Syngas production and recovery of active phase metals from gasifier slag containing spent catalyst

Patent metadata

Field	Value
Publication number	US-11732204-B2
Application number	US-201916672837-A
Country	US
Kind code	B2
Filing date	Nov 4, 2019
Priority date	Nov 4, 2019
Publication date	Aug 22, 2023
Grant date	Aug 22, 2023

Abstract

An integrated refinery process for the disposal of metal-containing spent coked catalyst from hydrotreating and/or hydrocracking unit operations includes introducing the spent coked catalyst into a membrane wall gasification reactor in the form of flowable particles along with predetermined amounts of oxygen and steam based upon an analysis of the hydrocarbon content of the coke, and optionally, a liquid hydrocarbon; gasifying the feed to produce synthesis gas and a slag material; recovering and subjecting the slag material to further processes in preparation for a leaching step to solubilize and form one or more active phase metal compounds that are recovered from the leaching solution, either separately by sequential processing, or together. The recovered active metal compounds can be used, e.g., in preparing fresh catalyst for use in the refinery's hydroprocessing units.

First claim

The invention claimed is:

1. An integrated refinery process for the gasification of an active metal-containing spent coked catalyst for the production of synthesis gas and the recovery of active metal compounds, the process comprising:
a. providing an active metal-containing spent coked catalyst, containing one or more active phase metals from the periodic table IUPAC group 4-12 deposited on or otherwise incorporated in an amorphous and/or structured support, wherein the spent coked catalyst provided in step (a) is substantially free of vanadium and nickel porphyrin compounds and is derived from hydroprocessing of a feedstock that is a fraction of crude that does not contain contaminant metals vanadium and nickel that naturally occur in the crude oil, said feedstock selected from the group consisting of naphtha, diesel, vacuum gas oil that has been subjected to hydrodemetallization treatment prior to hydroprocessing, and vacuum residue that has been subjected to hydrodemetallization treatment prior to hydroprocessing;
b. grinding the spent coked catalyst to produce a free-flowing mass of ground spent catalyst particles;
c. mixing the ground spent catalyst particles with a fluid carrier stream to form a pressurized, fluidized spent catalyst particulate feedstream;
d. injecting the fluidized spent catalyst particulate feedstream into the combustion chamber of a cold-wall tubular membrane wall partial oxidation gasification reactor in the presence of a predetermined amount of oxygen and steam;
e. operating the gasification reactor at a temperature in the range of from 900° to 1700° C. and a pressure from 20 to 100 bars;
f. subjecting the fluidized spent catalyst particulate feedstream to partial oxidation to produce hydrogen and carbon monoxide from the spent coked catalyst, and a slag material comprising the remnants of the spent coked catalyst containing the active metal compounds;
g. recovering the hydrogen and carbon monoxide from the reactor in the form of a hot synthesis gas;
h. recovering the slag material from the reactor as a solid material;
i. preparing the slag material for leaching;
j. contacting the prepared slag material with an aqueous leaching solution to solubilize the one or more active phase metals in the leaching solution;
k. separating the leaching solution containing the one or more solubilized metal compounds from any remaining solid depleted slag material; and
l. recovering the one or more solubilized active phase metal compounds from the leaching solution.

2. The process of claim 1 , wherein the spent coked catalyst provided in step (a) is substantially free of any hydrocarbon oils derived from the feedstock, the method further comprising adjusting the amount of oxygen and steam as a function of a composition and amount of coke deposited on the spent catalyst.

3. The process of claim 1 , wherein the one or more active phase metals are selected from the group consisting of Ni, Co, Mo, W, Pt and Pd.

4. The process of claim 1 , wherein the one or more active phase metals recovered in step (l) is selected from the group consisting of cobalt, molybdenum, tungsten, nickel, platinum and palladium.

5. The process of claim 1 , where more than one metal or metal compound is present in the slag, and each metal compound is solubilized in the leaching solution separately.

6. The process of claim 1 , wherein the leaching solution is an acid leaching solution comprised of an acid is selected from the group consisting of sulfuric acid, sulfonic acid, nitric acid, hydrochloric acid, acetic acid, citric acid, and combinations thereof.

7. The process of claim 1 , wherein the leaching solution is a basic leaching solution comprised of a member of the group consisting of ammonium hydroxide, ammonium carbonate, ammonium persulfate and sodium hydroxide, and combinations thereof.

8. The process of claim 1 , wherein depleted slag material remains in the leaching solution following the recovery of the one or more metal compounds in step (l) and the depleted slag material is (a) recovered and treated to remove and/or neutralize any remaining leaching solution, and (b) dried to form a flowable particulate material for subsequent processing.

9. The process of claim 1 , wherein a hydrocarbon oil comprises the fluid carrier stream.

10. The process of claim 9 , wherein the hydrocarbon oil comprises a light petroleum fraction boiling in the range of 36-370° C.

11. The process of claim 9 , wherein the hydrocarbon oil comprises residual oil boiling above 370° C.

12. The process of claim 11 , wherein the spent coked catalyst is fluidized in at least a portion of the residual oil to form the feedstream to the membrane reactor.

13. The process of claim 11 , wherein the spent coked catalyst is mixed with the residual oil to form a uniform pumpable dispersion.

14. The process of claim 1 , wherein the ash forming content of the spent coked catalyst particles is from 2 W % to 99 W % of the particulate feedstream.

15. The process of claim 1 , wherein the fluid carrier stream is a gaseous feedstream.

16. The process of claim 15 , wherein the gaseous feedstream contains a predetermined stoichiometric amount of oxygen.

17. The process of claim 15 , wherein the gaseous feedstream is air.

18. The process of claim 1 , further comprising controlling the amount of spent catalyst particles and oxygen entering the reactor to provide a stochiometric balance for partial combustion based on the hydrocarbon content of the catalyst particles and, if present, any residual hydrocarbon oil.

19. The process of claim 1 , wherein the ratio of oxygen-to-carbon in the gasifier is from 0.5:1 to 10:1.

20. The process of claim 1 , wherein the ratio of oxygen-to-carbon is from about 1:1 to 2:1 by weight.

21. The process of claim 1 , wherein the ground spent catalyst particles range in size from those passing a 35 to a 65 Tyler mesh size screen.

22. The process of claim 1 , further comprising passing the hot synthesis gas to a water-cooled heat exchanger to cool the synthesis gas, recovering high pressure steam from the heat exchanger, introducing the high pressure steam into a turbine generator to produce electricity, and recovering the cooled synthesis gas containing hydrogen.

23. The process of claim 1 , in which the one or more active metal compounds recovered in step (k) are used to prepare fresh catalysts.

24. The process of claim 1 , in which the one or more metals recovered are used to form alloys.

Assignees

• Saudi Arabian Oil Co

Inventors

• Koseoglu Omer Refa

Classifications

• C10J3/84 Primary

  with means for removing dust or tar from the gas · CPC title

• B01D11/0288

  Applications, solvents · CPC title

• C01B3/12

  by reaction of water vapour with carbon monoxide · CPC title

• C10J3/463

  in stationary fluidised beds · CPC title

• C01B2203/0283

  containing a CO-shift step, i.e. a water gas shift step · CPC title