AU2006341463A1 - A process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock - Google Patents

A process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock Download PDF

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Publication number
AU2006341463A1
AU2006341463A1 AU2006341463A AU2006341463A AU2006341463A1 AU 2006341463 A1 AU2006341463 A1 AU 2006341463A1 AU 2006341463 A AU2006341463 A AU 2006341463A AU 2006341463 A AU2006341463 A AU 2006341463A AU 2006341463 A1 AU2006341463 A1 AU 2006341463A1
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cd
feedstock
preferably
tan
process according
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AU2006341463A
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Carolus Matthias Anna Maria Mesters
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Priority to PCT/EP2006/061302 priority Critical patent/WO2007112782A1/en
Publication of AU2006341463A1 publication Critical patent/AU2006341463A1/en
Assigned to SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V. reassignment SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V. Alteration of Name(s) of Applicant(s) under S113 Assignors: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/066Zirconium or hafnium; Oxides or hydroxides thereof
    • 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
    • C10G45/00Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063Titanium; Oxides or hydroxides thereof
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/10Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/02Solids
    • B01J35/10Solids characterised by their surface properties or porosity
    • B01J35/1004Surface area
    • B01J35/101410-100 m2/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/02Solids
    • B01J35/10Solids characterised by their surface properties or porosity
    • B01J35/1004Surface area
    • B01J35/1019100-500 m2/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/02Solids
    • B01J35/10Solids characterised by their surface properties or porosity
    • B01J35/1033Pore volume
    • B01J35/1038Pore volume less than 0.5 ml/g
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0018Addition of a binding agent or of material, later completely removed among others as result of heat treatment, leaching or washing,(e.g. forming of pores; protective layer, desintegrating by heat)
    • 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
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1033Oil well production fluids
    • 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
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20Characteristics of the feedstock or the products
    • C10G2300/201Impurities
    • C10G2300/202Heteroatoms content, i.e. S, N, O, P
    • C10G2300/203Naphthenic acids, TAN

Description

WO 2007/112782 PCT/EP2006/061302 A PROCESS FOR REDUCING THE TOTAL ACID NUMBER (TAN) OF A LIQUID HYDROCARBONACEOUS FEEDSTOCK Field of the invention The present invention provides a process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock, in particular crude oil. 5 Background of the invention Crude oil and other liquid hydrocarbonaceous streams with a high amount of acids are difficult to refine. Especially in the distillation unit of a crude oil refinery, a high amount of acids leads to corrosion 10 problems. It is known that acids are removed by hydrotreating, i.e. the same process wherein other heteroatoms like sulphur and nitrogen are removed from liquid hydrocarbonaceous feedstocks. Hydrotreating, however, is a process that is carried out downstream of 15 the distillation unit in a refinery. In order to avoid corrosion problems resulting from the acid content of the crude oil, different crude oil streams are typically blended to obtain a crude oil feedstock with an acceptable amount of acids. 20 The acid content of a crude oil or of other hydrocarbonaceous liquids is generally expressed as the total acid number (TAN) of such liquid. The TAN represents milligrams KOH per gram liquid needed to neutralise the acid according to a procedure described in 25 ASTM D664. There is a need in the art for a process that is able to reduce the TAN of liquid hydrocarbonaceous streams such as crude oil that are used as feedstock in WO 2007/112782 PCT/EP2006/061302 -2 refineries, with minimum conversion of sulphur- and nitrogen-containing compounds and unsaturated hydrocarbons. By such process, an acceptable refinery feedstock would be obtained with minimal hydrogen 5 consumption. Summary of the invention It has been found that catalysts that are essentially free of the hydrogenating components that are typically used for hydroconversion reactions such as 10 hydrodesulphurisation, hydrodenitrogenation, and hydrocracking, i.e. compounds of metals of any one of Columns 5 to 10 of the Periodic Table of Elements, can be used for the selective hydrogenation of acids in liquid hydrocarbonaceous streams, in particular crude oil. 15 Accordingly, the present invention provides a process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock, wherein the feedstock is contacted, in the presence of a hydrogen-containing gas and at a temperature in the range of from 200 to 20 400 0 C and at elevated pressure, with a catalyst comprising an oxide of a metal of Column 3 or 4 of the Periodic Table of Elements or of a lanthanide, which catalyst is essentially free of Column 5 to 10 metals or compounds thereof, to obtain a liquid hydrocarbonaceous 25 product with a reduced total acid number. An advantage of the process according to the invention is that the total acid number of the feedstock is reduced by hydrogenation whilst other hydrogenation reactions such as hydrodesulphurisation, 30 hydrodenitrogenation and saturation of unsaturated hydrocarbons are minimised.

