Catalysts and methods for distillate end point reduction

Patent metadata

Field	Value
Publication number	US-2019309231-A1
Application number	US-201916359099-A
Country	US
Kind code	A1
Filing date	Mar 20, 2019
Priority date	Apr 6, 2018
Publication date	Oct 10, 2019
Grant date	—

Abstract

Systems and methods are provided for reducing the end point of distillate fuel boiling range fractions while reducing or minimizing conversion of the distillate fuel to naphtha or light ends. To perform end point reduction, a distillate boiling range fraction is exposed to a conversion catalyst that has a total surface area of at least 200 m2/g, an average pore size of 12 Angstroms or more, and/or a low acidity, where the conversion catalyst includes a supported Group 8-10 metal, such as a supported Group 8-10 noble metal. Such a conversion catalyst can have improved activity for reducing end point of a distillate fuel fraction while reducing or minimizing conversion relative to 177° C. Performing end point reduction using such a catalyst can allow for increased yields of distillate fuel boiling range products by allowing increased amounts of heavy feed components to be included in the input to a distillate fuel processing train.

First claim

1 . A method for producing a distillate fuel boiling range product, comprising:
exposing a feedstock comprising a T5 distillation point of 149° C. or more and a T90 distillation point of 370° C. or more in the presence of a conversion catalyst under conversion conditions to form a converted effluent, the conversion catalyst comprising a surface area of 200 m 2 /g or more, an average pore size of 12 Angstroms or more, and an collidine adsorption of 300 μmol/g or less, the conversion catalyst further comprising 0.01 wt % to 5.0 wt % of a Group 8-10 noble metal supported on the conversion catalyst, wherein the conversion conditions are effective to form a converted effluent having a T95 distillation point of 360° C. or less.

2 . The method of claim 1 , wherein the conversion catalyst further comprises an average pore size of 25 Angstroms or more; or wherein the conversion catalyst further comprises an average pore size of 120 Angstroms or less; or a combination thereof.

3 . The method of claim 1 , wherein the conversion conditions are effective for conversion of 30 wt % or more of the feedstock relative to a conversion temperature of 177° C.

4 . The method of claim 1 , a) wherein the conversion catalyst comprises a surface area of 500 m 2 /g or more, b) wherein the conversion catalyst comprises an Alpha value of 20 or less, c) wherein the conversion catalyst comprises a Bronsted acid site density of 100 μmol/g or less, d) wherein the conversion catalyst comprises a Lewis acid site density of 150 μmol/g or less, e) a combination of two or more of a)-d), or f) a combination of three or more of a)-d).

5 . The method of claim 1 , wherein the conversion catalyst is substantially free of crystals having a zeolitic framework with a 10-member ring pore channel, a 12-member ring pore channel, or a combination thereof.

6 . The method of claim 1 , wherein the conversion catalyst is substantially free of crystals having a zeolitic framework.

7 . The method of claim 1 , wherein the conversion catalyst comprises 0.1 wt % to 10 wt % of crystals having a zeolitic framework.

8 . The method of claim 1 , wherein the conversion catalyst comprises a mesoporous material, a mesoporous organosilicate, or a combination thereof.

9 . The method of claim 1 , wherein the conversion catalyst comprises MCM-41.

10 . The method of claim 1 , wherein the Group 8-10 noble metal comprises Pt, Pd, or a combination thereof.

11 . The method of claim 1 , wherein the feedstock comprises at least a portion of a dewaxed effluent from exposure of a feed to a dewaxing catalyst.

12 . The method of claim 1 , wherein converting the feedstock comprises exposing the feedstock to a catalyst bed comprising the conversion catalyst and a dewaxing catalyst, the catalyst bed comprising a mixed bed of catalyst, a stacked bed of catalyst, or a combination thereof.

13 . The method of claim 12 , wherein the dewaxing catalyst comprises a zeolitic framework structure having a 1-D, 10-member ring pore channel as the largest pore channel.

14 . The method of claim 1 , wherein the feedstock comprises 100 wppm or less of sulfur, 50 wppm or less of nitrogen, or a combination thereof.

15 . The method of claim 1 , further comprising hydroprocessing a feed comprising a 650° F.+ (˜343° C.+) portion under first hydroprocessing conditions to form a hydroprocessed effluent; and
fractionating at least a portion of the hydroprocessed effluent to form a fuels boiling range fraction comprising the feedstock.

16 . A system for producing a distillate fuel boiling range product, comprising:
a hydrotreating reactor comprising a hydrotreating feed inlet, a hydrotreating effluent outlet, and at least one fixed catalyst bed comprising a hydrotreating catalyst; a separation stage having a first separation stage inlet and a second separation stage inlet, the first separation stage inlet being in fluid communication with the hydrotreating effluent outlet, the separation stage further comprising a plurality of separation stage liquid effluent outlets, one or more of the separation stage liquid effluent outlets corresponding to product outlets; and a conversion reactor comprising a conversion feed inlet, a converted effluent outlet, and at least one fixed catalyst bed comprising a conversion catalyst, the conversion feed inlet being in fluid communication with at least one separation stage liquid effluent outlet, and the conversion catalyst comprising a surface area of 200 m 2 /g or more, a collidine adsorption of 300 μmol/g or less, and an effective pore size of 12 Angstroms or more, the conversion catalyst further comprising 0.01 wt % to 5.0 wt % of a Group 8-10 noble metal supported on the conversion catalyst.

17 . The system of claim 16 , wherein the conversion reactor further comprises a fixed bed comprising a dewaxing catalyst; wherein the conversion reactor further comprises a fixed bed comprising a hydrofinishing catalyst; or a combination thereof.

18 . The system of claim 16 , a) wherein the conversion catalyst comprises a surface area of 500 m 2 /g or more, b) wherein the conversion catalyst comprises an Alpha value of 20 or less, c) wherein the conversion catalyst comprises a Bronsted acid site density of 100 μmol/g or less, d) wherein the conversion catalyst comprises a Lewis acid site density of 150 μmol/g or less, e) a combination of two or more of a)-d), or f) a combination of three or more of a)-d).

19 . The system of claim 16 , wherein the conversion catalyst is substantially free of crystals having a zeolitic framework; or wherein the conversion catalyst comprises 0.1 wt % to 10 wt % of crystals having a zeolitic framework.

20 . The system of claim 16 , a) wherein the conversion catalyst comprises a mesoporous material, a mesoporous organosilicate, MCM-41, or a combination thereof; b) wherein the Group 8-10 noble metal comprises Pt, Pd, or a combination thereof; or c) a combination of a) and b).

Assignees

• Exxonmobil Res & Eng Co

Inventors

• O'Neill Brandon J
• Yohe Sara L
• Dandekar Ajit B

Classifications

• C10G45/52

  containing platinum group metals or compounds thereof · CPC title

• C10G65/043

  at least one step being a change in the structural skeleton · CPC title

• C10G45/08

  in combination with chromium, molybdenum, or tungsten metals, or compounds thereof · CPC title

• C10G65/12

  including cracking steps and other hydrotreatment steps · CPC title

• C10G65/08

  at least one step being a hydrogenation of the aromatic hydrocarbons · CPC title