Process for the removal of sulfur compounds from hydrocarbon feedstocks
The invention is directed to a process for the removal of contaminating sulfur compounds, more in particular thiophenic sulfur compounds, from hydrocarbon feedstocks, said process comprising contacting the feedstock in the presence of hydrogen with a sulfided nickel adsorbent, of which adsorbent the rate constant for tetralin hydrogenation activity at 150° C. is less than 0.01 l/s.g cat and wherein in said adsorbent part of the nickel is present in the metallic form.
1. A process for removing a contaminating sulfur compound from a hydrocarbon feedstock, comprising:
deactivating a surface of a nickel adsorbent with S, a polysulfide or a S-compound to form a sulfided nickel adsorbent;
contacting the hydrocarbon feedstock with the sulfided nickel adsorbent in the presence of hydrogen,
removing the contaminating sulfur compound from the hydrocarbon feedstock,
wherein the sulfided nickel adsorbent has a hydrogen adsorption capacity of less than or equal to 10 micromoles/g cat,
wherein an adsorbent part of the sulfided nickel adsorbent comprises at least 10%, on an atomic basis of metallic Ni, and
wherein a surface of the sulfided nickel adsorbent has an atomic S to Ni ratio of at least 0.5.
2. The process according to claim 1 , wherein the nickel adsorbent further comprises a metal oxide that forms a stable sulfide.
3. The process according to claim 1 , wherein the deactivating further comprises
precipitating the S, the polysulfide or the S-compound on the surface of the nickel adsorbent;
coprecipitating the S, the polysulfide or the S-compound with nickel adsorbent precursors, or
impregnating the nickel adsorbent with the S, the polysulfide or the S-compound.
4. The process according to claim 1 , wherein the
the deactivating further comprises deactivating the surface of the nickel adsorbent with the S-compound is selected from the group containing di-benzo-thiophene, 2-methyl thiophene, benzothiophene and dimethyl thiophene to form the sulfided nickel adsorbent.
5. The process according to claim 1 , wherein the sulfided nickel adsorbent further comprises silica.
6. The process according to claim 1 , wherein the sulfided nickel adsorbent is a calcined, reduced coprecipitant of the sulfided nickel adsorbent and silica.
7. The process according to claim 1 , wherein the process is carried out in a fixed bed or slurry phase.
8. The process according to claim 1 , wherein the process is conducted at a hydrogen partial pressure from 0.1 to 200 bar.
9. The process according to claim 1 , wherein the process is conducted at a hydrogen partial pressure from 10 to 75 bar.
10. The process according to claim 1 , wherein the process is conducted at a hydrogen partial pressure from 30 to 50 bar.
11. The process according to claim 1 , wherein the process is conducted at a temperature from 50 to 300 degrees C.
12. The process according to claim 1 , wherein the process is conducted at a temperature from 100 to 200 degrees C.
13. The process according to claim 1 , wherein the process is carried out with an LHSV from 0.1 to 10 hr −1 .
14. The process according to claim 13 , wherein the process is carried out with a GHSV between from 50 to 500 hr- 1 .
15. The process according to claim 1 , wherein the deactivating further comprises reducing the nickel adsorbent with hydrogen.
16. The process according to claim 15 , wherein the reducing the nickel adsorbent is conducted with the hydrogen at a temperature from 100 to 200 degrees C.
17. The process according to claim 1 , wherein the deactivating is conducted at a temperature from 100 to 500 degrees C.
18. The process according to claim 1 wherein the nickel adsorbent contains a structural promoter.
19. The process of claim 2 , wherein the nickel adsorbent is on a support.
20. The process according to claim 1 , wherein the deactivating further comprises deactivating the surface of the nickel adsorbent with aromatic sulfur compound.
21. The process according to claim 1 , wherein the contaminating sulfur compound comprises a thiophenic sulfur compound.
22. The process according to claim 21 , wherein the sulfided nickel adsorbent has a rate constant for tetralin hydrogenation activity at 150° C. of less than 0.01l/s.g cat.
23. The process according to claim 1 , wherein the removing further comprises removing substantially all of the contaminating sulfur compound from the hydrocarbon feedstock without removing hydrocarbon from the hydrocarbon feedstock.