WO2006005085A2 - Traitement des hydrocarbures - Google Patents

Traitement des hydrocarbures Download PDF

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Publication number
WO2006005085A2
WO2006005085A2 PCT/ZA2005/000101 ZA2005000101W WO2006005085A2 WO 2006005085 A2 WO2006005085 A2 WO 2006005085A2 ZA 2005000101 W ZA2005000101 W ZA 2005000101W WO 2006005085 A2 WO2006005085 A2 WO 2006005085A2
Authority
WO
WIPO (PCT)
Prior art keywords
acid
metal
treatment
oxygenates
hydrocarbons
Prior art date
Application number
PCT/ZA2005/000101
Other languages
English (en)
Other versions
WO2006005085A3 (fr
Inventor
Jan Mattheus Botha
Dieter Otto Leckel
Jacobus Lucas Visagie
Herman Preston
Donovan Smook
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 BRPI0512754A priority Critical patent/BRPI0512754B1/pt
Priority to GB0625235A priority patent/GB2429461B/en
Priority to AU2005260789A priority patent/AU2005260789B2/en
Publication of WO2006005085A2 publication Critical patent/WO2006005085A2/fr
Publication of WO2006005085A3 publication Critical patent/WO2006005085A3/fr
Priority to NO20070042A priority patent/NO343008B1/no

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Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2/00Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts

