may be achieved according to the present invention by providing a paraffin wax having a congealing point according to ASTM D938 of at least 75°C and a Saybolt colour according to ASTM D156 of at least 25 cm.
  • the paraffin wax is a fully refined wax which may be advantageously used in several wax applications .
  • paraffin wax may be advantageously used in wax applications such as candles, hot melt adhesives, crayons, packaging, and PVC extrusion lubricants.
  • Tropsch derived feed without a preceding hydrogenation step results in paraffin waxes having high Saybolt colours .
  • Tropsch derived waxes is for example described on page 181 in the "Handbook of Commercial Catalysts,
  • Fischer-Tropsch product stream is more stable with respect to product degradation in subsequent distillation steps. Degradation may be caused by exposure to high temperature and by oxygen ingress in vacuum columns .
  • a paraffin wax has a congealing point according to ASTM D938 of at least
  • the paraffin wax comprises primarily n-paraffins.
  • the paraffin wax according to the present invention comprises more than 85 wt . % of n-paraffins, preferably more than 90 wt . % of n-paraffins.
  • Paraffin waxes are known and described for example in US 2,692,835, WO2002/102941, EP 1 498 469 and WO
  • the paraffin wax according to the present invention has a congealing point according to ASTM D938 in the range of from 75 to 85°C.
  • paraffin wax according to the present invention has a congealing point according to ASTM D938 of at least 80°C.
  • paraffin wax according to the present invention has a Saybolt colour according to ASTM D156 of at least 25 cm.
  • the paraffin wax according to the present invention has a Saybolt colour according to ASTM D156 of at least 30 cm.
  • the Saybolt colour scale is used to quantify colour intensity for mildly coloured substances in liquid state.
  • waxes are molten for measurement.
  • the scale runs from ⁇ -16 cm to >30cm. >30 cm means water white. The higher the number the better (i.e. the lesser) the colour.
  • the paraffin wax according to the present invention has preferably an oil content according to ASTM D721 of less than 0.5 wt.%, more preferably less than 0.45 wt . % .
  • paraffin wax according to the present invention is a Fischer-Tropsch derived paraffin wax.
  • Fischer-Tropsch derived paraffin wax is derived from a Fischer-Tropsch process.
  • Fischer-Tropsch product stream is known in the art.
  • Fischer-Tropsch derived is meant a paraffin wax is, or is derived from a Fischer-Tropsch process.
  • a Fischer-Tropsch derived paraffin wax may also be referred to a GTL (Gas-to-
  • the Fischer-Tropsch derived paraffin wax comprises paraffins, primarily n-paraffins.
  • the paraffins primarily n-paraffins.
  • Fischer-Tropsch derived paraffin wax comprises more than 85 wt.% of n-paraffins, preferably more than 90 wt.% of n-paraffins .
  • the present invention provides a process to prepare a Fischer-Tropsch derived paraffin wax, the process at least comprising the following steps: (a) providing a Fischer-Tropsch product stream comprising paraffins having from 10 to 300 carbon atoms;
  • step (c) subjecting the fraction comprising 18 to 300 carbon atoms of step (b) to a hydrogenation step, thereby obtaining a hydrogenated fraction comprising 18 to 300 carbon atoms;
  • step (d) separating the hydrogenated fraction comprising 18 to 300 carbon atoms of step (c) , thereby obtaining one or more first light waxes having a congealing point in the range of 30 to 75°C and a second heavy wax having a congealing point in the range of 75 to 120°C;
  • step (e) separating the heavy wax of step (d) to obtain a distillate wax fraction having a congealing point of at least 75°C, preferably of at least 80°C;
  • step (e) hydrofinishing the distillate wax fraction of step (e) thereby obtaining a hydrofinished distillate wax fraction having a congealing point of at least 75°C, preferably of at least 80°C.
  • step (a) of the process according to the present invention a Fischer-Tropsch product stream comprising paraffins having from 10 to 300 carbon atoms is provided.
  • a Fischer-Tropsch product stream comprising paraffins having from 10 to 300 carbon atoms is meant 10 to 300 carbon atoms per molecule.
  • the Fischer-Tropsch product stream as provided in step (a) is derived from a Fischer-Tropsch process.
  • Fischer-Tropsch product stream is known in the art.
  • Fischer-Tropsch product is meant a synthesis product of a Fischer-Tropsch process.
  • Synthesis gas or syngas is a mixture of hydrogen and carbon monoxide that is obtained by conversion of a hydrocarbonaceous feedstock.
  • Suitable feedstock include natural gas, crude oil, heavy oil fractions, coal, biomass and lignite.
  • a Fischer-Tropsch product derived from a hydrocarbonaceaous feedstock which is normally in the gas phase may also be referred to a GTL (Gas-to- Liquids) product.
  • GTL Gas-to- Liquids
  • the product stream of the Fischer-Tropsch process is usually separated into a water stream, a gaseous stream comprising unconverted synthesis gas, carbon dioxide, inert gasses and CI to C3, and a C4+ stream.
  • the full Fischer-Tropsch hydrocarbonaceous product suitably comprises a CI to C300 fraction.
  • Fischer-Tropsch product which suitably comprises C3 to C9 fraction are separated from the Fischer-Tropsch product by distillation thereby obtaining a Fischer-Tropsch product stream, which suitably comprises CIO to C300 fraction.
  • the weight ratio of compounds having at least 60 or more carbon atoms and compounds having at least 30 carbon atoms in the Fischer-Tropsch product is preferably at least 0.2, more preferably 0.3.
  • the weight ratio in the Fischer-Tropsch product may lead to Fischer-Tropsch derived paraffin waxes having a low oil content .
