# US 10,865,167 B2 · Hydrocracking process

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- Number: US 10,865,167 B2
- Document ID: US10865167B2
- Status: Granted
- Kind: B2
- Application number: 16/331,828
- Filed: 2017-09-07
- Published: 2019-12-12
- Granted: 2020-12-15
- Earliest claimed: 2016-09-12
- Assignees: Sabic Global Technologies B.V.
- Applicants: Sabic Global Technologies B.V.
- Inventors: Ashim Kumar Ghosh; Alla Khanmamedova; Scott A. Stevenson; Luis Aramburo; David L. Sullivan; Cong Nguyen
- Web page: https://patentgrep.com/patent/US10865167B2

## CPC

- C07C 4/06: Catalytic processes {(C07C4/025 takes precedence)}
- C10G 45/62: containing platinum group metals or compounds thereof
- B01J 23/42: Platinum
- B01J 29/22: Noble metals
- B01J 29/44: Noble metals
- B01J 29/74: Noble metals
- B01J 35/394: {Metal dispersion value, e.g. percentage or fraction}
- B01J 35/643: {less than 2 nm}
- B01J 35/647: {2-50 nm}
- C10G 35/095: containing crystalline alumino-silicates, e.g. molecular sieves {(C10G35/065 takes precedence)}
- C10G 45/70: with catalysts containing platinum group metals or compounds thereof
- C10G 47/18: the catalyst containing platinum group metals or compounds thereof
- B01J 2229/186: not in framework positions
- C07C 2521/12: Silica and alumina
- C07C 2523/10: of rare earths
- C07C 2523/42: Platinum
- C07C 2523/44: Palladium
- C07C 2529/18: of the mordenite type
- C07C 2529/40: of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
- C07C 2529/44: Noble metals
- C10G 2300/104: Light gasoline having a boiling range of about 20 - 100 °C
- C10G 2300/1044: Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
- C10G 2300/301: Boiling range
- C10G 2400/28: Propane and butane
- C10G 2400/30: Aromatics
- C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

## Abstract

A process for hydrocracking 2,4-dimethylpentane and/or 2,2,3-trimethylbutane can comprise: contacting a hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst, wherein the hydrocracking feed stream comprises at least 0.5 wt % of 2,4-dimethylpentane and/or 2,2,3-trimethylbutane, based upon a total weight of the hydrocracking feed stream; and wherein the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75; preferably the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75 and a large pore zeolite having a pore size of 6-8 A and a silica to alumina molar ratio of 10-80, wherein the hydrogenation metal is deposited on the medium pore zeolite and the large pore zeolite.

## Claims

### Claim 1

A process of hydrocracking at least one of 2,4-dimethylpentane and 2,2,3-trimethylbutane, comprising:
contacting a hydrocracking feed stream comprising C5-C12 hydrocarbons in the presence of hydrogen with a hydrocracking catalyst under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-30 to produce a hydrocracking product stream comprising LPG;
wherein the hydrocracking feed stream comprises at least 0.5 wt % of 2,4-dimethylpentane and/or 2,2,3-trimethylbutane, based upon a total weight of the hydrocracking feed stream; and
wherein the hydrocracking catalyst comprises a hydrogenation metal in an amount of 0.010-0.30 wt % with respect to the total catalyst; and
wherein the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 Å and a silica to alumina molar ratio of 20-75.

### Claim 2 (depends on 1)

The process according to claim 1, wherein the total amount of 2,4-dimethylpentane and 2,2,3-trimethylbutane in the hydrocracking feed stream is at least 1.0 wt %.

### Claim 3 (depends on 1)

The process according to claim 1, wherein the hydrocracking catalyst comprises 0.08 to 0.25 wt % hydrogenation metal, 15 wt % to 25 wt % alumina, and a balance being the medium pore zeolite.

### Claim 4 (depends on 1)

The process according to claim 1, wherein the hydrocracking catalyst is in the form of powder and is free from a binder.

### Claim 5 (depends on 1)

The process according to claim 1, wherein the silica to alumina molar ratio of the medium pore zeolite is in the range of 20-50.

### Claim 6 (depends on 5)

The process according to claim 5, wherein the silica to alumina molar ratio of the medium pore zeolite is in the range of 20 to 30.

### Claim 7 (depends on 6)

The process according to claim 6, wherein the silica to alumina molar ratio of the medium pore zeolite is in the range of 21 to 29.

### Claim 8 (depends on 1)

The process according to claim 1, wherein a conversion of any 2,4-dimethylpentane is greater than or equal to 90%; and the conversion of any 2,2,3-trimethylbutane is greater than or equal to 90%.

### Claim 9 (depends on 1)

The process according to claim 1, wherein the hydrocracking catalyst comprises at least 0.030 wt %, of the hydrogenating metal in relation to the total weight of the catalyst.

### Claim 10 (depends on 1)

The process according to claim 1, wherein the hydrocracking catalyst comprises La and/or Ga.

### Claim 11 (depends on 1)

The process according to claim 1, wherein the process comprises separating BTX or benzene from the hydrocracking product stream.

### Claim 12 (depends on 1)

The process according to claim 1, wherein greater than or equal to 95% of the C5-C12 hydrocarbons are cracked.

### Claim 13 (depends on 1)

The process according to claim 1, wherein the hydrogenating metal is at least one element selected from palladium and platinum.

### Claim 14 (depends on 1)

The process according to claim 1, wherein the hydrocracking feed stream comprises benzene.

### Claim 15 (depends on 1)

The process according to claim 1, wherein the hydrocracking product stream comprises a greater amount of benzene compared to the hydrocracking feed stream.

### Claim 16

A process of hydrocracking at least one of 2,4-dimethylpentane and 2,2,3-trimethylbutane, comprising:
contacting a hydrocracking feed stream comprising C5-C12 hydrocarbons in the presence of hydrogen with a hydrocracking catalyst under process conditions including a temperature of 425-580° C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-30 to produce a hydrocracking product stream;
wherein the hydrocracking feed stream comprises at least 0.5 wt % of 2,4-dimethylpentane and/or 2,2,3-trimethylbutane, based upon a total weight of the hydrocracking feed stream;
wherein the hydrocracking catalyst comprises a hydrogenation metal in an amount of 0.01-0.30 wt % with respect to the total catalyst; and
wherein the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 Å and a silica to alumina molar ratio of 20-75 and a large pore zeolite having a pore size of 6-8 Å and a silica to alumina molar ratio of 10-80, wherein the hydrogenation metal is deposited on the medium pore zeolite and the large pore zeolite.

### Claim 17 (depends on 16)

The process according to claim 16, wherein the zeolite in the hydrocracking catalyst comprises 75-95 wt % of the medium pore zeolite and 5-25 wt % of the large pore zeolite with respect to the total amount of the zeolite.

### Claim 18 (depends on 16)

The process according to claim 16, wherein the hydrocracking catalyst has a deactivation rate of less than |−3.5×10−4 per hour|.

### Claim 19 (depends on 16)

The process according to claim 16, wherein the medium pore zeolite comprises a ZSM-5.

### Claim 20 (depends on 16)

The process according to claim 16, wherein the large pore zeolite comprises a mordenite.