Definitions

  • the invention relates to hydrothermal treatment of hydrocarbons prior to further processing.
  • the invention provides for a pre-treatment regime for Fischer-Tropsch (F-T) hydrocarbons prior to downstream processing.
  • F-T Fischer-Tropsch
  • the invention also relates to a chemical treatment of hydrocarbons prior to further processing.
  • the inventors have identified an area for process optimization in the processing of hydrocarbons.
  • the inventors have identified an area for process optimization in the processing of F-T synthesis products by hydroconversion in general.
  • F-T derived product streams contain oxygenates and to a certain extent metals and/or metal species.
  • Ketones, aldehydes, alcohols, esters and carboxylic acids are the main constituents of the oxygenate fraction.
  • Carboxylic acids and alcohols are able to form under appropriate conditions carboxylate and/or alkoxide complexes and/or metalloxanes with the metals and/or metal species present.
  • These metal carboxylates and/or alkoxides and/or metalloxanes may form deposits in processing equipment and catalyst beds. Eventually the deposits in the catalyst beds may grow to such an extent that shutdowns of reactors are inevitable.
  • the identified problem may be summarized as the plugging of downstream processing catalyst beds or bed by a constituent of said product streams or a reaction product of a constituent of said product, streams.
  • organometallic material and/or fine particulates are likely to be rich in aluminium, and/or silicon, and/or titanium, and/or zirconium, and/or cobalt, and/or iron, and/or alkaline earth elements such as calcium and barium etc.
  • the synthesis products from the F-T process were analyzed and it was found that the condensate fraction is devoid of metal impurities (1 ppm or less), but that the wax contains metal impurities in the order of 10 - 100 ppm. This indicates that the F-T process and/or filtration system and/or refractory materials and/or chemically leached metals or metal species may be the source of the metal impurities.
  • metal oxygenate species that contribute to bed plugging and either one or both may be important:
  • Fine particulates for example, fine particulates of less than 1 micron in diameter which can be stabilized by surface-active compounds (such as the oxygenates) allowing them to remain in suspension. However, when this surface layer is disrupted, the particulates precipitate and form deposits on collector media.
  • surface-active compounds such as the oxygenates
  • Organometallic type compounds for example, in the case of aluminium as the metal source, the formation of organoaluminium compounds of the Al-O-R type, like alkoxy-aluminium, aluminium carboxylates and alumoxanes, or of the Al-R type, like alkyl-aluminium, or combinations thereof are possible.
  • Bed-plugging has been seen with various catalysts and it occurs as a localized plug or as distributed particulate matter.
  • the F-T synthesis product stream carries organometallic material and/or solubilized fine catalyst particulates and/or filter aid and/or refractory material and/or chemically leached metals or metal species from the reactor system in low concentrations.
  • the wax contains oxygenates like acids and alcohols that help to keep the fine particulates in solubilized form in the wax.
  • oxygenates that keep the particulates in suspension, and/or the ligands of the organometallic components, are hydrogenated and/or protonated and the modified metal species are then deposited on the hydroconversion reactor catalyst bed, leading to what is termed "bed-plugging".
  • a method of treatment of hydrocarbons including hydrothermal treatment at a temperature of above 100 0 C of metal oxygenate components in F-T derived hydrocarbons.
  • the method may include chemical treatment of the metal oxygenate components in the F-T derived hydrocarbons, to modify the metal oxygenates,.
  • the method may include one or more of the following treating stages:
  • F-T derived hydrocarbons contain oxygenates and to a certain extent metals and/or metal species.
  • Ketones, aldehydes, alcohols, esters and carboxylic acids are the main constituents of the oxygenate fraction.
  • Carboxylic acids are able to form under appropriate conditions metal carboxylate complexes with the metal species present.
  • Alcohols are able to form under appropriate conditions metal alkoxide complexes with the metal species present.
  • the metal oxygenate may be a metal carboxylate, a metal alkoxide or a combination thereof or a metalloxane.
  • the metal oxygenate may be a carboxy substituted metalloxane.
  • the hydrothermal treatment may be carried out with water at above 100 0 C, preferably between 120 0 C to 370 0 C, and even as high a 400 0 C, typically 16O 0 C to 250 0 C and a pressure of 1 to 100 bar, preferably 5 to 50 bar..
  • the water for the hydrothermal treatment may be water added for the purpose of the hydrotreatment or reaction water already present in the F-T derived hydrocarbons, or a combination of both.
  • the hydrothermal treatment may be carried out in a substantially single liquid phase system in which both the hydrocarbons and water are present, said water being present at such levels as to ensure that substantially one liquid phase is present under the process conditions.
