# US 8,784,645 B2 · Process for producing hydrocarbon oil

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- Number: US 8,784,645 B2
- Document ID: US8784645B2
- Status: Granted
- Kind: B2
- Application number: 13/119,333
- Filed: 2009-09-16
- Published: 2011-09-08
- Granted: 2014-07-22
- Earliest claimed: 2008-09-18
- Assignees: Jx Nippon Oil & Energy Corporation
- Applicants: Yasutoshi Iguchi; Tatsuo Hamamatsu; Hideki Ono; Akira Koyama; Hideshi Iki
- Inventors: Yasutoshi Iguchi; Tatsuo Hamamatsu; Hideki Ono; Akira Koyama; Hideshi Iki
- Web page: https://patentgrep.com/patent/US8784645B2

## CPC

- C10G 3/46: {in combination with chromium, molybdenum, tungsten metals or compounds thereof}
- C10G 3/49: {containing crystalline aluminosilicates, e.g. molecular sieves}
- C10G 3/50: {in the presence of hydrogen, hydrogen donors or hydrogen generating compounds}
- C10G 45/04: characterised by the catalyst used
- C10G 45/06: containing nickel or cobalt metal, or compounds thereof
- C10G 45/08: in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
- C10G 2300/1014: of vegetal origin
- C10G 2300/1018: of animal origin
- C10G 2300/202: Heteroatoms content, i.e. S, N, O, P
- C10G 2300/207: Acid gases, e.g. H2S, COS, SO2, HCN
- C10G 2300/4006: Temperature
- C10G 2300/4012: Pressure
- C10G 2300/4081: Recycling aspects
- C10G 2300/70: Catalyst aspects
- C10G 2400/02: Gasoline
- C10G 2400/04: Diesel oil
- C10G 2400/08: Jet fuel
- Y02P 30/20: using bio-feedstock
- 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 method for manufacturing a hydrocarbon oil of the present invention comprises a first step wherein a plurality of reaction zones filled with a specific catalyst is disposed in series and a feedstock oil containing an oxygen-containing hydrocarbon compound derived from an animal or vegetable oil is supplied and hydrotreated under the conditions of a hydrogen pressure of 1 MPa or more and 10 MPa or less in each of the reaction zones; and a second step wherein hydrogen, hydrogen sulfide, carbon dioxide and water are removed from a product to be treated obtained in the first step to obtain a hydrocarbon oil. Among the plurality of reaction zones, the inlet temperature of the reaction zone disposed on the most upstream side is 150° C. or more and 250° C. or less, the inlet temperature of the second most upstream reaction zone or below is equal to or higher than the condensation temperature of water, and the outlet temperature of the reaction zone disposed on the most downstream side is 260° C. or more and 360° C. or less. The feedstock oil comprises a recycled oil containing a specific amount of a part of the hydrocarbon oil obtained in the second step and a specific amount of a sulfur-containing hydrocarbon compound.

## Claims

### Claim 1

A method for manufacturing a hydrocarbon oil, comprising:
a first step wherein a plurality of reaction zones filled with a catalyst which contains a porous inorganic oxide comprising two or more elements selected from aluminum, silicon, zirconium, boron, titanium and magnesium and one or more metals selected from Group 6A and Group 8 elements of the periodic table supported on the porous inorganic oxide is disposed in series and a feedstock oil containing an oxygen-containing hydrocarbon compound derived from an animal or vegetable oil is supplied and hydrotreated under the conditions of a hydrogen pressure of 1 MPa or more and less than 10 MPa in each of the reaction zones, and a ratio of hydrogen to oil (hydrogen/oil ratio) in the range of 100 to 1500 NL/L; and
a second step wherein hydrogen, hydrogen sulfide, carbon dioxide and water are removed from a product to be treated obtained in the first step to obtain a hydrocarbon oil,
wherein, among the plurality of reaction zones, the inlet temperature of the reaction zone disposed on the most upstream side is 150° C. or more and 250° C. or less, the inlet temperature of the second most upstream reaction zone or below is equal to or higher than the condensation temperature of water, the outlet temperature of the reaction zone disposed on the most downstream side is 260° C. or more and 360° C. or less,
wherein if the number of the reaction zones in the first step is represented by n, where n is an integer of 2 or more, and the inlet temperature and the outlet temperature of the kth reaction zone from the most upstream side are re resented respectively by tk and Tk where k is an integer of 2 to n, the relation between the partial pressure PW (in MPa) of the water produced as a by-product and the temperature tk (in ° C.) at that time satisfies the conditions represented b the following formula:
PW <6.11 ×10^{7.5×tk÷(tk+237.3)}×10−4,
and wherein the feedstock oil contains: a recycled oil in which a part of the hydrocarbon oil obtained in the second step is recycled and supplied in an amount of 0.5- to 5-fold by mass to the oxygen-containing hydrocarbon compound contained in the feedstock oil; and 1 to 50 ppm by mass of a sulfur-containing hydrocarbon compound in terms of the sulfur atom to the oxygen-containing hydrocarbon compound contained in the feedstock oil, wherein the sulfur-containing hydrocarbon compound is at least one selected from a sulfide, a disulfide, a polysulfide, a thiol, a thiophene, a benzothiophene, a dibenzothiophene, and a derivative thereof.

### Claim 2 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, wherein in each of the plurality of reaction zones, the difference between the outlet temperature and the inlet temperature is 80° C. or less and the sum of the difference between the outlet temperature and the inlet temperature in each of the reaction zones is 200° C. or less.

### Claim 3 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, wherein a part of the hydrocarbon oil is supplied as a quench oil between the adjacent reaction zones among the plurality of the reaction zones and thereby the inlet temperature of the reaction zone disposed on the downstream side of the supplying position of the quench oil is controlled.

### Claim 4 (depends on 3)

The method for manufacturing a hydrocarbon oil according to claim 3, wherein the recycled oil and/or the quench oil contain a part of a product obtained by isomerizing the hydrocarbon oil or a middle distillate fractioned from the hydrocarbon oil.

### Claim 5 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, wherein the hydrocarbon oil is fractionated into a light distillate, a middle distillate and a heavy distillate, and the cut temperature between the light distillate and the middle distillate is set at 100 to 200° C. and the cut temperature between the middle distillate and the heavy distillate is set at 300 to 400° C.

### Claim 6 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, further comprising a third step wherein the hydrocarbon oil or a middle distillate fractionated from the hydrocarbon oil is isomerized.

### Claim 7 (depends on 6)

The method for manufacturing a hydrocarbon oil according to claim 6, wherein an isomerized oil obtained in the third step is fractionated into a light distillate, a middle distillate and a heavy distillate, the cut temperature between the light distillate and the middle distillate is set at 100 to 200° C. and the cut temperature between the middle distillate and the heavy distillate is set at 300 to 400° C.

### Claim 8 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, wherein the oxygen-containing hydrocarbon compound is one or more compounds selected from a fatty acid and a fatty acid ester.

### Claim 9 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, wherein the catalyst has a pore volume of 0.30 to 0.85 ml/g as measured by a nitrogen adsorption BET method and an average pore diameter of 5 to 11 nm, and the ratio of the pore volume derived from pores having a pore diameter of 3 nm or less to the total pore volume is 35% by volume or less.

### Claim 10 (depends on 1)

The method for manufacturing a hydrocarbon oil according to claim 1, wherein the porous inorganic oxide contains the element phosphorus.