Catalytic stripping process

Abstract

This development proposed adding a catalyst to an oxygen stripper. The oxygen stripper would be run at a temperature just below or at coking temp. The oxygen stripper includes a catalyst containing Group VI or VII metals to remove free radicals. Most preferably, the catalyst is a nickel-molybdenum catalyst.

Claims

1. A process for stripping oxygen and saturating free radicals contained in a diesel stream comprising: passing the diesel stream to a reactor containing a catalyst comprised of groups VI or VII metals; passing a hydrogen gas stream containing hydrogen gas into the reactor to create a countercurrent flow with the diesel stream; contacting a portion of the hydrogen gas with the diesel stream, the oxygen being stripped by the portion of the hydrogen gas; reacting another portion of the hydrogen gas with the free radicals via the catalyst, the free radicals being saturated thereby and rendered unreactive; and removing the stripped oxygen and hydrogen gas stream from the reactor.

2. A process according to claim 1 wherein the catalyst includes nickel-molybdenum.

3. A process according to claim 1 wherein the catalyst includes cobalt molybdenum.

4. A process according to claim 1 wherein the diesel stream is a high sulfur diesel.

5. A process according to claim 1 wherein the diesel stream is a low sulfur diesel.

6. A process according to claim 1 wherein the diesel stream is an ultra low sulfur diesel.

7. A process according to claim 1 wherein the catalyst includes palladium.

8. A process according to claim 1 wherein the catalyst includes any combination of nickel, cobalt, and molybdenum.

9. A process according to claim 1 wherein the catalyst includes platinum.

10. A process according to claim 1, further comprising: removing the diesel stream from the reactor after the diesel stream is deoxygenated and its free radicals are rendered unreactive, and passing the diesel stream removed from the reactor to a hydrotreating unit.

11. A process according to claim 1, further comprising: removing the diesel stream from the reactor after the diesel stream is deoxygenated and its free radicals are rendered unreactive, passing the diesel stream removed from the reactor through a heat exchanger and passing the diesel stream from the heat exchanger to a hydrotreating unit.

12. A process according to claim 1 further comprising: heating the hydrogen gas stream prior to passing into the reactor to a temperature above that of the diesel stream.

13. A process according to claim 12 wherein the contacting the portion of the hydrogen gas with the diesel stream increases the temperature of the diesel stream.

14. A process according to claim 1 wherein the contacting the portion of the hydrogen gas with the diesel stream increases the temperature of the diesel stream.

15. A process according to claim 1 wherein the contacting the portion of the hydrogen gas with the diesel stream occurs prior to the reacting another portion of the hydrogen gas with the free radicals via the catalyst.

16. A process for stripping oxygen and saturating free radicals contained in an ultra-low sulfur diesel stream comprising: passing the ultra-low sulfur diesel stream to a reactor containing a catalyst comprised of groups VI or VII metals; passing a hydrogen gas stream containing hydrogen gas into the reactor to create a countercurrent flow with the ultra-low sulfur diesel stream; contacting a portion of the hydrogen gas with the ultra-low sulfur diesel stream, the oxygen being stripped by the portion of the hydrogen gas; reacting another portion of the hydrogen gas with the free radicals via the catalyst, the free radicals being saturated thereby and rendered unreactive; and removing the stripped oxygen and hydrogen gas stream from the reactor.

17. A process for stripping oxygen and saturating free radicals contained in a diesel stream that includes diesel with a sulfur content in excess of an ultra-low sulfur diesel content, the process comprising: passing the diesel stream to a reactor containing a catalyst comprised of groups VI or VII metals; passing a hydrogen gas stream containing hydrogen gas into the reactor to create a countercurrent flow with the diesel stream; contacting a portion of the hydrogen gas with the diesel stream, the oxygen being stripped by the portion of the hydrogen gas; reacting another portion of the hydrogen gas with the free radicals via the catalyst, the free radicals being saturated thereby and rendered unreactive; and removing the stripped oxygen and hydrogen gas stream from the reactor.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a schematic representation of one configuration of the apparatus according to this invention. A more common configuration is expected to compose of the stripper feeding a hydrotreating process directly without intermediate separation.