WO 2007/112782 PCT/EP2006/061302 -3 Detailed description of the invention In the process according to the invention, a liquid hydrocarbonaceous feedstock is contacted, in the presence of a hydrogen-containing gas at a temperature in the 5 range of from 200 to 400 0C and at elevated pressure, with a catalyst comprising an oxide of a Column 3 or 4 metal or of a lanthanide, which catalyst is essentially free of Column 5 to 10 metals or compounds thereof. The feedstock may be any liquid hydrocarbonaceous 10 stream comprising carboxylic, i.e. organic, acids. The process is particularly suitable for feedstocks comprising naphthenic acids. Preferably, the feedstock is a crude oil, a distillate stream such as naphtha or gasoil, a residue fraction of an atmospheric crude oil 15 distillation or a hydrocarbonaceous distillate product not meeting TAN product specifications, such as for example heating oil. The process according to the invention is particularly suitable for the reduction of the total acid number of crude oil. 20 The hydrogen-containing gas is preferably hydrogen or synthesis gas. The use of synthesis gas as hydrogen containing gas is particularly advantageous in a situation wherein no hydrogen gas is available, for example at remote places such as off-shore oil platforms. 25 The temperature and pressure at which the feedstock is contacted with the catalyst is such that hydrogenation of carboxylic acids takes place, i.e. at least 200 C. The temperature is below the temperature at which thermal decomposition of carboxylic acids occurs, i.e. below 30 400 C. Preferably, the temperature is in the range of from 250 to 390 C, more preferably of from 300 to 380 OC.