  • the hydrothermal treatment may be carried out in the presence of an adsorbent such as silica. Adsorption of the modified metal oxygenates takes place on the silica particles and these may subsequently be removed by filtration or other treating methods.
  • an adsorbent such as silica. Adsorption of the modified metal oxygenates takes place on the silica particles and these may subsequently be removed by filtration or other treating methods.
  • the hydrothermal treatment may also be achieved by maintaining the product stream under the temperature and pressure used in the F-T reactor after a primary filtration zone for sufficient time to enable particle growth and/or adsorption onto a filterable particle, i.e. the hydrothermal treatment may be carried out by maintaining the reactor conditions between primary and secondary filtration zones for sufficient time to allow for particle growth or adsorption onto a filterable particle.
  • the pressure may be selected to be higher than the water vapour pressure at the prevailing temperature. Sufficient time will be between 1 to 60 minutes, preferably between 1 to 30 minutes and more preferably between 5 to 10 minutes.
  • the optional chemical treatment may include trans-esterification to exchange longer hydrocarbon chain carboxylic acids or alcohols with shorter chain carboxylic acids.
  • the chemicals which may be used in the trans-esterification or ligand replacement step include, methanol, ethanol, oxalic acid, acetic acid, propanoic acetic, salicylic acid, succinic acid, tartaric acid, lactic acid, malonic acid, glycine acid, citric acid, carbonic acid, maleic acid, fumaric acid, phthalic acid, the anhydrides of these acids (e.g. maleic anhydride) and thermal decomposition products of these acids. Also included are solid acids such as silica-alumina and/or other mixed oxide systems that possess Br ⁇ nsted acidity. The interaction between these listed chemicals and the metal oxygenates may be speeded up by the thermal treatments.
  • Hydrothermal treatment may result in hydroxylation and formation of metal hydroxides and/or metal oxyhydroxides and/or metalloxanes.
  • the hydrothermal treatment may be done before, with or after the optional chemical treatment.
  • a method of treatment of hydrocarbons including chemical treatment with one or more chemical treatment agents in a single liquid phase of metal oxygenate components in F-T derived hydrocarbons to modify the metal oxygenates.
  • the chemical treatment may be followed by one or more of the following treating stages:
  • the chemical treatment agents which may be used in the trans-esterification or ligand replacement step include, methanol, ethanol, oxalic acid, acetic acid, propanoic acetic, salicylic acid, succinic acid, tartaric acid, lactic acid, malonic acid, glycine acid, citric acid, carbonic acid, maleic acid, fumaric acid, phthalic acid, the anhydrides of these acids (e.g. maleic anhydride) and thermal decomposition products of these acids. Also included are solid acids such as silica-alumina and/or other mixed oxide systems that possess Br ⁇ nsted acidity. The interaction between these listed chemicals and the metal oxygenates may be speeded up by the thermal treatments.
  • the chemical treatment may be carried out in a single liquid phase in which both the hydrocarbons and one or more chemical treatment agents are present, said chemical treatment agent or agents being present at levels below their saturation level in the hydrocarbons, for example wax.
  • the amounts of chemical treatment agents added may be such as to give a single liquid phase i.e. total dissolution of the chemical treatment agents in the hydrocarbons under the process conditions.
  • I he chemical treatment may include trans-esterification to exchange longer hydrocarbon chain carboxylic acids or alcohols with shorter chain carboxylic acids.
  • the polar solvents include, amongst others, water, melted organic acids, ethylene glycol, ionic liquids and combinations thereof.
  • Filter materials used in the filtration include clays, silica, silica-aluminas, silicated aluminas, cellulose, activated carbons, sintered metals and material filters such as nylons and polycarbonates.
  • the adsorbents and/or filterable particles include clays, silica, silica-aluminas, silicated aluminas, cellulose, activated carbons, sintered metals, titania and material filters such as nylons and polycarbonates.
  • the adsorbents may also be used as filter material.
  • the adsorbents may be added during the chemical and/or hydrothermal treatment, or during any of the downstream processes.
  • Reactor wax from a Low-Temperature F-T (LTFT) plant was analyzed and found to contain metal carboxylates (M x [ ⁇ 2CR]y), carboxy substituted metalloxanes ([M(O) x (OH)y( ⁇ 2CR) z ] n ), alkoxides and combinations thereof that were leached from the catalyst, and/or support, and/or reactor, and/or filter clays, and/or refractory materials.
  • metal carboxylates M x [ ⁇ 2CR]y
  • carboxy substituted metalloxanes [M(O) x (OH)y( ⁇ 2CR) z ] n
  • alkoxides and combinations thereof were leached from the catalyst, and/or support, and/or reactor, and/or filter clays, and/or refractory materials.
  • modified metal oxygenates obtained from the exchange of the longer hydrocarbon chain carboxylic acids with shorter chain carboxylic acids or hydroxylation with water, result in the modified metal oxygenates being more soluble in polar solvents like water or ethylene glycol and can be extracted from the wax by these polar solvents.