  • step (b) of the process according to the present invention the Fischer-Tropsch product stream of step (a) is separated to obtain at least a fraction comprising 10 to 17 carbon atoms and a fraction comprising 18 to 300 carbon atoms .
  • the separation is preferably performed by means of a distillation at atmospheric or slightly below atmospheric pressure conditions. It is preferred that the
  • step (c) of the process according to the present invention the fraction comprising 18 to 300 carbon atoms of step (b) is subjected to a hydrogenation step, thereby obtaining a hydrogenated fraction comprising 18 to 300 carbon atoms.
  • the hydrogenation is suitably carried out at a temperature between 200 and 275°C and at a pressure between 20 and 70 bar.
  • step (d) of the process according to the present invention the hydrogenated fraction comprising 18 to 300 carbon atoms of step (c) is separated to obtain one or more first light waxes having a congealing point in the range of 30 to 75 °C and a second heavy wax having a congealing point in the range of 75 to 120°C.
  • light wax wax having a congealing point in the range of from 30 to 75°C.
  • heavy wax wax having a congealing point in the range of from 75 to 120°C.
  • the hydrogenated fraction comprising 18 to 300 carbon atoms of step (c) is separated by vacuum distillation at a pressure between 5 and 20 mbar, preferably between 5 and 15 mbar, and more preferably between 10 and 15 mbar. Also the distillation is
  • the first light one or more waxes are obtained as distillate and/or side cuts in vacuum distillation, e.g. a first light wax fraction having a congealing point in the range of from 30 to 35°C, a second light wax fraction having a congealing point in the range of from 50 to 60°C, and a third light wax fraction having a congealing point in the range of from 65 to 75°C.
  • the first light wax fraction is obtained as top cut of the vacuum distillation
  • the second light wax fraction is obtained as a side cut of the vacuum distillation
  • the third light wax fraction is obtained as heavier side cut of the vacuum distillation.
  • one or more light wax fractions having a congealing point in the range of from 30 to 75°C of step (d) are hydrofinished thereby obtaining one or more hydrofinished wax fractions having a congealing point in the range of from 30 to 75°C.
  • a wax fraction having a congealing point in the range 30 to 75°C is hydrofinished thereby obtaining a hydrofinished wax fraction having a congealing point in the range of from
  • the first and second light wax fractions are hydrofinished thereby obtaining a first light hydrofinished wax fraction having a congealing point in the range of from 30 to 35°C, and a second light
  • hydrofinished wax fraction having a congealing point in the range of from 50 to 60°C.
  • At least the third light wax i.e. the heaviest side cut of the vacuum distillation step is hydrofinished thereby obtaining a hydrofinished wax fraction having a congealing point in the range of 65-
  • step (e) of the process according to the present invention the heavy wax of step (d) is separated thereby obtaining distillate wax having a congealing point of at least 75°C, preferably of at least 80°C.
  • the second heavy wax of step (d) is separated, thereby obtaining at least one distillate wax fraction having a congealing point in the range of from
  • step (d) is separated, thereby obtaining at least one distillate wax fraction having a congealing point in the range of from
  • 70 to 90°C preferably 70 to 85°C and more preferably 75 to 85°C.
  • step (f) of the process according to the present invention the distillate fraction of step (e) is hydrofinished thereby obtaining a hydrofinished
  • distillate wax having a congealing point of at least 75°C, more preferably of at least 80°C.
  • the heavy distillate wax fraction having a congealing point in the range of from 75 to 85°C is hydrofinished thereby obtaining a hydrofinished heavy distillate wax fraction having a congealing point in the range of from 75 to 85°C.
  • the heavy distillate wax fraction having a congealing point in the range of from 70 to 90°C, preferably in the range of from 70 to 85°C and more preferably in the range of from 75 to 85°C are
  • the heavy residual wax fraction having a congealing point in the range of from 95 to 120°C is hydrofinished thereby obtaining a hydrofinished heavy residual wax fraction having a congealing point in the range of from 95 to 120°C.
  • the heavy second wax of step (e) is preferably separated by short path distillation at a pressure between 0.05 and 0.5 mbar, and more preferably between 0.1 and 0.3 mbar.
  • the distillation is preferably carried out at a temperature of from 200 to 350°C and more preferably from 250 to 300°C.
  • the distillate wax fraction having a congealing point of at least 75°C, preferably of at least 80°C is obtained as the distillate fraction of the short path distillation.
  • distillate is meant a fraction obtained with distillation which is a top cut or side cut but not a residual bottom fraction.
  • Short path distillation also known as molecular distillation is known in the art and therefore not described here in detail.
  • An example of a form of short path distillation is a Wiped Film Evaporator. Typical short path distillations are for example described in Chapter 9.1 in "Distillation, operations and
  • Figure 1 schematically shows a process scheme of the process scheme of a preferred embodiment of the process according to the present invention.
  • a Fischer- Tropsch product stream is obtained (not shown) .
