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WO1999037737A1 - Traitement des cires - Google Patents

Traitement des cires Download PDF

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Publication number
WO1999037737A1
WO1999037737A1 PCT/EP1999/000293 EP9900293W WO9937737A1 WO 1999037737 A1 WO1999037737 A1 WO 1999037737A1 EP 9900293 W EP9900293 W EP 9900293W WO 9937737 A1 WO9937737 A1 WO 9937737A1
Authority
WO
WIPO (PCT)
Prior art keywords
wax
cracking
feed
lighter
stage
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/EP1999/000293
Other languages
English (en)
Inventor
Christopher Marland
Anthony John Olivier
Pravasivan Sathanathan Padayachee
Ashwin Ramduth
Josias Willem Van Der Merwe
Godlieb Gerhardus Swiegers
James Christiaan Meyer
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.)
Schuemann Sasol GmbH and Co KG
Schumann Sasol South Africa Pty Ltd
Original Assignee
Schuemann Sasol GmbH and Co KG
Schumann Sasol South Africa 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 Schuemann Sasol GmbH and Co KG, Schumann Sasol South Africa Pty Ltd filed Critical Schuemann Sasol GmbH and Co KG
Priority to AU26191/99A priority Critical patent/AU2619199A/en
Publication of WO1999037737A1 publication Critical patent/WO1999037737A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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