  • modified metal oxygenates obtained from the exchange of the longer hydrocarbon chain carboxylic acids with shorter chain carboxylic acids or hydroxylation with water result in the growth of the particles that can then be filtered out.
  • the modified metal oxygenates obtained from the exchange of the longer hydrocarbon chain carboxylic acid with shorter chain carboxylic acids or alcohols or hydroxylation with water, result in the formation of extractable/adsorbable particles onto an adsorbent.
  • the experimental set-up used for this investigation is displayed in Figure 1. It is a continuous process in down-flow mode. Application of pressure is optional. Water is pumped, using an HPLC pump, from a reservoir placed on a balance, through a 140°C hot pipe. The water (2 wt % relative to the wax) joins the molten wax which is heated up to 140 0 C. The combined streams then trickle over a sand bed heated to a temperature of 35O 0 C. The inert material is used for better distribution or mixing between the aqueous and wax phases and to increase the residence time, giving growth opportunity for the modified aluminium oxygenates and improving the efficiency of the separation process.
  • the product after the sand bed is passed through a 1 micron filter (or smaller) to collect the modified aluminium oxygenate agglomerates.
  • the wax product after the filter has an aluminium content of ⁇ 1 ppm Al as determined by ICP. Filters of a size bigger than 1 micron can be used optionally in combination with a filter aid.
  • PAA Polyacrylic acid
  • the wax (200 g) containing 50 ppm aluminium was first melted in an oven at 140 0 C, and then placed in the Parr autoclave, and heated to 165 0 C with stirring (700 rpm).
  • 0.1 wt % PAA was added to 2 wt % water and placed in a metal tube that was then connected to the Parr reactor. After the desired temperature was reached, the pressure of the vessel was increased to 10 bar through the metal tube. This ensured that all the aqueous solution was forced in the Parr autoclave.
  • the first sample was taken 5 minutes after this addition. Samples were also taken at 10 minutes.
  • the sampling bottle was placed in the oven at 140 0 C. This wax was then hot filtered (140 0 C) through a 0.45 ⁇ m filter paper. The wax was then analyzed for aluminium using ICP. As can be observed from the results, PAA was effective in removing the modified metal oxygenates at 165°C.
  • BA Use of hydrothermal conditions and a filterable particle/adsorbent to modify and adsorb modified metal oxygenates.
  • the wax (200 g) containing soluble metal oxygenates was first melted in an oven at 140 0 C. To the melted wax was added 0.1 -0.01 wt % Aerosil 380 (Degussa). The wax was then heated to 170 0 C with stirring (200 rpm). Water (4 ml) was placed in a metal tube that was connected to the Parr reactor. After the desired temperature was reached, a sample was taken. Thereafter, the water was added to the reaction mixture and samples were taken at 5 and 10 minutes (Table B4) and passed through a 2.5 micron filter. The water modified the metal complex so that it could adsorb onto the filterable particle.
  • wax (200 g) containing 45 ppm aluminium was first melted in an oven at 140 0 C, and then placed in the Parr autoclave, and heated to 170 0 C with stirring (700 rpm).
  • Maleic anhydride (0.1 wt %) dissolved in water (2 wt %) was placed in a metal tube that was then connected to the Parr reactor. After the desired temperature was reached, the pressure of the vessel was increased to 300psi through the metal tube. This ensured that all the aqueous solution was forced in the Parr autoclave. Two samples were taken after 15 minutes after this addition. After the wax was sampled, one sample was placed in the oven at 140 0 C.
  • This wax was then hot filtered (140 0 C) through a 0.8 ⁇ m filter paper.
  • Sample 2 was cooled down before being reheated to 140 0 C and filtered.
  • the aluminium content of the wax was determined using ICP analysis. Unlike the citric acid treated wax, the filterability of the maleic acid treated wax remained the same, whereas the reaction conditions determine the filterability of the citric acid treated wax.
  • contaminated wax was pumped at a set temperature through a 10 mm diameter tube containing adsorbent or filter material.
  • the pressure listed is caused by the wax flow rate and adsorbent characteristics.
  • experiment C1 contaminated wax containing 14 ppm aluminium and other metals such as cobalt, was pumped through a cellulose Arbocel BVB40 as filter/absorbent without water or acid been added (see table C1). No removal of aluminium was observed.
  • experiment C2 In experiment C2, experiment C1 was repeated but 2 wt % water was added to the wax (see Table C2). The addition of water led to the complete removal for continuous filtering of up to 2.5 hours.
  • experiment C3 experiment C2 was repeated but with Vitacel LOO as filter material/adsorbent.
  • experiment C4 was repeated but with Celpure S1000 as filter material/adsorbent.
  • experiment C5 was repeated but with spray dried Degussa silica (Aerosil 380) as filter material/adsorbent.
  • Table C3 Treatment of contaminated wax containing approx. 14 ppm aluminium.
  • Table C4 Treatment of contaminated wax containing approx. 16 ppm aluminium.

