Process and apparatus for producing hydrocarbons by hydrogenating a terpene feed

Patent metadata

Field	Value
Publication number	US-9677011-B2
Application number	US-201013382823-A
Country	US
Kind code	B2
Filing date	Jul 2, 2010
Priority date	Jul 7, 2009
Publication date	Jun 13, 2017
Grant date	Jun 13, 2017

Abstract

The invention relates to a process and an apparatus for producing hydrocarbon components in the presence of a hydrodesulphurization catalyst. The components obtained by the process are suitable for use as fuel composition as such or as an additive in fuel compositions, and in cosmetics or pharmaceutical products.

First claim

The invention claimed is:

1. A process for producing fuel hydrocarbon components, said process comprising:
providing a terpene feed selected from a group consisting of crude sulphate turpentine derived from kraft pulping process of wood (CST), crude turpentine derived from mechanical pulping of wood, distillation bottoms from turpentine distillation, turpentine evaporated from crude tall oil, sulphur-containing C5 to C10 hydrocarbon streams from wood processing, and mixtures thereof, at a WHSV of about 0.5 to about 10, measured in accordance with the following equation:

WHSV
⁡

[

h

-
1

]

=

V

feed
⁡

[

g
/
h

]

m

catalyst
⁡

[
g
]

wherein V feed[g/h] means a pumping velocity of the terpene feed, and M catalyst[g] means an amount of the catalyst;
subjecting the terpene feed and a hydrogen gas, in a volumetric ratio of hydrogen gas to the terpene feed of from about 100 to about 1500 Nl/l, to a hydrogenation step at a temperature range of from about 275° C. to about 425° C. and at a pressure of 10 to 150 bar, in the presence of a hydrodesulphurization catalyst selected from a group consisting of NiO/MoO 3 , CoO/MoO 3 and a mixture of NiO/MoO 3 and CoO/MoO 3 on a support selected from Al 2 O 3 and Al 2 O 3 —SiO 2 , to produce hydrocarbon components comprising C 4 to C 28 hydrocarbons; and
recycling at least a portion of the hydrocarbon components back to the terpene feed and/or to the hydrogenation step.

2. The process of claim 1 , wherein a sulphur feed is optionally fed to the hydrogenation step.

3. The process of claim 1 , wherein the hydrocarbon components are subjected to separation to separate gasoline, diesel, naphtha and jet range hydrocarbon fractions.

4. The process of claim 1 , wherein the hydrocarbon components are subjected to a hydrogen sulphide removal step to remove any residual hydrogen sulphide from the mixture.

5. The process of claim 1 , wherein the residual hydrogen sulphide is removed by stripping, flashing or bubbling with inert gas.

6. The process of claim 1 , wherein the hydrogenation step is carried out at a temperature of about 400° C.

7. The process of claim 1 , wherein the hydrogenation step is carried out at a pressure of about 20 to about 70 bar.

8. The process of claim 1 , wherein the hydrogenation step is carried out at a pressure of about 25 to about 50 bar.

9. The process of claim 1 , wherein a volumetric ratio of H 2 gas fed to the hydrogenation step to the terpene feed is in the range from about 100 to about 350 Nl/l.

10. The process of claim 1 , wherein a volumetric ratio of H 2 gas fed to the hydrogenation step to the terpene feed is in the range from about 100 to about 300 Nl/l.

11. The process of claim 1 , wherein the WHSV is in the range of about 1 to about 5.5.

12. The process of claim 1 , wherein a mixture of 1-isopropyl-4-methylbenzene, 1-isopropyl-4-methylcyclohexane and 2,6-dimethyloctane or isomers thereof is formed.

13. The process of claim 12 , wherein WHSV is about 2 to about 3.5 and the temperature is greater than about 330° C.

14. The process of claim 12 , wherein 1-isopropyl-4-methylbenzene is isolated.

15. The process of claim 1 , wherein the hydrocarbon components obtained are fuel compositions or additives in fuel compositions.

16. The process of claim 15 , wherein the fuel compositions are gasoline, diesel, naphtha or jet fuel.

17. The process of claim 1 , wherein sulphur is supplied to the process and wherein the added amount of sulphur is in the range of about 100 to 200 ppm.

Assignees

• Knuuttila Pekka
• Nousiainen Jaakko
• Upm Kymmene Corp

Inventors

• Knuuttila Pekka
• Nousiainen Jaakko

Classifications

• C10G45/02 Primary

  to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing · CPC title

• C10G3/46

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

• Y02P30/20

  using bio-feedstock · CPC title

• C10G3/50

  in the presence of hydrogen, hydrogen donors or hydrogen generating compounds · CPC title

• C10G45/58

  to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins (C10G32/00 takes precedence; improving or increasing the octane number or aromatic content of naphtha C10G35/00) · CPC title