Definitions

  • THIS INVENTION relates to the treatment of waxes. It relates in particular to a process for treating a wax, and to a wax when produced by the process.
  • a process for treating a wax which process includes thermally cracking, in a cracking stage, a feed wax having a congealing point X °C, to produce, as a primary product, a lighter wax having a congealing point Y°C, where X > Y.
  • primary product is meant that the lighter wax forms at least 52% m/m of the product produced by the cracking of the feed wax.
  • the feed wax may be a hard wax of which the congealing point, X, may be above 60°C.
  • the congealing point, X, of the hard wax is above 90°C.
  • the feed wax may be a Fischer-Tropsch derived hard wax.
  • Fischer-Tropsch derived in relation to the hard wax is meant a wax fraction or cut obtained by subjecting a synthesis gas comprising mainly carbon monoxide and hydrogen to a low temperature 2
  • Fischer-Tropsch derived hard wax comprises mostly normal paraffins, most of which have a carbon number greater than 1 8, i.e. greater than C 18 , and some isomers, olefins and lighter components. Generally, the individual components of the wax have a large spread of carbon numbers and thus a large spread of boiling points.
  • the Fischer-Tropsch derived hard wax may be a product of a low temperature Fischer-Tropsch synthesis process, using either a slurry bed reactor or a fixed bed reactor.
  • a significant portion of the hard wax e.g . at least about 95% m/m, may comprise hydrocarbons of C 32 and heavier and may consist predominantly of normal paraffins, but may also include isomers and olefins.
  • the process may include pre-treating the feed wax, and in particular the Fischer-Tropsch derived hard wax to remove a lighter fraction, prior to cracking the feed wax in the cracking stage.
  • the hard wax may thus be a wax produced by the Fischer-Tropsch synthesis process, from which a lighter fraction has been removed. Removal of the lighter fraction may be by any suitable method known to a person skilled in the art.
  • At least a portion of the feed wax may be hydrogenated prior to cracking it. Hydrogenation may be effected by contacting the feed wax with hydrogen in the presence of a suitable catalyst at an elevated temperature and an elevated pressure, using any suitable method known to those skilled in the art. 3
  • the feed wax may be pre-heated to a temperature of at least 230°C, prior to cracking the feed wax in the cracking stage.
  • the feed wax is preheated to a temperature of at least 260°C, prior to cracking the feed wax in the cracking stage.
  • the thermal cracking is thus effected at an elevated temperature, which may be in the range of 360°C to 600°C.
  • the thermal cracking is effected at a temperature in the range of 420 °C to 520°C, e.g. at about 460 °C.
  • the cracking of the hard wax may be conducted at an elevated pressure.
  • the elevated pressure may be in the range of 1 00kPa g to 1 500kPa g , more preferably in the range of 350kPa g to 600kPa g , e.g . at about 500kPa g . It will be appreciated that, by raising the pressure in the cracking stage, the equilibrium between vapour present or formed during the cracking of the feed wax and the liquid wax in the cracking stage, is effected . At lower pressures, removal of lighter components from the cracking stage is thus facilitated.
  • the cracking may be effected for a sufficient period of time to obtain a desired degree of cracking, e.g. from about 30 seconds to about 30 minutes.
  • a desired degree of cracking e.g. from about 30 seconds to about 30 minutes.
  • the residence time of the feed wax in the cracking stage i.e. the cracking time, required to obtain a desired degree of cracking, is dependant on the temperature at which the cracking occurs, and the residence time may thus fall outside the range provided above.
  • the cracking may be effected in the presence of an inert gas, e.g . steam or nitrogen.
  • the inert gas may be used to control the residence time of the feed wax in the cracking stage. 4
  • a light fraction of the lighter wax formed during the cracking stage and the inert gas may be separated from any uncracked feed wax and/or from a heavier fraction of the lighter wax formed during the cracking stage by any suitable separation method known to those skilled in the art, e.g. stripping and/or distillation. At least a portion of any uncracked feed wax and/or at least a portion of the heavier fraction of the lighter wax may be recycled to the cracking stage, where it is cracked or recracked together with fresh feed wax, thus increasing the yield of the process.
  • the products from the cracking stage may be passed to a quenching stage, to lower the temperature and thus to halt the cracking.
  • the invention extends to a lighter wax when produced by the process as hereinbefore described.
  • the congealing point or temperature, Y, of the lighter wax is in the range 60°C to 90°C.
  • the lighter wax may be separated into different product fractions by using methods known to those skilled in the art, such as distillation.
  • the product fractions include, but are not limited to
  • Some or all of these product fractions may be hydrotreated or oxidised to modify the product fraction characteristics.
  • the Applicant has surprisingly found that by subjecting a hard wax, particularly a Fischer-Tropsch derived hard wax to a mild thermal cracking process, a lighter wax is produced as a primary product.
  • the lighter wax has a similar range of hydrocarbons than the hard wax, but has higher concentrations of the lighter hydrocarbons in the range, and thus has a lower congealing temperature than the hard wax.
  • the Applicant has also surprisingly found that the process is very flexible and that the composition (carbon distribution) of the lighter wax can be controlled to a large extent through manipulation of the temperature at which the cracking of the hard wax is effected, the residence time of the hard wax in the cracking stage, the use of an inert, and the use of a recycle as described above.
  • reference numeral 1 0 generally indicates a process according to the invention for converting a Fischer- Tropsch derived hard wax to a lighter wax having a congealing temperature which is less than the congealing temperature of the hard wax.
  • the process 10 includes a feed line 1 2 leading to a pre-heater
  • a flow line 1 6 leads from the pre-heater 1 4 to a cracker 1 8.
  • An inert feed line 20 leads to the cracker 1 8, and a flow line 22 leads from the cracker 1 8 to a cooler 24.
  • a flow line 26 leads from the cooler 24 to a distillation column 28. 6
  • An overhead withdrawal line 30 leads from the top of the distillation column 28, and a bottom withdrawal line 32 leads from the bottom of the distillation column 28.
  • a recycle flow line 34 leads from the bottom withdrawal line 32 into the flow line 1 6.
  • other tie-in points for the recycle flow line 34 e.g . into the feed line 1 2, are feasible.
  • a quench line 36 leads from the recycle flow line 34 into the flow line 22.
  • a feedstock comprising a Fischer-Tropsch derived hard wax, typically having a congealing temperature, X, above about 90 °C, enters the process 10 along the feed line 1 2 and is pre-heated to a temperature of 280°C in the pre-heater 1 4 to provide a pre-heated hard wax feedstock.
  • the pre-heated hard wax feedstock is mixed with recycled uncracked hard wax and/or a heavier fraction of the lighter wax fed from the recycle flow line 34, before the resultant wax mixture enters the cracker 1 8.
  • the wax mixture is cracked at an elevated temperature of 480°C and at an elevated pressure of 400kPa g , in the presence of an inert gas such as steam or nitrogen, fed to the cracker 1 8 by means of the inert feed line 20.
  • the wax mixture has a residence time in the cracker 1 8 of about 1 5 minutes.
  • at least a portion of the wax mixture is cracked to produce a wax product which includes, as a primary product, a lighter wax having a congealing temperature, Y, which is less than the congealing temperature of the hard wax feedstock.
  • Y is in the range of 60 - 90°C.
  • the wax product may also include uncracked hard wax. 7
  • the wax product leaves the cracker 1 8 through the flow line
  • the quenched wax product enters the cooler 24, where its temperature is further reduced to about 300 °C, before it is fed along the flow line 26 into the distillation column 28.
  • the wax product (and thus also the lighter wax) is separated into a light hydrocarbon fraction, which includes the inert gas, and which leaves the distillation column 28 along the overhead withdrawal line 30, and a heavier hydrocarbon fraction which includes any uncracked hard wax and which leaves the distillation column
  • the heavier hydrocarbon fraction to be recycled is withdrawn from the bottom withdrawal line 32 and recycled into the flow line 1 6 by means of the recycle flow line 34, as described above.
  • a Fischer-Tropsch derived hard wax having a congealing temperature of 101 °C and comprising 59% m/m of hydrocarbons having a carbon number above C 49 and 21 % m/m of hydrocarbons having a carbon 8 number between C 19 and C 41 (See Table 1 ) was cracked in a cracking stage at about 440°C and about 500kPa g for a period of about 1 5 minutes.
  • the cracking of the hard wax was conducted in the absence of an inert gas.
  • a lighter wax having a congealing temperature of 88 °C and comprising 24% m/m of hydrocarbons having a carbon number above C 4g and 54% m/m of hydrocarbons having a carbon number between C 1g and C 41 (see Table 2) was produced, as a heavier hydrocarbon fraction of the primary product, after a light hydrocarbon fraction was removed.
  • the lighter wax produced has a similar range of hydrocarbons as the Fischer-Tropsch derived hard wax, but has higher concentrations of the lighter hydrocarbons in the range, which explains the lower congealing temperature of the lighter wax.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé permettant de traiter une cire, lequel procédé consiste à faire subir un craquage thermique, lors d'une phase de craquage, à une cire d'alimentation présentant un point de congélation X °C, de manière à produire, comme produit primaire, une cire plus légère présentant un point de congélation Y °C, X étant supérieur à Y. On utilise généralement comme cire d'alimentation une cire dure dérivée de type Fischer-Tropsch.
PCT/EP1999/000293 1998-01-27 1999-01-19 Traitement des cires Ceased WO1999037737A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU26191/99A AU2619199A (en) 1998-01-27 1999-01-19 Treatment of waxes