WO 2007/112782 PCT/EP2006/061302 -4 The process is performed at elevated pressure, i.e. above atmospheric pressure. Preferably, the pressure is in the range of from 2 to 200 bar g, more preferably of from 10 to 150 bar g, even more preferably of from 25 to 5 120 bar g. The catalyst comprises an oxide of a metal of Column 3 or 4 of the Periodic Table of Elements (latest IUPAC notation) or of a lanthanide. The oxide may also be a mixed oxide of two or more of such metals. The catalyst 10 may also comprise a mixture of two or more of such oxides. The catalyst is essentially free of metals of Columns 5 to 10 of the Periodic Table of Elements (latest IUPAC notation) or of compounds thereof. Reference herein to a catalyst essentially free of certain compounds is to 15 a catalyst that is free of such compounds except for minimal amounts, typically in the ppm range or lower, that may be present as unintentional contaminants or as left-overs from a mineral ore refining process for obtaining the oxide of the Column 3 or 4 metal or 20 lanthanide. Preferably, the catalyst comprises an oxide of a Column 4 metal or of a lanthanide. Preferred Group 4 metal oxides are titanium oxide and zirconium oxide, a preferred oxide of a lanthanide is ceria. More 25 preferably, the catalyst consists of titanium oxide and/or zirconium oxide, even more preferably of zirconium oxide. The catalyst may be prepared by any preparation method known in the art. Preferably, the catalyst is 30 prepared such that its specific surface area is at least 10 m 2 /g, more preferably at least 30 m 2 /g. The feedstock for the process according to the invention preferably has a total acid number of at least WO 2007/112782 PCT/EP2006/061302 -5 0.2 mg KOH/g feedstock, preferably at least 0.5 mg KOH/ g feedstock, more preferably at least 1.0 mg KOH/ g feedstock. Reference herein to the total acid number is to the amount of KOH (in mg) per gram feedstock as 5 determined by ASTM D664. The liquid hydrocarbonaceous product has preferably a TAN of at most 0.2 mg KOH/g feedstock, more preferably at most 0.1 mg KOH/g feedstock, even more preferably at most 0.05 mg KOH/g feedstock. 10 The TAN is preferably reduced to such extent that the liquid hydrocarbonaceous product with a reduced total acid number has at most 50% of the TAN of the feedstock, more preferably at most 30%. Example 15 Hydrogenation process In a microflow reactor, crude oil was contacted with a solid inert material (0.1 mm silicon carbide particles) or with one of the catalysts described below (catalyst particles diluted with silicon carbide particles: 20 1/1 v/v) in the presence of a hydrogen-containing gas or nitrogen for at least 100 hours. Two different crude oils were used. For experiments 1 to 8 and 13 to 16, a West African crude oil was used (crude 1); for experiments 9 to 12, a crude oil from the Middle-East was used 25 (crude 2). The specifications of both crude oils are shown in table 1. The exact conditions for each experiment are given in table 2. The total acid number (TAN) of the liquid effluent of each of the experiments was determined according to 30 ASTM D664. The hydrogen sulphide concentration in the vapour phase effluent was determined by gas chromatography. TAN of the liquid effluent and the WO 2007/112782 PCT/EP2006/061302 -6 hydrogen sulphide concentration in the vapour phase effluent are also shown in table 2. Experiments 3, 4, 6, 7, 9, 10, 12 and 14 to 16 are experiments according to the invention. Experiments 1, 2, 5 5, 8, 11, and 13 are comparison experiments. Table 1 Crude oil specification Crude 1 Crude 2 Property Sulphur content (% wt) 0.41 4.1 Ni content (mg/kg) 32 36 V content (mg/kg) 4 138 TAN (mg KOH/g oil) 2.7 1.3 Density (g/ml) 0.93 0.91 Sediment (mg/kg) 10 1250 Water content (% wt) 0.08 0.27

C

5 + asphalthenes (mg/kg) 0.26 9.7 Catalysts The following catalysts were used in the hydrogenation experiments. Titania catalyst 1 10 A titania catalyst further referred to as titania 1 was prepared as follows. An amount of 3192 grams of titania powder (P25, ex. Degussa; loss on ignition: 4.4 wt% at 540 0 C) was mixed with 100 grams oxalic acid dihydrate in a mix-muller kneader (Simpson). After 15 4 minutes of mix-mulling, 981 grams of de-ionised water and 100 grams of polyethylene glycol were added and mix mulling was continued for another 12 minutes. Then, 100 grams of methyl cellulose were added and mix-mulling was continued for another 20 minutes. The thus-formed WO 2007/112782 PCT/EP2006/061302 -7 mixture was shaped by extrusion through a 1.7 mm diameter trilobe-shaped die-plate. The trilobes were dried for 2 hours at 120 0 C and calcined for 2 hours at 500 'C. The resulting titania trilobes have a surface area 5 of 52 m 2 /g as measured by nitrogen adsorption (BET method) and a pore volume of 0.31 ml/g as measured by mercury intrusion. Titania catalyst 2 Titania particles commercially available as X096 10 (ex. CRI Catalyst Company) were used as titania catalyst (further referred to as titania 2). These titania particles have a surface area of 120 m 2 /g as measured by nitrogen adsorption (BET method) and a pore volume of 0.32 ml/g as measured by mercury intrusion. 15 Zirconia catalyst A zirconia catalyst was prepared as follows. An amount of 264 grams of zirconia powder (RC100, ex. Daiichi; loss on ignition: 5.3 wt% at 540 0 C) was mixed with 90 grams of a solution of 5 wt% polyvinyl alcohol in 20 de-ionised water in a kneader (Werner&Pfeider Sigma kneader type LUK 0.75). After 7 minutes of kneading, 2.5 grams of a cationic poly acryl amide (Superfloc, ex. Cytec) were added and after 20 minutes of kneading 8 grams of de-ionised water were added. The mixture was 25 kneaded for another 22 minutes. The thus-formed mixture was shaped by extrusion into 1.7 mm diameter trilobes. The extrudates were dried for 2 hours at 120 0 C and calcined for 2 hours at 550 C. The resulting zirconia trilobes have a surface area 30 of 54 m 2 /g as measured by nitrogen adsorption (BET method) and a pore volume of 0.35 ml/g as measured by mercury intrusion.

