US20070170091A1

US20070170091A1 - Production of high-cetane diesel fuel from low-quality biomass-derived feedstocks

Info

Publication number: US20070170091A1
Application number: US11/644,882
Authority: US
Inventors: Jacques Monnier; Michio Ikura; Guy Tourigny
Original assignee: Canada Minister of Natural Resources
Current assignee: Canada Minister of Natural Resources
Priority date: 2005-09-26
Filing date: 2006-12-26
Publication date: 2007-07-26
Also published as: JP4885962B2; US7754931B2; EP1928983B1; AU2006294366B2; AU2006294366A1; CA2621231C; AU2006294366A2; WO2007033460A1; CA2621231A1; EP1928983A4; EP1928983A1; US20070068848A1; JP2009510185A

Abstract

A method is taught for producing diesel fuels of high cetane value from a triglyceride feedstock, comprising pretreating the triglyceride feedstock by thermal cracking or rapid pyrolysis to partially convert the triglycerides and produce a middle distillates stream, and catalytically hydrotreating the middle distillate fraction to produce high cetane value diesel fuels. A biomass-derived diesel fuel is also taught having sulphur content below 10 ppm, a cetane-value of at least 70, a cloud point below 0° C. and a pour point of less than −4° C. A blended diesel fuel is also taught comprising 5 to 20 vol. % of the biomass-derived diesel fuel of the present invention and 80 to 95 vol. % of a petroleum diesel, based on total volume of the blended diesel fuel.

Description

CROSS REFERENCE TO RELATED APPLICATIONS

The present application is a continuation-in-part of U.S. patent application Ser. No. 11/234,175 filed Sep. 26, 2005.

FIELD OF THE INVENTION

The present invention relates to a two-step method for producing diesel fuel having a high cetane value from low quality biomass-derived feedstocks.

BACKGROUND OF THE INVENTION

In recent years, the area of biomass-derived diesel fuels has drawn a great deal of attention. These fuels are plant and animal based and are produced from such sources as canola, corn, soybean etc. Biomass-derived fuels are generally environmentally less damaging to use than traditional fossil fuels.
Another potential source for biomass-derived diesel fuels is from the waste greases of animal rendering facilities and waste cooking oils, such as those found as restaurant trap greases. However these waste greases and oils tend to contain contaminants that must effectively be removed before processing.
In the past, catalytic hydrotreating has been performed on triglyceride feedstocks in an attempt to produce high-cetane diesel fuels. Examples of such processes can be seen in U.S. Pat. Nos. 5,705,722 and 4,992,605, herein incorporated by reference.
The cetane value of a diesel fuel is a measure of how easily the fuel will auto-ignite at predetermined pressure and temperature and is often used to determine fuel quality. However, large quantities of hydrogen are required for this process, which is a major operating cost in the production of biomass-derived diesel fuel by catalytic hydrotreating. Reducing the volume of hydrogen consumed in the process would make the process economics more favourable. As well, hydrotreating was found to work best for very high quality feedstocks, such as tallow, vegetable oils (canola oil, soya oil, etc.) and yellow grease. Lower quality feedstocks, such as restaurant trap grease were found to be difficult to convert by catalytic hydrotreating, due to their heterogeneous nature and the presence of contaminants. These contaminants were found to rapidly deactivate the catalyst, thereby reducing hydrotreating reactor time on stream, requiring large quantities of catalyst to be used, and increasing operating costs. There is therefore a great need to find efficient methods of producing a high cetane value product from low quality waste triglyceride feedstocks, such as restaurant trap greases and other waste greases, which can be used as a diesel fuel or as diesel fuel blending stock. There is also a need to find efficient methods to reduce hydrogen consumption in the catalytic hydrotreating stage.

SUMMARY OF THE INVENTION

The present invention thus provides a method of producing diesel fuels of high cetane values from triglyceride feedstocks, comprising pretreating the triglyceride feedstocks by thermal cracking or rapid pyrolysis to partially convert the triglycerides and produce a middle distillates stream, and catalytically hydrotreating the middle distillate fraction to produce high cetane value diesel fuels.
The present invention also provides a biomass-derived diesel fuel having sulphur content below 10 ppm, a cetane-value of at least 70, a cloud point below 0° C. and a pour point below −4° C.
In yet another embodiment, the present invention provides a blended diesel fuel comprising 5 to 20 vol. % of the biomass-derived diesel fuel of the present invention and 80 to 95 vol. % of a petroleum diesel, based on total volume of the blended diesel fuel.

