초록 ▼

A process for reducing the naphthenic acidity of petroleum oils, or their liquid fractions, is described, the process comprising a thermal treatment of the petroleum oils, or their liquid fractions, in the presence of an adsorbent the surface of which is covered by high molecular weight carbon compo

A process for reducing the naphthenic acidity of petroleum oils, or their liquid fractions, is described, the process comprising a thermal treatment of the petroleum oils, or their liquid fractions, in the presence of an adsorbent the surface of which is covered by high molecular weight carbon compounds. Preferred adsorbents are the spent or coked FCC catalysts.

대표청구항 ▼

What is claimed is: 1. A method for reducing a naphthenic acidity of a feedstock of petroleum oils or of their liquid fractions, the method comprising the steps of: feeding the feedstock to a reactor; contacting, in the reactor, the feedstock with an adsorbent to cause a reduction of the napthenic

What is claimed is: 1. A method for reducing a naphthenic acidity of a feedstock of petroleum oils or of their liquid fractions, the method comprising the steps of: feeding the feedstock to a reactor; contacting, in the reactor, the feedstock with an adsorbent to cause a reduction of the napthenic acidity of the feedstock, wherein the adsorbent comprises a spent or coked FCC catalyst having a surface area of 60 to 250 m2/g, wherein a ratio of adsorbent to feedstock ranges from 0.1 to 5, wherein the reactor has a temperature between 200�� C. and 500�� C. and a pressure of 0.01 to 0.3 MPag, wherein the reactor has a residence time of between 1 second and 2 hours, wherein an effluent exiting the reactor comprises a treated feedstock with a reduced naphthenic acidity and the adsorbent, and wherein the reduction of the napthenic acidity of the feedstock occurs substantially by thermal treatment; and separating, in a liquid/solid separation system, the treated feedstock from the adsorbent. 2. The method of claim 1, wherein the reduction of the napthenic acidity of the feedstock does not occur as a result of either contacting the feedstock with an alkali aqueous solution or a reaction in the presence of hydrogen. 3. The method of claim 1, wherein the reactor has a temperature between 250�� C. and 350�� C. 4. The method of claim 1, wherein the feedstock has a water content of less than 0.1% by weight. 5. The method of claim 1, wherein the surface area of the adsorbent is from 100 to 200 m2/g. 6. The method of claim 1 further comprising the steps of: treating the adsorbent with an alkaline solution prior to the step of contacting the feedstock with the adsorbent, wherein the concentration of an alkaline base of the alkaline solution is in the range of from 5 to 15% by weight, and wherein a mass ratio of alkaline base to mass of the adsorbent is from 0.05 to 0.5; and drying the adsorbent through exposure to a temperature between 100 and 120�� C. for 10 to 16 hours. 7. The method of claim 6, wherein the alkaline base comprises a metal hydroxide of group IA. 8. The method of claim 6, wherein the alkaline base comprises a metal hydroxide of group IIA. 9. The method of claim 6, wherein the alkaline base comprises ammonium hydroxide. 10. The method of claim 6, wherein the alkaline base is selected from the group consisting of a metal hydroxide of group IA, a metal hydroxide of group IIA, ammonium hydroxide, and a mixture thereof. 11. The method of claim 1, wherein the liquid/solid separation system is selected from the group consisting of a cyclone, a hydrocyclone, and a centrifuge.