Process for purification of biological feed material

Patent metadata

Field	Value
Publication number	US-10815428-B2
Application number	US-201314395168-A
Country	US
Kind code	B2
Filing date	Apr 17, 2013
Priority date	Apr 18, 2012
Publication date	Oct 27, 2020
Grant date	Oct 27, 2020

Abstract

The present invention relates to a process for the purification of biological feed material and to a process for catalytically converting the purified biological feed material into hydrocarbons suitable as biofuel components. The purified feed material is treated in a reactor system including a catalytically active guard bed phase and a catalytically active main reaction phase. At least one of the phases includes a catalyst bed with a combination of hydrodeoxygenating (HDO) and hydrodewaxing (HDW) catalysts. The process provides biofuel with acceptable ignition and cold flow properties.

First claim

The invention claimed is:

1. A process for the purification of biological feed material, comprising:
purifying biological feed material by using a heater and evaporator combination, wherein the biological feed material is first treated in the heater and subsequently treated in a series of three evaporators;
wherein the biological feed material is subjected to treatment in the heater to produce a first fraction comprising water and light components having a boiling point of 150-210° C. at normal pressure and second fraction comprising heavier components and residues, and the second fraction is directed to a first evaporator;
wherein the biological feed material is treated in the heater at a temperature of 80 to 150° C. and under a pressure of 40 to 80 mbar to obtain a first fraction and a second fraction from the heater.

2. The process according to claim 1 where the biological feed material comprises tall oil materials.

3. A process for producing biofuel or biofuel components, comprising:
purifying biological feed material by using a heater and evaporator combination, wherein the biological feed material is first treated in the heater and subsequently treated in a series of three evaporators to obtain purified biological feed material, wherein the biological feed material is subjected to treatment in the heater to produce a first fraction comprising water and light components having a boiling point of 150-210° C. at normal pressure and second fraction comprising heavier components and residues, and directing the second fraction to a first evaporator;
feeding of the purified biological feed material into a reactor system, which comprises a catalytically active guard bed phase and a catalytically active main reaction phase and wherein the purified biological feed material is contacted, in at least one catalyst bed of said phases, with a combination of hydrodeoxygenating (HDO) and hydrodewaxing (HDW) catalysts,
treating the purified biological feed material catalytically with hydrogen in the reactor system to cause hydro deoxygenation, isomerization and cracking of feed material components to provide a hydroprocessing product, and
recovering at least a fraction of the hydroprocessing product as biofuel or biofuel components;
wherein the biological feed material is treated in the heater at a temperature of 80 to 150° C. and under a pressure of 40 to 80 mbar to obtain a first fraction and a second fraction from the heater.

4. The process according to claim 3 , wherein the combination of HDO and HDW catalysts comprises mixture(s) or layers of the catalysts.

5. The process according to claim 3 , wherein said mixture(s) is/are provided by physically mixing HDO and HDW catalyst particles or by adding HDO and HDW catalyst metals onto the same support material.

6. The process according to claim 3 wherein the biological feed material comprises tall oil materials.

7. The process according to claim 3 wherein the HDO catalyst is selected from the group consisting of NiMo, CoMo and a mixture of Ni, Mo and Co on a support selected from Al2O3, SiO2 and ZrO2, and the HDW catalyst is selected from NiW/Al2O3 and NiW/zeolite/Al2O3.

8. The process according to claim 3 wherein the HDO catalyst comprises NiMo/Al2O3 and the HDW catalyst comprises NiW/zeolite/Al2O3.

9. The process according to claim 3 wherein the main reaction phase comprises two or more main catalyst beds with their respective combinations of HDO and HDW catalysts.

10. The process according to claim 3 wherein the main reaction phase comprises two or more main catalyst beds, which operate in series.

11. The process according to claim 3 wherein the proportion of the HDO catalyst at the inlet of the main reaction phase is higher than the proportion of the HDW catalyst.

12. The process according to claim 3 wherein the reactor system comprises two or more guard catalyst beds, wherein HDW catalyst is combined with HDO catalyst in at least one of the guard catalyst beds.

13. The process according to claim 3 wherein the feed after the guard bed phase passes through the main catalyst beds of the reactor system in series as a continuous flow without outlets for byproducts or other side streams.

14. The process according to claim 3 wherein water is separated from the hydroprocessing product by cooling.

15. The process according to claim 3 wherein hydrogen sulfide and carbon dioxide are separated from the gaseous hydroprocessing products by amine scrubbing.

16. The process according to claim 3 wherein a diesel fraction and a naphtha fraction are recovered and a heavy fraction is recirculated to the inlet end of the guard bed phase or the main reaction phase.

17. The process according to claim 3 wherein the feed material is treated in a heater selected from conventional heater, falling film evaporator, plate molecular still and thin film evaporator.

18. The process according to claim 3 wherein the second fraction from the heater is treated in the first evaporator selected from short path evaporator, plate molecular still and thin film evaporator.

19. The process according to claim 18 wherein the second fraction from the heater is treated in the first evaporator at a temperature of 180 to 250° C. and under a pressure of 40 to 80 mbar to obtain a third fraction and a fourth fraction from the first evaporator.

20. The process according to claim 19 wherein the fourth fraction from the first evaporator is treated in a second evaporator selected from thin film evaporator, short path evaporator and plate molecular still, preferably short path evaporator is used.

21. The process according to claim 20 wherein the fourth fraction from the first evaporator is treated in a second evaporator at a temperature of 200 to 350° C. and under a pressure of 0.01 to 50 mbar to obtain a fifth fraction and a sixth fraction from the second evaporator.

22. The process according to claim 21 wherein the sixth fraction from the second evaporator is treated in a third evaporator selected from short path evaporator and plate molecular still.

23. The process according to claim 22 wherein the sixth fraction from the second evaporator is treated a third evaporator at a temperature of 250 to 400° C. and under a pressure of 0.01 to 10 mbar to obtain a seventh fraction and a eighth fraction from the third evaporator.

24. The process according to claim 23 wherein the fifth fraction from the second evaporator and the seventh fraction from the third evaporator are used as the purified feed.

25. Fuel having characteristics meeting specification EN 590 diesel and comprising at least one hydrocarbon fraction produced by the process of claim 3 .

26. The process according to claim 1 where the biological feed material is selected from crude tall oil, tall oil components, tall oil derivatives and mixtures thereof.

27. The process according to claim 3 wherein the biological feed material is selected from crude tall oil, tall oil components, tall oil derivatives and mixtures thereof.

28. The process according to claim 18 wherein the first evaporator is thin film evaporator.

29. The process according to claim 20 wherein the second evaporator is short path evaporator.

30. The process according to claim 22 wherein the third evaporator is short path evaporator.

Assignees

• Upm Kymmene Corp

Inventors

• Nousiainen Jaakko
• Kotoneva Jari
• Laumola Heli
• Lindberg Teemu
• Mokkila Kosti

Classifications

• C10L1/04

  essentially based on blends of hydrocarbons · CPC title

• C10G3/50 Primary

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

• C10G3/49

  containing crystalline aluminosilicates, e.g. molecular sieves · CPC title

• C10G3/46 Primary

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

• Y02P30/20

  using bio-feedstock · CPC title