BRIEF DESCRIPTION OF THE DRAWINGS

The present invention will now be described in further detail with reference to the following drawings, in which: FIG. 1 is a flow diagram of a first preferred process for carrying out the present invention; and
FIG. 2 is a flow diagram of a second preferred process for carrying out the present invention.

DEFINITIONS

Biomass-derived diesel fuel—a diesel fuel produced by catalytic hydrotreating of biomass feedstocks and containing practically no oxygen.
Biodiesel—a diesel fuel produced from the transesterification of biomass-derived oils with alcohol and containing oxygen.
Cetane number—measure of the ignition quality of diesel fuel obtained by comparing it to reference fuels or blends of reference fuels of known cetane number in a standardized engine test. The reference fuels are n-cetane, having good ignition quality (CN=100), and heptamethylnonane, having poor ignition quality (CN=15).
High cetane value—for the purposes of the present invention a high cetane value is defined as a value of at least 70.
Waste triglyceride feedstock—a triglyceride from waste sources such as restaurant trap grease, waste from animal rendering facilities and other waste oil and grease sources, generally having at least some contaminants.
Catalytic hydrotreating—a refinery process for catalytically converting and removing sulphur, nitrogen and oxygen from fuels and fuel feedstocks at elevated hydrogen pressures and appropriate temperatures.
Middle distillates—encompass a range of petroleum fractions from kerosene to lubricating oil and include light fuel oils and diesel fuel, generally having a boiling point in the range of 150 to 345° C.
Thermal cracking—the process of breaking down large hydrocarbon molecules into smaller molecules under high temperature and pressure.
Cloud point—a measure of the ability of a diesel fuel to operate under cold weather conditions. Defined as the temperature at which wax first becomes visible when diesel fuel is cooled under standardized test conditions.
Pour point—the lowest temperature at which a fuel flows, when cooled under standardized test conditions. Generally taken to be 3° C. (5.4° F.) or 1° C. (1.8° F.) (depending on selected temperature interval) above the temperature of the no-flow point at which a test vessel of fuel shows no movement when applying a controlled burst of nitrogen gas onto the specimen surface (ASTM D 5949).
Rapid pyrolysis—a process of decomposing chemicals at very high temperatures and in the absence of an oxidizing agent. Rapid pyrolysis has very short residence times compared to other thermal decomposition methods.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

