A process for producing free fatty acids

专利摘要:
A process for producing free fatty acids from oil comprising chlorophyll is disclosed. The invention is based on blending oil comprising chlorophyll with fats, followed by hydrolysis and distillation.
公开号:FI20176150A1
申请号:FI20176150
申请日:2017-12-22
公开日:2019-06-23
发明作者:Jukka-Pekka Pasanen；Annika Malm；Rami Piilola
申请人:Neste Oyj；
IPC主号:

专利说明:

A PROCESS FOR PRODUCING FREE FATTY ACIDS
FIELD OF THE INVENTION
The present invention relates to processing of oil comprising chlorophyll. In 5 particular the invention relates to production of free fatty acids free of impurities from oil comprising chlorophyll, such as algal oil.
BACKGROUND
Chlorophyll containing oils, such as algal oil, are promising sources of renewable hydrocarbons. Algal oil differs from many vegetable oils and animal fats in that it io contains large amounts of chlorophyll. In addition algal oils typically contain high amounts of chlorine, metals and phosphorus. Major amount of nitrogen present in algal oil is found in the chlorophyll, contrary to nitrogen present in typical vegetable oil where nitrogen is primarily present in amino acids. Chlorophyll composes of four membered porphyrin ring that is highly stable and has a high 15 molecular mass. Because of its high molecular mass chlorophyll or its degradation products that still have a high molecular mass are known to cause plugging of catalyst or adsorbent pores and coking of the catalyst surfaces leading to catalyst deactivation. Therefore, when oils rich in chlorophyll are used in industrial processes such as fuel production, chlorophyll needs to be removed 20 prior to catalytic processing.
Previous technologies to remove chlorophyll include adsorptive treatment with different clays, enzymatic disruption of the chlorophyll ring structure, strong acid treatment, and membrane filtration. These technologies have typically been designed for removal of chlorophyll from vegetable oils that contain considerably 25 lower amount of chlorophyll than algal oils. Because of the high chlorophyll content of algal oil, these previous technologies are not feasible in industrial scale for removing chlorophyll due to increased costs and processing difficulties. Therefore, for example analytical methods sometimes used to process and analyse algal oil are not useful in production at industrial scale.
Fat splitting and distillation is known technology to process fats and oils when producing free fatty acids. In this process triglycerides are processed with water
20176150 prh 22 -12- 2017 at high temperature, leading to the disruption (splitting) of the triglycerides into free fatty acids and glycerol. The resulting oil phase can be separated from the water-glycerol phase, and the free fatty acids can be separated from the oily phase by distillation.
The inventors have now found out that when using a feedstock comprising oil which has high chlorophyll content in a fat splitting and distillation process, after the splitting step the resulting water-glycerol phase and the free fatty acid phase are not sufficiently separated, and the resulting product is a emulsion, which is difficult to break.
io To prevent formation of emulsions when processing oil comprising high amount of chlorophyll, previous technologies have used pre-treatment of the oil to prepare and separate free fatty acids. Previously pre-treatment methods to separate the oily phase from the water-glycerol phase have included degumming to remove emulsifying components prior to hydrolysis, acidic conditions and/or demulsifying salts during the hydrolysis, and use of organic solvents after hydrolysis. However, these solutions are not feasible in industrial scale because they involve use of chemicals that are harmful to environment and may corrode equipment used in the process. Further, it has now been seen that they do not sufficiently improve the phase separation with oil comprising high amount of 20 chlorophyll.
An object of the present invention is to provide a processing method for oil comprising high amount of chlorophyll, which can be used to obtain free fatty acids that are simultaneously purified so that their further processing is possible and does not require expensive or complicated processing steps.
SUMMARY
According to the first aspect is provided a process for production of free fatty acids, the process comprising the steps of:
a. Providing a feedstock comprising a blend of: oil comprising chlorophyll and fat;
b. Hydrolysing the feedstock to obtain at least an oily phase;
c. Recovering the oily phase; and
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d. Distilling the oily phase for recovering free fatty acids contained therein
An advantage of the invention is that efficient hydrolysis and recovery of the oily phase is achieved. As the Examples indicate, the hydrolysis step alone is not yet efficient in removal of chlorophyll or its degradation products that still have an intact porphyrin ring structure. The oily phase, whose separation and recovery is made efficient by this invention, is then processed through distillation to produce free fatty acids of high quality and purity. In the recovered free fatty acids both the chlorophyll content and its degradation products and elemental impurities are considerably reduced.
Further, as the Examples indicate, if there is no pre-treatment like degumming prior to the hydrolysis, the present invention achieves simultaneous formation of free fatty acids and removal of elemental impurities from the oily phase during the hydrolysis step. Without bound by a theory this purification results from simultaneous water and glycerol washing of the oily phase and/or thermal effects. According to the second aspect is provided a free fatty acid fraction obtained by the process of the first aspect comprising at least 95% free fatty acids having carbon number C14-C28