WO 2007/112782 PCT/EP2006/061302 -8 NiMo on alumina A conventional hydrodesulphurisation catalyst comprising Ni and Mo on alumina, which is commercially available as CRITERION RM-5030 (ex. Criterion Catalyst 5 Company), was used.

WO 2007/112782 PCT/EP2006/061302 0 CCd U) -(I') C C ) )C CD C) d)LC) LiD CdLi CD CD 4 C) CD i S H(N (Nl C) C)D ( V CD C) C) C) V V 0 ~> U) - CD CD CD CD CD CD CD CD CD C) CD CD (1d co (N Q0 Q0 F- > ) co 00 LO) C) LiD Lr) ZT C) 4 r- F- > N (N (9 (N (N (N (N (n (N (N -C 4J C) CD CD CD CD CD CD CD C) C) C) C) CD C) CD C) CD LiD f) if) Li LD if) LiD -H L4H4 Cd CD CD CD 0 C) C) C) C) C) C) C) C) C) C) C) CD v-HU) U) Nd C)) N N N \ -H U) od Cd U) (N (N ( N ( (N >(N (NN >i (N (N .H 4U) Pd 44J 4J -H- 5 4) 4- -H 01 0- -- d -H 1 -H -H - -H Cd -H H l Cd- -H 02 Cd Cd 41 4 2 4-) 41 m~~ d 4 41 M2 C 4-2 U) -Cd (D N 42 CL4 41 Cd 4 co >x 0 C) v-H (N H U) -H (N (n 31 (9) (9 - 0 ) () -H v- WO 2007/112782 PCT/EP2006/061302 42 co Cd 4J CO CD CD 4- 0M Q4 N ,- Cd~ 04 'T U -C) mf U v v md 0 0. 4-2 CD CD -H. C> C) C) CD 2 )C C) C) C4 -H a >1 0.C Q 4 4 Cd a) a)C ) C -C d t C Ud Cd -C C)D~ ) C d DQ 0d 0-H (0 m CDU ) ( -nU U-) -H0 Cd d Cd Cd Cd 4 Cd Cd C 0) >,i C5 Cd Cd > C H Cfd co '-H -H* 0 Cd Cd 4-A~ 0 qd CdCd r-H 0 0 -Hu Cd -0 CL 0 f) U) m n )>, \ Cdi H - 0 e- (n0 Cd =d> 0.~~ (___ 44dC C -H -1 CD -4 CD Cd Cd '4 H 0 Cd~ 0.-1C -H : Cd1 -0 -0 Cd 0 Cd '-4 C) Z .Q C) C)d U) a) u -Cd 'Cd ( 41 m C-4 C\1 H Cd -4 > H 0 -H> 42) 4-) 0 0 C 4-- a) - 4 -- (N ) - 0. Cd d -Q Q) 0)44 4 m 00 m0 co Cd m 0 -H CH Cd r- Cd M '440 Cd ffd 42 Cd r:N (N ( (N0d C -H4 co 1 -H H. 42 42 C Q '0 u H-H Cd C -H -4 Cd4H '-1 Cd -4 rl -H0 Cd 0 5 d C dr~ C H- - H U)4 42 2 Cd 42 414 CdU -H4 -m -H -H -a)~- d (D4 1-1 Cd 4 -H -H -H Cd Cd4 03 '- '4 'i Cd (0 - 0 '0 -H '0 Cd 4 '0 tC C :Cd Cd) co C) 0 '-H -HT '-4 '-H -C d C) C - H Cd U. -H -H 4-4

