# US 2010/0163458 A1 · Method of converting effluents of renewable origin into fuel of excellent quality by using a molybdenum-based catalyst

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- Number: US 2010/0163458 A1
- Document ID: US20100163458A1
- Status: Published application
- Kind: A1
- Application number: 12/644,710
- Filed: 2009-12-22
- Published: 2010-07-01
- Earliest claimed: 2008-12-23
- Assignees: IPF, Inc.
- Inventors: Antoine DAUDIN; Laurent Bournay; Thierry Chapus
- Web page: https://patentgrep.com/patent/US20100163458A1

## CPC

- B01J 23/28: Molybdenum
- B01J 27/051: Molybdenum
- B01J 27/19: Molybdenum
- B01J 29/74: Noble metals
- C10G 3/44: {characterised by the catalyst used}
- C10G 3/48: {further characterised by the catalyst support}
- C10G 3/50: {in the presence of hydrogen, hydrogen donors or hydrogen generating compounds}
- C10G 3/54: {characterised by the catalytic bed}
- B01J 27/0515: {with iron group metals or platinum group metals}
- C10G 2300/1014: of vegetal origin
- C10G 2300/1018: of animal origin
- C10G 2300/202: Heteroatoms content, i.e. S, N, O, P
- C10G 2300/4018: Spatial velocity, e.g. LHSV, WHSV
- C10G 2400/04: Diesel oil
- C10G 2400/08: Jet fuel
- Y02P 30/20: using bio-feedstock
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- 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
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

## Abstract

The invention is concerned with a supported or unsupported catalyst comprising an active phase constituted by a sulfur-containing group VIB element, the group VIB element being molybdenum, and a hydrodeoxygenation process with a yield of hydrodeoxygenation product which is greater than or equal to 90% of charges from renewable sources using a catalyst according to the invention.

## Claims

### Claim 1

A supported or unsupported catalyst comprising an active phase constituted by a sulfur-containing group VIB element, the group VIB element being molybdenum, said catalyst in the case of a supported catalyst having a group VIB element content of between 17 and 35% by weight of oxide of said group VIB element in relation to the total mass of the catalyst and also comprising a doping element selected from phosphorus, boron and silicon deposited on said support.

### Claim 2 (depends on 1)

A catalyst according to claim 1, in which said catalyst comprises an amorphous inorganic support selected from the group formed by alumina, silica, silica-aluminas, magnesia, clays and mixtures of at least two of those minerals.

### Claim 3 (depends on 2)

A catalyst according to claim 2, in which said catalyst comprises an alumina amorphous inorganic support.

### Claim 4 (depends on 1, 2, 3)

A catalyst according to one of claims 1 to 3, in which said catalyst comprises an amorphous inorganic support constituted by alumina alone.

### Claim 5 (depends on 1, 2, 3, 4)

A catalyst according to one of claims 1 to 4, in which said catalyst contains a phosphorus content which is strictly above 0.5% and below 8% by weight of P2O5 oxide in relation to the total mass of the catalyst.

### Claim 6 (depends on 1, 2, 3, 4, 5)

A process for the hydrodeoxygenation of charges from renewable sources with a hydrodeoxygenation product yield which is more than or equal to 90%, using a catalyst according to one of claims 1 to 5, at a temperature of between 120 and 450° C., at a pressure of between 1 MPa and 10 MPa, at an hourly space velocity of between 0.1 h−1 and 10 h−1 and in the presence of a total amount of hydrogen mixed with the charge such that the hydrogen/charge ratio is between 50 and 3000 Nm3 of hydrogen per m3 of charge.

### Claim 7 (depends on 6)

A process according to claim 6, in which said yield of hydrodeoxygenation product is above 96%

### Claim 8 (depends on 6, 7)

A process according to one of claims 6 or 7, in which said process is carried out in fixed bed.

### Claim 9 (depends on 6, 7)

A process according to one of claims 6 or 7, in which said process is carried out in ebullating bed.

### Claim 10 (depends on 6, 7, 8, 9)

A process according to one of claims 6 to 9, in which the effluent resulting from hydrodeoxygenation undergoes at least one separation step, and, preferably, a gas/liquid separation step, and a separation step from water and from at least one liquid hydrocarbon base.

### Claim 11 (depends on 10)

A process according to claim 10, in which a step for eliminating nitrogenous compounds from said liquid hydrocarbon base is carried out after said optional step of separation from water.

### Claim 12 (depends on 6, 7, 8, 9, 10, 11)

A process according to one of claims 6 to 11, in which at least part of the liquid hydrocarbon base obtained at the end of the step for elimination of the nitrogenous organic compounds is hydroisomerised in the presence of a hydroisomerisation catalyst.

### Claim 13 (depends on 6, 7, 8, 9, 10, 11, 12)

A process according to one of claims 6 to 12, in which said hydroisomerisation catalyst comprises at least one group VIII metal and/or at least one group VIB metal as hydrodehydrogenating function and at least one amorphous inorganic support as hydroisomerising function.

### Claim 14 (depends on 6, 7, 8, 9, 10, 11, 12)

A process according to one of claims 6 to 12, in which said hydroisomerisation catalyst comprises an active metal phase constituted by platinum and a ZBM-30-based hydroisomerising function.