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  • 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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)
  • Water Treatment By Sorption (AREA)

Abstract

L'invention concerne un procédé de traitement des hydrocarbures qui comprend le traitement hydrothermique à une température de plus de 100 °C de composés oxygénés dans des hydrocarbures dérivés de F-T.
PCT/ZA2005/000101 2004-07-06 2005-07-04 Traitement des hydrocarbures WO2006005085A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
BRPI0512754A BRPI0512754B1 (pt) 2004-07-06 2005-07-04 tratamento de hidrocarbonetos
GB0625235A GB2429461B (en) 2004-07-06 2005-07-04 Treatment of hydrocarbons
AU2005260789A AU2005260789B2 (en) 2004-07-06 2005-07-04 Method of treatment of Fischer-Tropsch derived hydrocarbons
NO20070042A NO343008B1 (no) 2004-07-06 2007-01-03 Behandling av hydrokarboner

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ZA2004/5364 2004-07-06
ZA200405364 2004-07-06

Publications (2)

Publication Number Publication Date
WO2006005085A2 true WO2006005085A2 (fr) 2006-01-12
WO2006005085A3 WO2006005085A3 (fr) 2006-03-09

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Application Number Title Priority Date Filing Date
PCT/ZA2005/000101 WO2006005085A2 (fr) 2004-07-06 2005-07-04 Traitement des hydrocarbures

Country Status (8)

Country Link
AU (1) AU2005260789B2 (fr)
BR (1) BRPI0512754B1 (fr)
GB (1) GB2429461B (fr)
NL (1) NL1029418C2 (fr)
NO (1) NO343008B1 (fr)
RU (1) RU2383581C2 (fr)
WO (1) WO2006005085A2 (fr)
ZA (1) ZA200610736B (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006053350A1 (fr) * 2004-11-10 2006-05-18 Sasol Technology (Pty) Ltd Traitement de courants d'hydrocarbures de masse molaire elevee
WO2010112690A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procédé de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
WO2010112691A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch mettant en oeuvre une resine
WO2014202596A1 (fr) * 2013-06-20 2014-12-24 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé pour éliminer des métaux à partir de fractions d'hydrocarbures à point d'ébullition élevé
WO2016118982A2 (fr) 2015-01-20 2016-07-28 The Petroleum Oil And Gas Corporation Of South Africa (Pty) Ltd Élimination des particules fines d'un catalyseur ltft
US11306260B1 (en) 2020-10-29 2022-04-19 Marathon Petroleum Company Lp Systems and methods for enhanced inorganic contaminant removal from hydrocarbon feedstock
US11788023B2 (en) 2021-10-12 2023-10-17 Marathon Petroleum Company Lp Systems and methods of converting renewable feedstocks into intermediate hydrocarbon blend stocks and transportation fuels

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2531324A (en) * 1947-10-18 1950-11-21 California Research Corp Preparation of alkylated aromatic hydrocarbons and sulfonation thereof
US2661362A (en) * 1947-11-26 1953-12-01 Standard Oil Dev Co Removal of oxygenated organic compounds from hydrocarbons
WO2002007883A2 (fr) * 2000-07-24 2002-01-31 Sasol Technology (Proprietary) Limited Production d'hydrocarbones a partir d'un gaz de synthese
WO2003012008A2 (fr) * 2001-07-27 2003-02-13 Sasol Technology (Proprietary) Limited Production de cire produite par synthese fischer-tropsch