The present process employs a novel combination of thermal cracking followed by catalytic hydrotreating to convert low quality triglycerides feedstock into usable biomass-derived diesel fuel. In the present process, thermal cracking is used as a pre-treatment step before catalytic hydrotreating, to partially break down the triglycerides into lower molecular weight components and fatty acids, which can then easily be hydrotreated to produce a diesel fuel having a high cetane value and low sulphur content. As an alternate to thermal cracking, rapid pyrolysis of waste triglycerides can also be used in the present process and details of rapid pyrolysis are given below.
A flow diagram of the process steps and streams of a one embodiment of the present invention is shown in FIG. 1. A feedstock of low quality triglycerides is fed to thermal cracking unit 10. The feedstock can be any variety of waste biomass, including restaurant trap greases, waste greases from animal rendering facilities and other forms of waste oils and greases and low-quality vegetable oils. Preferably, the feedstock 18 is restaurant trap grease and other low-quality feedstocks. The feedstock stream 18 can be heterogeneous in nature and can contain water, carbon particles and have oxygen content as high as 14 wt. % or more.
In the thermal cracking unit 10, the feedstock 18 is partially converted into a mixture of fatty acids and lower molecular weight hydrocarbons. Thermal cracking is preferably carried out under mild cracking conditions which are defined as preferably an operating temperature in the range of from 390 to 460° C., more preferably from 410 to 430° C., and preferably an operating pressure of from 0 to 415 kPa, more preferably from 205 to 275 kPa. Thermal cracking produces various fractions including gases 24, naphtha plus water 26, middle distillate 22, and residue 20.
In an optional embodiment (not shown), the triglyceride feedstock may be filtered to remove any macroscopic contaminant particles.
The middle distillate stream 22 makes up more than half of the thermally cracked product and has been found to have suitable characteristics for further hydrotreating. Middle distillates typically encompass a range of petroleum equivalent fractions from kerosene to lubricating oil and include light fuel oils and diesel fuel. In one embodiment of the present invention the middle distillates were found to have a boiling point range of from 150 to 345° C., and more preferably from 165 to 345° C. The middle distillates fraction was found to contain as much as 40% less oxygen than the starting triglycerides feedstock 18, resulting in less hydrogen being required in the subsequent hydrotreating step.
The middles distillate stream 22 is fed to a catalytic hydrotreating unit 12 containing a catalyst to facilitate and enhance the hydrotreating process. This catalyst is a commercial hydrotreating catalyst such as, for example, nickel-molybdenum, cobalt-molybdenum or nickel-tungsten on a catalyst support. It is preferably a supported nickel-molybdenum catalyst. Known methods in the art can be used to maintain activation of the catalyst, thereby lengthening the useful life of the catalyst.
Hydrogen 28 is also fed to the hydrotreating unit 12. The present inventors have found that, by partially removing oxygen from the feed in the thermal cracking pre-treatment stage, hydrogen consumption in the hydrotreating step decreases significantly. Typical hydrogen consumption for hydrotreatment of clean, high quality biomass feedstock, without thermal cracking, is in the range of 2.3 to 3.0 kg H₂per 100 kg of feedstock. By contrast, hydrogen consumption during hydrotreating of the thermally cracked middle distillates stream 22 is only between 1.5 to 2.0 kg H₂per 100 kg of middle distillate feed 22 to the hydrotreating unit 12.
It has also been observed that, when processing thermally cracked waste triglycerides, hydrotreating can be conducted at lower temperatures than those required for clean, high quality biomass feedstock. Hydrotreating temperatures in the range of 330 to 400° C., and more preferably 350 to 390° C., are used in the present invention, compared to at least 375° C. typically required for hydrotreating uncracked, clean biomass-derived feedstocks.
Hydrotreated product 30 can optionally then be fed to a separator 14 in which the product 30 is separated into a gas stream 35, a water stream 36 and a liquid organic product stream 38. The gas stream 35 can be recycled back to the hydrotreating unit 12 as a hydrogen recycle stream 32, or it can form a fuel gas by-product stream 34.
In a preferred embodiment, the separated liquid organic product stream 38 is fed to a distillation column 16 to further separate diesel fuel 40 from any paraffinic residues 42.
Naphtha 26 and gases 24 from the thermal cracking unit 10 and fuel gas 34 from the hydrotreating step can optionally be sold as valuable by-products. The residue streams 20 and 42 are small and can be discarded by well known means in the art. Stream 42 is much cleaner than stream 20 and can also possibly be used as feedstock for petrochemical applications.
Catalytic hydrotreatment of the middle distillate stream 22 produces a biomass-derived diesel fuel having a cetane value of from 75 to 80 and sulphur content below 10 ppm. Oxygen content of the resultant diesel fuel, an indication of the extent of conversion of the feedstock to diesel fuel, was found to be in the range of 0.09 wt % or less, on the basis of the weight of product diesel.
The biomass-derived diesel fuel of the present invention also exhibits excellent cold-flow properties. The cloud point of the fuel is as low as −1.4 to −2.5 ° C. and the pour point is −4° C. or less.
In a further embodiment, the biomass-derived diesel fuel of the present invention can be used as diesel blending stock to produce a high cetane value blended diesel fuel. Preferably the blended diesel fuel comprises 5 to 20 vol. % of the biomass-derived diesel fuel of the present invention and 80 to 95 vol. % petroleum diesel, based on a total volume of the blended diesel fuel. More preferably, the blended diesel fuel comprises 10 vol. % of the biomass-derived diesel fuel of the present invention and 90 vol. % petroleum diesel, based on a total volume of the blended diesel fuel. The cetane value of the blended diesel fuel was found to be proportional to the quantities of biomass-derived diesel and petroleum diesel used in the blend and was generally higher than typical values of 40 to 50 for standard petroleum diesel. Cold flow properties of such a blended diesel fuel are improved by the addition of petroleum diesel and are superior to those of the biomass-derived diesel fuel alone.
As mentioned earlier, the step of thermal cracking can optionally be replaced by a step of rapid pyrolysis. This process is shown in FIG. 2. Rapid pyrolysis is a process of decomposing a chemical at very high temperatures and in the absence of an oxidizing agent. Rapid pyrolysis has very short residence times when compared to thermal cracking.
In the present invention, rapid pyrolysis of triglycerides, more specifically trap grease, was conducted at temperatures ranging from 480° C. to 600° C. for approximately 2 seconds. The triglycerides 18 are fed to a fluidized bed reactor 44 which is preferably fluidized with steam 46, although other suitable fluidizing media known in the art can also be used and are encompassed by the present invention. Steam 46 may be fed to the reactor at a ratio ranging from 0.5 to 1.5, relative to the triglyceride feed stream 18. The preferred steam to triglyceride feed ratio is 0.9.
Any known inert gas 48 can optionally be added to the reactor to purge the reactor of free oxygen during pyrolysis. The inert gas 48 is preferably nitrogen. A catalyst may also be added, and suitable catalysts include, but are not limited to acid washed activated carbon, calcined sewage sludge solids and silica sand, such as silica alumina. The catalyst acts to enhance the selective cracking of triglyceride molecules to largely free fatty acid molecules.

