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Process to upgrade kerosenes and a gasoils from naphthenic and aromatic crude petroleum sources

a technology of naphthenic and aromatic crude petroleum and gasoil, which is applied in the direction of liquid carbonaceous fuels, lubricant compositions, fuels, etc., can solve the problems of unsuitable to meet certain environmentally driven fuel specifications, naphthalene levels are too high in kerosenes produced, and the middle distillate fuels produced from naphthenic or aromatic crudes may not be suitable to meet the strict environmental driven fuel specification requirements

Inactive Publication Date: 2007-01-25
SHELL OIL CO
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Benefits of technology

[0018] This object is achieved with the following process. Process to prepare a kerosene and a gasoil product from a crude petroleum source having a Watson characterisation factor K value of equal or below 12.0 by (a) isolation of a petroleum derived kerosene fraction and a petroleum derived gasoil fraction from said crude petroleum source, wherein the petroleum derived kerosene fraction has a smoke point of below 25 mm or below 19 mm if naphthalenes content of the kerosene fraction is below 3% vol and the p...

Problems solved by technology

However virgin kerosenes and virgin gasoils produced from Naphthenic and / or Aromatic crudes are being characterised by certain quality properties which makes them unsuitable to meet certain environmentally driven fuels specifications as required by an increasing number of legislators in various Regions and Markets.
Sometimes naphthalenes levels are too high in kerosenes produced from these crudes in case of high final boiling points of the kerosenes.
The consequence of these emission driven fuel requirements is that middle distillate fuels produced from naphthenic or aromatic crudes may not be suitable to meet the severe environmental driven fuels specification requirements being set for Avtur and Diesel.
This option may need however expensive investment for those refineries not equipped with these processing units.
A disadvantage of blending with paraffinic crudes is that such crudes are not always available at the refinery location or only at a much higher price.
Another disadvantage is, that it is not always possible to find a paraffinic crude to blend which will meet both kerosene and gas oil properties and volume demands of distillates to the qualities respectively quantities as specified.
Nevertheless, as explained above, when optimizing both kerosene and gas oil products in a refinery blending environment such quality give-away cannot always be avoided.

Method used

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Examples

Experimental program
Comparison scheme
Effect test

example 1

[0034] A naphthenic crude having a UOPK value of 11.5 is distilled into a naphtha fraction, a kerosene fraction and a gas oil fraction. The properties of the different fractions are listed in Table 1.

TABLE 1Distillates properties of a typical Naphthenic crudeKeroseneGas oilYield on12.236.9naphthenic crude(% woc)Initial boiling165235point (° C.)Final boiling235350point (° C.)Density840887(spec 3Diesel EN 590)Smoke point18—(spec >25 mm)Aromatics (% vol)2143Sulphur (% wt)0.020.07Cetane number3338.5(spec >51

example 2

[0035] Example 1 is repeated. In addition an paraffinic crude having a Watson K characterisation factor value of 12.3 was distilled to obtain blending components to improve the kerosene and gas oil properties of the fractions listed in Table 1. The amount of paraffinic crude that was used was enough to obtain a kerosene and gas oil mixture to adjust the respective fraction of Table 1 to meet the desired specification. The properties of the blends are reported in Table 2.

TABLE 2Distillates properties of Paraffinic andNaphthenic crudes and blendCrude BlendNaphthenicParaffinic(31 / 69 % w / wcrudecrudeN / P)KeroGasoilKeroGasoilKeroGasoilYield on12.236.917.128.615.531.3paraffiniccrude (% woc)Initial165235165235165235boilingpoint (° C.)Final235350235350235350boilingpoint (° C.)Density8408877908260.8060.845(kg / m3)(spec kg / m3 DieselEN 590)Smoke point18—26—24(spec>19 mm)Aromatics214316141724(% vol)Sulphur0.020.070.010.040.010.05(% wt)Cetane3338.55262.84755number(spec >51

[0036] As can be seen fr...

example 3

[0037] Example 1 is repeated. To the kerosene and gas oil fractions of Table 1 an amount of Fischer-Tropsch kerosene and gas oil (having the properties as listed in Table 3) respectively is added in an amount sufficient to meet the smoke point and cetane number specifications. The resulting properties are listed in Table 4.

TABLE 3FT Distillates propertiesFischer-TropschFischer-Tropschderived kerosenederived Gas oilInitial boiling150200point (° C.)Final boiling200345point (° C.)Density (kg / m3)738775Smoke point (mm)>50—Cetane number6076Sulphur (ppmwt)detection limits)detection limits)Aromatics (% vol)

[0038]

TABLE 4Blends of FT distillates with Naphthenic crude distillatesGasoilKeroseneKeroseneGasoilBlendfromBlendfromwithNaphthenicwith FTNapthenicFT GascrudekerosenecrudeoilFraction of05034Fischer-Tropschderivedcomponents inblend (% wt)Initial boiling165162235220point (° C.)Final boiling235230350348point (° C.)Density kg / m3840834887845(spec 3EU 590 Diesel)Smoke point mm1819.6——(spec >1...

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PUM

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Abstract

A process to prepare a kerosene and a gasoil product from a crude petroleum source having a Watson characterization factor K value of equal or below 12.0 by (a) isolation of a petroleum derived kerosene fraction and a petroleum derived gasoil fraction from said crude petroleum source, wherein the petroleum derived kerosene fraction has a smoke point of below 25 mm or below 19 mm if naphthalenes content of the kerosene fraction is below 3% vol and the petroleum derived gas oil has a cetane number of below 50 or a density higher than 845 kg / m3, ( ) adding a Fischer-Tropsch derived kerosene fraction to the petroleum derived kerosene fraction in an amount sufficient to obtain a mixture having a smoke point value of above 25 mm or above 19 mm if the naphthalenes content of the mixture is below 3% vol and (c) adding a Fischer-Tropsch derived gas oil fraction to the petroleum derived gasoil fraction such that the resultant mixture has a cetane number value of above 51.

Description

FIELD OF INVENTION [0001] Process to upgrade low quality kerosenes and gasoils from Naphthenic and Aromatic crude petroleum sources, featuring a value for the Watson characterisation factor K of equal of below 12. BACKGROUND OF INVENTION [0002] Crude petroleum sources featuring a value for the Watson characterisation factor K of in between 11 and 12 are also referred to as “naphthenic” crude. If the K factor below 11 the crude is also referred to as “aromatic” crude. The Watson characterisation factor K for hydrocarbons has been defined in the API technical data book (Section 2 Characterisation). [0003] Virgin naphtha fractions as distilled from Napthenic or Aromatic crudes are very suitable to prepare high octane motor gasoline components as they are easy convertable via Catalytic Reforming to high octane value reformates. However virgin kerosenes and virgin gasoils produced from Naphthenic and / or Aromatic crudes are being characterised by certain quality properties which makes the...

Claims

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Application Information

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IPC IPC(8): C10L1/16C10L1/04C10L1/08
CPCC10L1/08C10L1/04
Inventor BOSCH, WILLEM
Owner SHELL OIL CO
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