초록 ▼

This invention is directed to a method and apparatus for controlling and optimizing the feed of two or more oxidizers to an aqueous stream, thereby providing a synergistic effect. The system combines the use of amperometric or ORP based sensor technology with amperometric sensor technology employing

This invention is directed to a method and apparatus for controlling and optimizing the feed of two or more oxidizers to an aqueous stream, thereby providing a synergistic effect. The system combines the use of amperometric or ORP based sensor technology with amperometric sensor technology employing a gas permeable membrane, thereby providing definitive control of each oxidizer feed stream.

대표청구항 ▼

This invention is directed to a method and apparatus for controlling and optimizing the feed of two or more oxidizers to an aqueous stream, thereby providing a synergistic effect. The system combines the use of amperometric or ORP based sensor technology with amperometric sensor technology employing

This invention is directed to a method and apparatus for controlling and optimizing the feed of two or more oxidizers to an aqueous stream, thereby providing a synergistic effect. The system combines the use of amperometric or ORP based sensor technology with amperometric sensor technology employing a gas permeable membrane, thereby providing definitive control of each oxidizer feed stream. conducting the lubricating oil feedstock to a solvent extraction zone and separating therefrom an aromatics rich extract and a paraffins rich raffinate; (b) stripping the raffinate of solvent to produce a raffinate feed having a dewaxed oil viscosity index from about 80 to about 105 and a final boiling point of no greater than about 650° C.; (c) passing the raffinate feed to a first hydroconversion zone and processing the raffinate feed in the presence of a hydroconversion catalyst under hydroconversion conditions to produce a first hydroconverted raffinate; (d) passing the hydroconverted raffinate from the first hydroconversion zone to a second hydroconversion zone and processing the hydroconverted raffinate in the presence of a bulk metal catalyst under hydroconversion conditions wherein the bulk metal catalyst comprises a non-noble metal Group VIII molybdate in which at least a portion but less than all of the molybdenum is replaced by tungsten to produce a second hydroconverted raffinate; (e) passing the second hydroconverted raffinate to a hydrofinishing reaction zone and conducting cold hydrofinishing of the second hydroconverted raffinate in the presence of a hydrofinishing catalyst under cold hydrofinishing conditions wherein the bulk metal catalyst is represented by the formula: (X)b(Mo)c(W)dOz wherein X is a non-noble Group VIII metal, the molar ratio of b: (c+d) is 0.5/1 to 3/1, the molar ratio of c:d is >0.01/1, and z=[2b+6(c+d)]/2. 4. The process of claims 1 to 3 wherein the molar ratio of b:(c+d) is 0.75/1 to 1.5/1. 5. The process of claim 4 wherein the molar ratio of b:(c+d) is 0.75/1 to 1.25/1. 6. The process of claims 1 to 3 wherein the molar ratio of c:d is >0.1/1. 7. The process of claim 6 wherein the molar ratio of c:d is 1/10 to 10/1. 8. The process of claim 7 wherein the molar ratio of c:d is 1/3 to 3/1. 9. The process of claims 1, 2 or 3 wherein the hydroconversion conditions in the first hydroconversion zone include temperatures of from 300 to 420° C., hydrogen pressures of from 300 to 3000 psig (2170 to 20786 kPa), liquid hourly space velocities of from 0.1 to 10 and hydrogen treat gas rates of from 500 to 5000 scf/B (89 to 890 m3/m3). 10. The process of claim 2 wherein the hydroconversion conditions in the second hydroconversion zone include temperatures of from 300 to 420° C., hydrogen pressures of from 300 to 3000 psig (2170 to 20786 kPa), liquid hourly space velocities of from 0.1 to 10 and hydrogen treat gas rates of from 500 to 5000 scf/B (89 to 890 m3/m3). 11. The process of claim 3 wherein the hydroconversion conditions in the first hydroconversion zone include temperatures of from 300 to 420° C., hydrogen pressures of from 300 to 3000 psig (2170 to 20786 kPa), liquid hourly space velocities of from 0.1 to 10 and hydrogen treat gas rates of from 500 to 5000 scf/B (89 to 890 m3/m3). 12. The process of claims 1 to 3 wherein the cold hydrofinishing conditions include temperatures of from 250 to 360° C., hydrogen pressures of from 300 to 3000 psig (2170 to 20786 kPa), liquid hourly space velocities of from 0.1 to 10 and hydrogen treat gas rates of from 500 to 5000 scf/B (89 to 890 m3/m3). 13. The process of claim 2 wherein the hydroconversion catalyst in the second hydroconversion zone is the bulk metal catalyst of step (c). 14. The process of claim 2 wherein the hydroconversion catalyst in the second hydroconversion zone is a non-bulk metal hydrotreating catalyst containing at least one Group VIB and at least one Group VIII metal. 15. The process of claim 3 wherein the hydroconversion catalyst in the first hydrconversion zone is a non-bulk metal hydrotreating catalyst containing at least one Group VIB and at least one Group VIII metal. 16. The process of claims 14 or 15 wherein the Group VIB metal is molybdenum or tungsten and the Group VIII metal is a non