Sample data from rapid pyrolysis trials on a trap grease feedstock is listed in Table 1 below. The resultant pyrolysis products are shown in Table 2.

TABLE 1


Rapid pyrolysis conditions

Run ID

	261	265	253

Temperature (° C.)	511	575	580
Fluidizing media	Steam	Steam	Steam
Steam/Feed ratio	˜0.9	˜0.9	˜0.9
by weight
N₂purge/Feed	˜7	˜7	˜7
ratio by weight
Catalyst	Acid washed	Sewage sludge	Silica sand
	activated	solids,
	carbon,	calcined at
	35 mesh minus	750° C.
Gas phase contact	˜2	˜2	˜2
time (s)

TABLE 2


Rapid Pyrolysis Products

	261	265	253

Gas	28.2	11.3	7.6
Liquid	50.3	89.4	90.7
Solids (coke)	9.0	Trace	1.4
Total above	87.5	100.7	99.7

The liquid fraction identified in Table 2 above contains middle distillates 22 as well as naphtha 26 and some residue 20. The boiling point distribution of the liquid fraction was determined by thermogravimetric analysis (TGA) and is given in Table 3 below. The middle distillates yield is given in Table 4. These tables indicate that rapid pyrolysis of triglycerides produces an even larger proportion of desirable middle distillates than thermal cracking.

TABLE 3

Boiling point distribution of the liquid fraction (from TGA)

261 265 253

Naphtha (IBP ˜165° C.) 86% 10% 8%

Middle distillate 12% 75% 64%

(165˜345° C.)

Residue (345° C. plus) 2% 15% 28%

TABLE 4


Middle distillate yield with respect to feed

	261	265	253

	Middle distillate (wt % of feed)	6%	67%	58%

The middle distillate fraction 22 produced by rapid pyrolysis was found to have varying free fatty acids (FFA) content, depending on the pyrolysis conditions. These details are shown in Table 5 below:

