Patent Application
20060249430
The present invention provides a process for reducing the total acid number (TAN) of a liquid hydrocarbonaceous feedstock, in particular crude oil.
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 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 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.
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 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 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 consumption.
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 400° 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 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, hydrodenitrogenation and saturation of unsaturated hydrocarbons are minimised.
It has been found that catalysts that are essentially free of the hydrogenating components that are typically used for hydroconversion reactions such as 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.
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 range of from 200 to 400° C. 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 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 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.
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.
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 400° C. Preferably, the temperature is in the range of from 250 to 390° C., more preferably of from 300 to 380° C.
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 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 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 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 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 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 prepared such that its specific surface area is at least 10 m2/g, more preferably at least 30 m2/g.
The feedstock for the process according to the invention preferably has a total acid number of at least 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 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.
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%.
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: 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 (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 ASTM D664. The hydrogen sulphide concentration in the vapour phase effluent was determined by gas chromatography. TAN of the liquid effluent and the 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, 8, 11, and 13 are comparison experiments.
Catalysts
The following catalysts were used in the hydrogenation experiments.
Titania Catalyst 1
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° C.) was mixed with 100 grams oxalic acid dihydrate in a mix-muller kneader (Simpson). After 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 mixture was shaped by extrusion through a 1.7 mm diameter trilobe-shaped die-plate. The trilobes were dried for 2 hours at 120° C. and calcined for 2 hours at 500° C.
The resulting titania trilobes have a surface area of 52 m2/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 (ex. CRI Catalyst Company) were used as titania catalyst (further referred to as titania 2). These titania particles have a surface area of 120 m2/g as measured by nitrogen adsorption (BET method) and a pore volume of 0.32 ml/g as measured by mercury intrusion.
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° C.) was mixed with 90 grams of a solution of 5 wt % polyvinyl alcohol in de-ionised water in a kneader (Wemer&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 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° C. and calcined for 2 hours at 550° C.
The resulting zirconia trilobes have a surface area of 54 m2/g as measured by nitrogen adsorption (BET method) and a pore volume of 0.35 ml/g as measured by mercury intrusion.
NiMo on Alumina
A conventional hydrodesulphurisation catalyst comprising Ni and Mo on alumina, which is commercially available as CRITERION RM-5030 (ex. Criterion Catalyst Company), was used.
aWHV: weight hourly velocity, i.e. kg oil/kg catalyst/hour. In experiments 1 and 2, no catalyst was present and no comparable WHV could be defined (the weight hourly velocity of the oil was 1.1 kg/kg SiC/h in experiments 1 and 2).
bgas rate in normal litres gas per kg oil.
cTAN in mg KOH/g oil.
dnot detectable; liquid effluent did not have a smell of hydrogen sulphide.
enot detectable; liquid effluent had a smell of hydrogen sulphide.
fsyngas composition: 33.2 vol % hydrogen; 20.7 vol % CO; balance nitrogen.
| Number | Date | Country | Kind |
|---|---|---|---|
| 05075793.9 | Apr 2005 | EP | regional |