  • This product is separated in a distillation column 2 into a fraction 10 comprising 10 to 17 carbon atoms and a fraction 20 comprising 18 to 300 carbon atoms.
  • Fraction 20 is fed to a hydrogenation reactor 3 wherein fraction 20 is converted to a hydrogenated fraction 30.
  • Fraction 30 is distilled in a vacuum distillation column 4 to recover one or more wax fractions 40 having a congealing point in the range of from 30 to 75°C and a heavy fraction 50.
  • Fractions 40 is fed to a hydrofinishing reactor 5 wherein fractions 40 is converted to
  • hydrofinished fractions 60 having a congealing point in the range of from 30 to 75°C.
  • Heavy wax 50 is distilled in a short path
  • distillation column 6 to recover a distillate wax fraction 70 having a congealing point of at least 80°C.
  • Fraction 70 is fed to a hydrofinishing reactor 7 wherein fraction 70 is converted to a hydrofinished fraction 80 having a congealing point of at least 80°C.
  • fraction 10 is fed to a hydrogenation reactor 8 wherein fraction 10 is converted to a hydrogenated fraction 90 comprising 10 to 17 carbon atoms.
  • Fischer-Tropsch derived paraffin wax fractions having a congealing point of at least 80 °C were obtained using a Fischer-Tropsch process.
  • a Fischer-Tropsch effluent was prepared according to the method described in US6858127. Based on C1+ hydrocarbons the effluent had a C30+ content of 51.1 %m and a C60+ content of 28.5 %m.
  • the effluent was separated in a fraction A which is in the gas phase at ambient conditions and a fraction B which is in the liquid or solid phase at ambient conditions.
  • care was taken to avoid temperatures above 370°C for any part of the distillation equipment in contact with hydrocarbons and to avoid contact of hydrocarbons with oxygen. All distillations described below were carried out in a continuous mode.
  • Fraction B was subjected to a distillation at atmospheric pressure yielding a top stream comprising a fraction containing molecules with 9 or less carbon atoms, a side cut C containing molecules with 10 to 17 carbons atoms and a bottom stream D containing molecules with 18 to 300 carbon atoms.
  • the effective outpoint for the separation between streams C and D was 310°C.
  • Fraction F consists of hydrogenated normal paraffins in the CIO to C17 range.
  • the residue of the atmospheric distillation (fraction D) was subjected hydrogenated over a nickel catalyst as described in WO 2007/082589 (Catalyst G) .
  • Process conditions were: a weight hourly space velocity (WHSV) of 1.0 kg/l/h, 30 bar of pure hydrogen at reactor inlet, a hydrogen over feedstock ratio of 1000 Nl/kg and a temperature of 220°C.
  • WHSV weight hourly space velocity
  • Fraction H consists of hydrogenated normal paraffins in the C18 to C300 range.
  • Fraction H is subjected to a vacuum distillation.
  • the distillation was run at a bottom temperature of 320°C and a pressure of 15 mbar.
  • the effective outpoint between bottom stream and heaviest distillate was 490°C.
  • Several refined waxes were obtained as distillates of which the heaviest was subjected to a hydrofinishing operation over a nickel catalyst as described in WO 2007/082589 (Catalyst G) .
  • Process conditions were: a weight hourly space velocity (WHSV) of 1.0 kg/l/h, 60 bar of pure hydrogen at reactor inlet, a hydrogen over feedstock ratio of 1000 Nl/kg and a temperature of 240°C.
  • WHSV weight hourly space velocity
  • fraction J The residue of this vacuum distillation (fraction J) is subjected to a short path distillation with an effective cut point of 540°C. The distillation was run at 0.2 mbar and 260°C .
  • distillate of the short path distillation (fraction K) is subjected to a hydrofinishing operation over a nickel catalyst as described in WO 2007/082589
  • WHSV weight hourly space velocity
  • the product was separated in a fraction L which is in the gas phase at ambient conditions and a fraction M which is in the solid phase at ambient conditions.
  • Fraction M is obtained as a refined wax with a congealing point of about 80°C
  • the yield of fraction M was 6.8 %m of the Fischer-Tropsch effluent on a hydrocarbon basis.
  • Fraction M is the desired heavy Fischer-Tropsch based distillate hard wax. Properties of fraction M can be found in Table 1.
  • the Saybolt colour scale is used to quantify colour intensity for mildly coloured substances in liquid state.
  • waxes are molten for measurement.
  • the scale runs from ⁇ -16 cm to >30cm.
  • >30 cm means water white. The higher the number the better (i.e. the lesser) the colour.
  • Table 1 show that starting from a hydrogenated Fischer-Tropsch effluent having C30+ content of 51.1%m and a C60+ content of 28.5 %m a Fischer-Tropsch derived paraffin wax having a congealing point of about 80°C was obtained. Furthermore, the paraffin wax has a low oil content and a high Saybolt colour.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne une cire de paraffine présentant un point de congélation, selon la norme ASTM D938, d'au moins 75°C, et une couleur Saybolt, selon la norme ASTM D156, d'au moins 25 cm.
PCT/EP2015/081328 2014-12-31 2015-12-29 Procédé pour préparer une cire de paraffine Ceased WO2016107860A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
CN201580071670.5A CN107109258A (zh) 2014-12-31 2015-12-29 制备石蜡的方法
US15/542,940 US20180002618A1 (en) 2014-12-31 2015-12-29 Process to prepare paraffin wax
MYPI2017702307A MY192547A (en) 2014-12-31 2015-12-29 Process to prepare a paraffin wax
JP2017535343A JP2018508600A (ja) 2014-12-31 2015-12-29 パラフィンワックスを調製する方法
SG11201705115XA SG11201705115XA (en) 2014-12-31 2015-12-29 Process to prepare a paraffin wax
CN202210121634.7A CN114574243A (zh) 2014-12-31 2015-12-29 制备石蜡的方法
EP15817899.6A EP3240872A1 (fr) 2014-12-31 2015-12-29 Procédé pour préparer une cire de paraffine