TABLE 5

Fatty acids in the middle distillate fraction

Run ID

261 265A 265B 253

Pyrolysis Temperature(°C.) 511 575 575 580

Total FFA wt % 0.63 45.70 45.50 33.17
It was noted that the largest middle distillates fraction was produced by rapid pyrolysis at a temperature of 575° C. As well, FFA content was highest for this temperature range. A preferred temperature range for rapid pyrolysis of the present process is therefore from 550° C. to 600° C. and a most preferred range is from 565° C. to 585° C.
The difference in middle distillates yield between the run at 575° C. and the run at 580° C. is thought to be due to the difference in catalysts rather than the small difference in temperature. Catalyst derived from sewage sludge is less acidic than silica sand. Thus, although the run with silica sand produced a slightly larger liquids fraction by deoxygenation, this was accompanied by higher coke and residue formation, resulting in an overall lower level of middle distillates. Thus the sewage sludge appears to provide a preferred balance between higher middle distillate yield and lower coke formation.
It has also been noted that middle distillates produced by rapid pyrolysis comprise about 0.3 ppm nitrogen, compared with 5200 ppm nitrogen content in middle distillates obtained by mild thermal cracking.
As well, total sulphur in the middle distillate obtained by mild thermal cracking was in the order of 500 ppm whereas that in the middle distillate obtained by rapid pyrolysis was 150 ppm.
The following examples better illustrate the process of the present invention:

EXAMPLE 1

Conversion of Restaurant Trap Grease into Biomass-Derived Diesel
Restaurant trap grease having an average density of 0.925 g/mL, and an oxygen content of 13.72 wt % was fed to a thermal cracking unit where it was cracked at a temperature of 418.5° C. and a pressure of 300 kPa for 40 minutes. Thermal cracking produced a gas stream, a naphtha stream, a middle distillate stream having a boiling point in the range of from 165 to 345° C., water and residue. The middle distillates stream made up 63.0 wt % of the total cracked product and its oxygen content was only 7.99 wt %.
The middle distillate stream was then fed to a catalytic hydrotreating unit. Hydrotreating produced a biomass-derived diesel fuel having a cetane value of 75.4, a pour point of −6.0° C. and a cloud point of −2.5° C. The diesel was found to have less than 10 ppm sulphur content, which is well within tolerable commercial limits.

EXAMPLE 2

Conversion of Yellow Grease into Biomass-Derived Diesel
Yellow grease is waste grease resulting for rendering of animal fat. In this case, yellow grease, having a density of 0.918 g/mL and an oxygen content of 11.56 wt. % was fed to a thermal cracking unit in which it was cracked at 411° C. and 100 kPa for 40 minutes. Thermal cracking produced a product containing 68.6 wt % middle distillates (165° C.-345° C.), 7.0 wt % naphtha and the remainder gas, water and residues.
The middle distillate stream, which was found to have 8.29 wt % oxygen, was then fed to a catalytic hydrotreating unit. The resultant biomass-derived diesel stream had a cetane value of 79.2, a pour point of −4.0° C. and a cloud point of −1.4° C. The sulphur content of the diesel was found to be less than 10 ppm.
This detailed description of the process and methods is used to illustrate one embodiment of the present invention. It will be apparent to those skilled in the art that various modifications can be made in the present process and methods and that various alternative embodiments can be utilized. Therefore, it will be recognized that various modifications can also be made to the applications to which the method and processes are applied without departing from the scope of the invention, which is limited only by the appended claims.

Claims

1. A method of producing diesel fuels of high cetane value from a triglyceride feedstock, comprising:

a. pretreating the triglyceride feedstock by thermal cracking to partially convert the triglycerides and produce a middle distillates fraction; and

b. catalytically hydrotreating the middle distillate fraction to produce high cetane value diesel fuels.

2. The method of claim 1 wherein the triglycerides feedstock is selected from the group consisting of restaurant trap grease, animal fats, waste greases, low-quality vegetable oils and combinations thereof.

3. The method of claim 1 wherein the middle distillates have a boiling point in the range of from 160° C. to 345° C.

4. The method of claim 1 wherein thermal cracking is conducted at a temperature of from 390° C. to 460° C.

5. The method of claim 1 wherein thermal cracking is conducted at a temperature of from 410° C. to 430° C.

6. The method of claim 1 wherein catalytic hydrotreating consumes less than 2.0 kg of hydrogen) per 100 kg of middle distillate fed to the hydrotreating step.

7. The method of claim 1 wherein catalytic hydrotreating is conducted at a temperature of from 330° C. to 400° C.

8. The method of claim 6 wherein catalytic hydrotreating is conducted at a temperature of from 350° C. to 390° C.

9. The method of claim 1 wherein catalytic hydrotreating is conducted using a commercial hydrotreating catalyst.

10. The method of claim 9 wherein the commercial hydrotreating catalyst is nickel-molybdenum, cobalt-molybdenum or nickel-tungsten on a catalyst support.

