Two-phase moving bed reactor utilizing hydrogen-enriched feed

Patent metadata

Field	Value
Publication number	US-11084991-B2
Application number	US-202016863653-A
Country	US
Kind code	B2
Filing date	Apr 30, 2020
Priority date	Jun 25, 2019
Publication date	Aug 10, 2021
Grant date	Aug 10, 2021

Abstract

A process for conversion of a liquid hydrocarbon feedstock in a moving bed hydroprocessing reactor is provided in which (a) hydrogen gas is dissolved in the liquid feedstock and (b) the mixture is flashed to remove and recover any light components, leaving a hydrogen-enriched feedstock. A homogeneous and/or heterogeneous catalyst is added to the feedstock upstream of the moving bed hydroprocessing rector.

First claim

The invention claimed is:

1. A process for converting a liquid hydrocarbon feedstock into lower molecular weight hydrocarbon compounds in a moving bed reactor, the process comprising:
a. mixing the liquid hydrocarbon feedstock and an excess of hydrogen gas in a mixing zone under predetermined conditions of temperature and hydrogen partial pressure to dissolve a portion of the hydrogen gas in the liquid hydrocarbon feedstock and produce a mixture of hydrogen-enriched liquid hydrocarbon feedstock and undissolved hydrogen gas;
b. introducing the mixture produced in step (a) into a flashing zone to separate the undissolved hydrogen gas and any light hydrocarbon components present from the hydrogen-enriched hydrocarbon feedstock, the flashing zone being operated under predetermined conditions of temperature and pressure corresponding to those in a downstream reaction zone, and recovering the hydrogen-enriched liquid hydrocarbon feedstock;
c. introducing the hydrogen-enriched liquid hydrocarbon feedstock into the reaction zone of at least one moving bed reactor containing at least one catalyst or catalyst precursor under reaction conditions that are predetermined containing respect to the hydrocarbon feedstock, and reacting the feedstock and hydrogen exothermally to convert at least a portion of the feedstock into lower boiling hydrocarbons;
d. recovering a reactor effluent from the at least one moving bed reactor comprising converted hydrocarbon products and unconverted liquid feedstock;
e. introducing the reactor effluent from the at least one moving bed reactor into a separation zone to separate converted hydrocarbon products from unconverted liquid feedstock;
f. recovering the converted hydrocarbon products from the separation zone; and
g. recovering the unconverted liquid feedstock from the separation zone.

2. The process of claim 1 in which at least a portion of the unconverted liquid feedstock recovered from the separation zone is recycled to the reaction zone to form a portion of the hydrogen-enriched liquid hydrocarbon feedstock.

3. The process of claim 2 in which the unconverted liquid feedstock is analyzed to confirm the presence of a predetermined minimum concentration of dissolved hydrogen prior to being recycled to the reaction zone.

4. The process of claim 2 in which hydrogen is added to the unconverted recycle liquid feedstock prior to its reintroduction into the reaction zone.

5. The process of claim 1 in which the hydrogen is added to saturate the liquid feedstock entering the reaction zone.

6. The process of claim 1 in which the at least one catalyst is a solid heterogeneous catalyst having an average particle size ranging from 0.6 mm to 2.5 mm.

7. The process of claim 1 in which an oil soluble homogeneous catalyst is added to the liquid hydrocarbon feedstock.

8. The process of claim 1 in which fresh oil soluble homogeneous liquid catalyst is added to the unconverted liquid feedstock upstream of one or more of the at least one reactors.

9. The process of claim 1 in which the reaction zone includes a plurality of moving bed reactors arranged in series, each reactor optionally preceded by a hydrogen mixing zone in which an excess of hydrogen is added to the recycled unconverted liquid effluent from an upstream reactor and a flashing zone to separate light components and undissolved hydrogen and passing an unconverted hydrogen-enriched liquid hydrocarbon feedstock to a downstream reactor.

10. The process of claim 9 in which the unconverted recycled liquid hydrocarbon feedstock is saturated with hydrogen.

11. The process of claim 8 in which a predetermined amount of fresh heterogeneous catalyst is added to the plurality of moving bed reactors during the processing of the hydrogen-enriched or saturated feedstock.

12. The process of claim 11 which is continuous and in which fresh catalyst is added to the plurality of reactors during the continuous operation of the process.

13. The process of claim 1 , wherein a portion of the catalyst is removed from the moving bed reactor with the unconverted liquid recycle stream and separated from the liquid recycle stream prior to further processing of the recycle stream.

14. The process of claim 1 , wherein the liquid hydrocarbon feedstock has a boiling point above 370° C.

15. The process of claim 12 , wherein the liquid hydrocarbon feedstock in step (a) comprises one or more of straight run distillates and other intermediate refinery streams as an additional source of hydrogen absorbing liquids.

16. The process of claim 1 , wherein the reaction zone comprises two or more moving bed reactors.

17. The process of claim 1 , wherein the converted hydrocarbon products are full range or narrow range products comprising naphtha, middle-distillates, gas oils or residues.

18. The process of claim 1 , wherein the at least one catalyst is selected from catalysts comprising at least one active metal from Periodic Table groups VI, VII and VIIIB, or IUPAC Groups 6-10, on a support of alumina, silica-alumina, silica, titania, magnesia or zeolites.

19. The process of claim 18 , wherein the at least one catalyst is selected from the group comprising cobalt, nickel, molybdenum and tungsten.

20. The process of claim 18 , wherein the at least one catalyst comprises active metals in the range of from 0.1W % to 30 W % based on the total weight of the catalyst.

Assignees

• Saudi Arabian Oil Co

Inventors

• Koseoglu Omer Refa

Classifications

• C10G67/02 Primary

  plural serial stages only · CPC title

• C10G47/28 Primary

  according to the "moving-bed" technique · CPC title

• C10G2300/202

  Heteroatoms content, i.e. S, N, O, P · CPC title

• C10G67/14 Primary

  including at least two different refining steps in the absence of hydrogen · CPC title

• C10G2300/308

  Gravity, density, e.g. API · CPC title