Claims (10)

1. A process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock, wherein the feedstock is contacted, in the presence of a hydrogen containing gas and at a temperature in the range of from 5 200 to 400 0 C and at elevated pressure, with a catalyst comprising an oxide of a metal of Column 3 or 4 of the Periodic Table of Elements or of a lanthanide, which catalyst is essentially free of Column 5 to 10 metals or compounds thereof, to obtain a liquid hydrocarbonaceous 10 product with a reduced total acid number.
2. A process according to claim 1, wherein the oxide is an oxide of a Column 4 metal or of a lanthanide, preferably is titanium oxide or zirconium oxide, more preferably zirconium oxide. 15
3. A process according to claim 2, wherein the catalyst essentially consists of titanium oxide and/or zirconium oxide.
4. A process according to any one of the preceding claims, wherein the pressure is in the range of from 2 to 20 200 bar g, preferably of from 10 to 150 bar g, more preferably 25 to 120 bar g.
5. A process according to any one of the preceding claims, wherein the temperature is in the range of from 250 to 390 'C, preferably of from 300 to 380 'C. 25
6. A process according to any one of the preceding claims, wherein the hydrogen-containing gas is synthesis gas or hydrogen.
7. A process according to any one of the preceding claims, wherein the feedstock has a TAN of at least WO 2007/112782 PCT/EP2006/061302 - 12 0.2 mg KOH/g feedstock, preferably at least 0.5 mg KOH/ g feedstock, preferably at least 1.0 mg KOH/g feedstock.
8. A process according to any one of the preceding claims, wherein the liquid hydrocarbonaceous product has 5 a TAN of at most 0.2 mg KOH/g feedstock, preferably at most 0.1 mg KOH/g feedstock, more preferably at most 0.05 mg KOH/g feedstock.
9. A process according to any one of the preceding claims, wherein the liquid hydrocarbonaceous product with 10 a reduced total acid number has a TAN of at most 50% of the TAN of the crude oil product, preferably at most 30%.
10. A process according to any one of the preceding claims, wherein the liquid hydrocarbonaceous feedstock is crude oil.
AU2006341463A 2006-04-04 2006-04-04 A process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock Abandoned AU2006341463A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2006/061302 WO2007112782A1 (en) 2006-04-04 2006-04-04 A process for reducing the total acid number (tan) of a liquid hydrocarbonaceous feedstock

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EP (1) EP2001976A1 (en)
JP (1) JP5399234B2 (en)
CN (1) CN101405371B (en)
AU (1) AU2006341463A1 (en)
CA (1) CA2647760C (en)
MX (1) MX2008012567A (en)
WO (1) WO2007112782A1 (en)

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB496779A (en) * 1937-01-04 1938-12-06 Bataafsche Petroleum A process for removing naphthenic acids from mineral lubricating oils or lubricating oil fractions
US3846288A (en) * 1973-07-05 1974-11-05 Gulf Research Development Co Acid number reduction of hydrocarbon fractions using a solid catalyst and methanol
US6547957B1 (en) * 2000-10-17 2003-04-15 Texaco, Inc. Process for upgrading a hydrocarbon oil
US20020148754A1 (en) * 2001-02-08 2002-10-17 Gong William H. Integrated preparation of blending components for refinery transportation fuels
BRPI0405578B1 (en) * 2003-12-19 2014-08-19 Shell Internationale Res Maaschappij B V Crude oil product and method for producing transport fuel, heating fuel, lubricants or chemical substances
EP1781760A1 (en) * 2004-07-07 2007-05-09 California Institute Of Technology Process to upgrade oil using metal oxides

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MX2008012567A (en) 2008-10-10
JP2009532536A (en) 2009-09-10
CN101405371B (en) 2012-07-18
JP5399234B2 (en) 2014-01-29
CA2647760C (en) 2013-12-10
EP2001976A1 (en) 2008-12-17
WO2007112782A1 (en) 2007-10-11
CN101405371A (en) 2009-04-08
CA2647760A1 (en) 2007-10-11

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