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2531324A (en) * 1947-10-18 1950-11-21 California Research Corp Preparation of alkylated aromatic hydrocarbons and sulfonation thereof
US2661362A (en) * 1947-11-26 1953-12-01 Standard Oil Dev Co Removal of oxygenated organic compounds from hydrocarbons
WO2002007883A2 (fr) * 2000-07-24 2002-01-31 Sasol Technology (Proprietary) Limited Production d'hydrocarbones a partir d'un gaz de synthese
WO2003012008A2 (fr) * 2001-07-27 2003-02-13 Sasol Technology (Proprietary) Limited Production de cire produite par synthese fischer-tropsch

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006053350A1 (fr) * 2004-11-10 2006-05-18 Sasol Technology (Pty) Ltd Traitement de courants d'hydrocarbures de masse molaire elevee
GB2434589A (en) * 2004-11-10 2007-08-01 Sasol Technology Treatment of high molar mass hydrocarbon streams
GB2434589B (en) * 2004-11-10 2009-02-25 Sasol Technology Treatment of high molar mass hydrocarbon streams
WO2010112690A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procédé de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch
WO2010112691A1 (fr) 2009-04-03 2010-10-07 IFP Energies Nouvelles Procede de production de distillats moyens par hydroisomerisation et hydrocraquage d'une fraction lourde issue d'un effluent fischer-tropsch mettant en oeuvre une resine
WO2014202596A1 (fr) * 2013-06-20 2014-12-24 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé pour éliminer des métaux à partir de fractions d'hydrocarbures à point d'ébullition élevé
WO2016118982A2 (fr) 2015-01-20 2016-07-28 The Petroleum Oil And Gas Corporation Of South Africa (Pty) Ltd Élimination des particules fines d'un catalyseur ltft
US11306260B1 (en) 2020-10-29 2022-04-19 Marathon Petroleum Company Lp Systems and methods for enhanced inorganic contaminant removal from hydrocarbon feedstock
WO2022094560A1 (fr) * 2020-10-29 2022-05-05 Marathon Petroleum Company Lp Systèmes et procédés de séparation d'eau et d'élimination de solides d'une charge d'alimentation prétraitée et non filtrée
US11352570B1 (en) 2020-10-29 2022-06-07 Marathon Petroleum Company Lp Systems and methods for enhanced inorganic contaminant removal from hydrocarbon feedstock
US11702601B2 (en) 2020-10-29 2023-07-18 Marathon Petroleum Company Lp Systems and methods for separating water and removing solids from pre-treated and unfiltered feedstock
US11725151B2 (en) 2020-10-29 2023-08-15 Marathon Petroleum Company Lp Systems and methods for enhanced inorganic contaminant removal from hydrocarbon feedstock
US11788023B2 (en) 2021-10-12 2023-10-17 Marathon Petroleum Company Lp Systems and methods of converting renewable feedstocks into intermediate hydrocarbon blend stocks and transportation fuels
US11993754B2 (en) 2021-10-12 2024-05-28 Marathon Petroleum Company Lp Systems and methods of converting renewable feedstocks into intermediate hydrocarbon blend stocks and transportation fuels

Also Published As

Publication number Publication date
AU2005260789A1 (en) 2006-01-12
GB2429461A (en) 2007-02-28
NO343008B1 (no) 2018-09-24
WO2006005085A3 (fr) 2006-03-09
BRPI0512754A (pt) 2008-04-08
GB2429461B (en) 2009-05-06
BRPI0512754B1 (pt) 2016-03-29
GB0625235D0 (en) 2007-02-07
RU2383581C2 (ru) 2010-03-10
ZA200610736B (en) 2008-09-25
AU2005260789B2 (en) 2010-06-17
RU2007101688A (ru) 2008-08-20
NL1029418A1 (nl) 2006-01-09
NO20070042L (no) 2007-03-23
NL1029418C2 (nl) 2007-03-19

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