DETAILED DESCRIPTION OF THE INVENTION

(2) This invention adds a small amount of hydrogenation catalyst to an oxygen stripper. Either structured packing is used with a catalyst support or pelleted catalyst may be used, depending on the bed design. The hydrogenation catalyst can be provided in any form, such as extrudates, pellets, raschig rings and structured packing, as well as other commercially available types. It has been discovered that use of small amounts of hydrogenation catalyst is sufficient to remove enough oxygen from the hydrocarbon feed stream to keep the heat exchanger of the hydrotreaters clean and unfouled by polymerized free radicals.

(3) Feedstock, when received and/or just before feeding to a hydrotreater will be counter currently contacted with hot hydrogen (350 F. or less). The hydrogen contained in the catalyst contact strips oxygen from the feedstock, stopping further damage to the hydrotreater. The catalyst reacts the hydrogen with the free radicals to cap them and render them unreactive. Temperatures are kept low enough to use minimum energy, while only reacting with the most reactive free radical component of the feedstock. The operating temperatures are preferably less than 350 F.

(4) Referring now to FIG. 1, an oxygenated feedstock 12 is fed into a stripper unit 10 at a location proximate the top of the stripper unit 10. The feedstock flows downward through the stripper unit 10. Hot hydrogen gas 14 (generally 350 F. or less) is fed into the stripper unit 10, below the feedstock 12 entrance. The hydrogen gas 14 rises through the stripper unit 10, counter-currently to the flow of the feedstock 12. The hot hydrogen 14 contact strips oxygen from the feedstock 12 to create free radicals. The hydrogen gas carries the free radicals through the catalyst 16 to cap the free radicals and render them unreactive. The hydrogen gas exits the stripper 10 through exit 15. The deoxygenated feedstock 18 flows directly to a hydrotreating unit 20. As an alternative, the deoxygenated feedstock is sent directly to a reactor for fractionation. After processing, the hydrotreated products exit unit 20 via line 22.

(5) Catalyst 16 typically is, preferably, a catalyst containing Group VI or VII metals, such as platinum, molybdenum, tungsten, nickel or cobalt. More preferably, the catalyst is a nickel-molybdenum or cobalt-molybdenum catalyst. Catalyst 16 may require a catalyst support, such as a structured packing. The structured packing, preferably, is open mesh knitted stainless steel wire or a pelleted catalyst.

(6) The hydrocarbon feed stream 12 may vary widely. Typically, the stream 12 is a naphtha, kerosene, or diesel stream or components thereof such as a light cycle oil (LCO).

Example 1

(7) Oxygenated LCO is transported to and unloaded to a tank. This LCO may be processed by this invention prior to unloading to the tank and/or when routed to the LCO hydrotreater. The LCO is introduced to or near the top tray of a stripping column, and trickles down the stripper to the bottom where it is collected and pumped to either a storage tank or the hydrotreater. Hydrogen at 300 F. is introduced to the bottom of the stripper through a distribution device, just below a section of hydrotreating catalyst in sufficient quantity to saturate all or most of the free radicals in the LCO, rendering it polymerization free and/or significantly reduced with no oxygen to cause further damage. Hydrogen travels countercurrent to the oil up the column, heating the oil and stripping residual oxygen from the LCO.

Example 2

(8) Naphtha is transported by pipeline, picking up oxygen in breakout tanks as it travels. The naphtha is processed by this invention prior to being fed to the hydrotreater. The catalyst is applied to the bottom tray of the oxygen stripper. A steam heater is applied to heat the hydrogen to an estimated 250 F. Countercurrent stripping is used per the invention in capping of free radicals and significantly reducing fouling of the preheat exchangers of the hydrotreaters.

(9) The above detailed description of the present invention is given for explanatory purposes. It will be apparent to those skilled in the art that numerous changes and modifications can be made without departing from the scope of the invention. Accordingly, the whole of the foregoing description is to be construed in an illustrative and not a limitative sense, the scope of the invention being defined solely by the appended claims.