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ZA98660 1998-01-27
ZA98/0660 1998-01-27

Publications (1)

Publication Number Publication Date
WO1999037737A1 true WO1999037737A1 (fr) 1999-07-29

Family

ID=25586831

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1999/000293 Ceased WO1999037737A1 (fr) 1998-01-27 1999-01-19 Traitement des cires

Country Status (2)

Country Link
AU (1) AU2619199A (fr)
WO (1) WO1999037737A1 (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001046340A1 (fr) * 1999-12-22 2001-06-28 Chevron U.S.A. Inc. Transformation d'alcanes c1-c3 et de produits de fischer-tropsch en alpha olefines et en autres hydrocarbures liquides
WO2002070601A1 (fr) * 2001-03-02 2002-09-12 Exxonmobil Research And Engineering Company Amelioration de l'indice de fluidite des polymeres par adjonction de cires fischer-tropsch presentant un poids moleculaire eleve
WO2006070006A2 (fr) 2004-12-30 2006-07-06 Shell Internationale Research Maatschappij B.V. Procede de preparation d'olefines inferieures a partir de paraffine lourde
EP2690156A1 (fr) 2012-07-25 2014-01-29 Terra Trade Spólka Z O.O. Procédé de production des cires paraffiniques et leur utilisation

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB773237A (en) * 1954-02-10 1957-04-24 Ruhrchemie Ag Process for softening hard paraffin wax by cracking

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB773237A (en) * 1954-02-10 1957-04-24 Ruhrchemie Ag Process for softening hard paraffin wax by cracking

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001046340A1 (fr) * 1999-12-22 2001-06-28 Chevron U.S.A. Inc. Transformation d'alcanes c1-c3 et de produits de fischer-tropsch en alpha olefines et en autres hydrocarbures liquides
US6497812B1 (en) 1999-12-22 2002-12-24 Chevron U.S.A. Inc. Conversion of C1-C3 alkanes and fischer-tropsch products to normal alpha olefins and other liquid hydrocarbons
WO2002070601A1 (fr) * 2001-03-02 2002-09-12 Exxonmobil Research And Engineering Company Amelioration de l'indice de fluidite des polymeres par adjonction de cires fischer-tropsch presentant un poids moleculaire eleve
WO2006070006A2 (fr) 2004-12-30 2006-07-06 Shell Internationale Research Maatschappij B.V. Procede de preparation d'olefines inferieures a partir de paraffine lourde
WO2006070006A3 (fr) * 2004-12-30 2006-08-24 Shell Int Research Procede de preparation d'olefines inferieures a partir de paraffine lourde
EA010360B1 (ru) * 2004-12-30 2008-08-29 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ получения низших олефинов из тяжелой фракции синтетической нефти, полученной процессом фишера-тропша
EP2690156A1 (fr) 2012-07-25 2014-01-29 Terra Trade Spólka Z O.O. Procédé de production des cires paraffiniques et leur utilisation

Also Published As

Publication number Publication date
AU2619199A (en) 1999-08-09

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