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP14200715.2 2014-12-31
EP14200715 2014-12-31

Publications (1)

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WO2016107860A1 true WO2016107860A1 (fr) 2016-07-07

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PCT/EP2015/081328 Ceased WO2016107860A1 (fr) 2014-12-31 2015-12-29 Procédé pour préparer une cire de paraffine

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US (1) US20180002618A1 (fr)
EP (1) EP3240872A1 (fr)
JP (1) JP2018508600A (fr)
CN (2) CN114574243A (fr)
MY (1) MY192547A (fr)
SG (2) SG11201705115XA (fr)
WO (1) WO2016107860A1 (fr)

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CN109988548B (zh) * 2017-12-29 2020-10-02 内蒙古伊泰煤基新材料研究院有限公司 高温相变蜡及其制备方法
CN111205891A (zh) * 2018-11-21 2020-05-29 内蒙古伊泰煤基新材料研究院有限公司 一种塑料加工用蜡及其制备方法

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SG10201907003PA (en) 2019-09-27
MY192547A (en) 2022-08-27
SG11201705115XA (en) 2017-07-28
CN107109258A (zh) 2017-08-29
US20180002618A1 (en) 2018-01-04
EP3240872A1 (fr) 2017-11-08
CN114574243A (zh) 2022-06-03

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