11. The method of claim 1, further comprising filtering the triglyceride feedstock to remove macroscopic contaminant particles before thermal cracking.

12. The method of claim 1, further comprising conducting separation after catalytic hydrotreating to produce a gas stream, a water stream and a liquid organic product stream.

13. The method of claim 12, further comprising distilling the liquid organic product stream to further separate diesel fuels from paraffinic residues.

14. The method of claim 12, further comprising the step of recycling the gas stream as hydrogen recycle during catalytic hydrotreating.

15. A biomass-derived diesel fuel having a cetane-value of at least 70, a cloud point below 0° C. and a pour point of less than −4° C.

16. The diesel fuel of claim 15, having a sulphur content of below 10 ppm.

17. The diesel fuel of claim 15, produced by the process of claim 1.

18. A blended diesel fuel comprising 5 to 20 vol. % biomass-derived diesel fuel as described in claim 15 and 80 to 95 vol. % petroleum diesel, based on a total volume of the blended diesel fuel.

19. The blended diesel fuel of claim 18 comprising 10 vol. % biomass-derived diesel fuel as described in claim 15 and 90 vol. % petroleum diesel, based on a total volume of the blended diesel fuel.

20. A method of producing diesel fuels of high cetane value from a triglyceride feedstock, comprising:

a. pretreating the triglyceride feedstock by rapid pyrolysis to partially convert the triglycerides and produce a middle distillates fraction; and

21. The method of claim 20 wherein the triglycerides feedstock is selected from the group consisting of restaurant trap grease, animal fats, waste greases, low-quality vegetable oils and combinations thereof.

22. The method of claim 20 wherein the middle distillates have a boiling point in the range of from 160° C. to 345° C.

23. The method of claim 20 wherein rapid pyrolysis is conducted at a temperature of from 480° C. to 600° C.

24. The method of claim 20 wherein rapid pyrolysis is conducted at a temperature of from 550° C. to 600° C.

25. The method of claim 20 wherein rapid pyrolysis is conducted at a temperature of from 565° C. to 585° C.

26. The method of claim 20 wherein the triglyceride feedstock is fluidized with steam.

27. The method of claim 26 wherein the steam to triglyceride feedstock ratio ranges from 0.5 to 1.5.

28. The method of claim 27 wherein the steam to triglyceride feedstock ratio is 0.9.

29. The method of claim 20 wherein an inert gas is used to purge any oxidizing agents during rapid pyrolysis.

30. The method of claim 29 wherein the inert gas is nitrogen.

31. The method of claim 20 wherein a catalyst is used during rapid pyrolysis to enhance the cracking of triglycerides to largely free fatty acids.

32. The method of claim 31 wherein the catalyst is selected from the group consisting of acid washed activated carbon, calcined sewage sludge solids and silica sand.

33. The method of claim 20 wherein catalytic hydrotreating consumes less than 2.0 kg of hydrogen) per 100 kg of middle distillate fed to the hydrotreating step.

34. The method of claim 20 wherein catalytic hydrotreating is conducted at a temperature of from 330° C. to 400° C.

35. The method of claim 34 wherein catalytic hydrotreating is conducted at a temperature of from 350° C. to 390° C.

36. The method of claim 20 wherein catalytic hydrotreating is conducted using a commercial hydrotreating catalyst.

37. The method of claim 36 wherein the commercial hydrotreating catalyst is nickel-molybdenum, cobalt-molybdenum or nickel-tungsten on a catalyst support.

38. The method of claim 20, further comprising filtering the triglyceride feedstock to remove macroscopic contaminant particles before rapid pyrolysis.

39. The method of claim 20, further comprising conducting separation after catalytic hydrotreating to produce a gas stream, a water stream and a liquid organic product stream.

40. The method of claim 39, further comprising distilling the liquid organic product stream to further separate diesel fuels from paraffinic residues.

41. The method of claim 39, further comprising the step of recycling the gas stream as hydrogen recycle during catalytic hydrotreating.

42. The diesel fuel of claim 15, produced by the process of claim 20.