According to the third aspect is provided a method of producing renewable fuel comprising the steps of:
a. Providing a feedstock comprising a blend of: oil comprising chlorophyll and fat,
b. Hydrolysing the feedstock to obtain at least an oily phase;
c. Recovering the oily phase;
d. Distilling the oily phase for recovering the free fatty acids contained therein; and
e. Subjecting the recovered free fatty acids to chemical reactions to generate hydrocarbons or alkylesters of fatty acids, wherein the free fatty acids are optionally used as: a co-feed in fuel production, as the only feed in fuel production, and/or the fuel obtained from the free fatty acids is used in a blend with another fuel;
20176150 prh 22 -12- 2017 whereby renewable fuel is produced.
In an embodiment in the method the oil comprising chlorophyll the total content of free fatty acids, monoglycerides, diglycerides and triglycerides as analysed by ISO 15304M-2002 is lower than 90% w/w;
The method is advantageous in that it effectively and economically utilises oil comprising high amount of chlorophyll as a source of renewable feedstock. With the present method, catalytic conversion of the free fatty acids is possible because of the high quality and purity of the obtained product. Thus, problems relating to catalyst blocking and inactivation can be avoided.
io According to the fourth aspect is provided a method of removing chlorophyll from a feedstock comprising:
a. Providing a feedstock comprising a blend of oil comprising chlorophyll and fat;
b. Hydrolysing the feedstock to obtain at least an oily phase;
c. Recovering the oily phase; and
d. Distilling the oily phase.
In an embodiment the steps of the above methods and processes are carried out in the indicated sequence starting from the step a.
DETAILED DESCRIPTION OF THE INVENTION
As used herein, the term “comprising” includes the broader meanings of ’’including”, ’’containing”, and ’’comprehending, as well as the narrower expressions “consisting of” and “consisting only of”.
In an embodiment at least one component of the composition of the invention has a different chemical, structural or physical characteristic compared to the 25 corresponding natural component from which the at least one component is derived from. In an embodiment said characteristic is at least one of: more uniform size or molecular weight, more homogeneous dispersion or solution, higher purity.
If the feedstock to be hydrolysed contains only oil having high chlorophyll 30 content, such as algal oil, without blending it with fat, phase separation does not
20176150 prh 22 -12- 2017 take place efficiently after hydrolysis, and an emulsion is obtained instead of separate phases. The resulting emulsion is difficult to process further at an industrial scale e.g. because of its high viscosity. Consequently, the emulsion cannot be separated without using impractical methods, such as organic solvents 5 or extensive centrifugation. When fat splitting is typically performed for vegetable oils and animal fats, these emulsion problems are often solved by removing phospholipids from the feed by degumming and/or bleaching. However, it has now been seen that with oils having high chlorophyll content these conventional pre-treatment methods are not efficient in preventing emulsion formation, and io even algal oils with low phosphorus and, thus, low phospholipid content, leads into formation of emulsion. Without bound by any theory, it is believed that the tendency of even pre-treated, i.e., degummed and/or bleached algal oil to lead to emulsion problems is due to the non-triglyceride type components present in such oils having high chlorophyll content.
The present process is advantageous in that it provides an efficient production of free fatty acids from oil comprising chlorophyll with high purity with respect to metals, chlorophyll and chlorophyll degradation products. During the manufacturing process, the oily phase is efficiently separated from the aqueous phase containing glycerol. Further, with the present process a solid phase can be 20 formed during fat splitting and efficiently removed after fat splitting.
During the hydrolysis step the oily phase, which contains hydrophobic components, can be washed. The combination of hydrolysis and distillation according to the invention further enables processing the oil comprising chlorophyll into a fatty acid stream that is essentially free of chlorophyll and 25 chlorophyll degradation products that contain an intact porphyrin ring structure.
By using the present invention the resulting free fatty acids also contain a low amount of other impurities, such as elemental impurities. In an embodiment the fat that is used in the blend together with the oil comprising chlorophyll, comprises or substantially consist of animal fat, vegetable oil, or a mixture 30 thereof.
In an embodiment the total free fatty acid, mono-, di and triglyceride content of the fat as analysed by ISO 15304M-2002 is in the level of typical vegetable oil and animal fat, i.e. >90 % w/w and more preferably >95 % w/w.
20176150 prh 22 -12- 2017
As the Examples indicate, common pre-treatments prior to the hydrolysis step, like degumming, do not improve the phase separation after the hydrolysis.
Accordingly, in an embodiment is provided a process, which does not involve pre-treatment of the feedstock before hydrolysis. In another embodiment the 5 process does not involve degumming. Omitting a pre-treatment phase is advantageous because it simplifies the process and makes it more economical.
As the Examples indicate, even if the process does not involve pre-treatment prior to the hydrolysis, a simultaneous formation of free fatty acids and removal of elemental impurities from the oily phase can be achieved during the hydrolysis io step. Without being bound by a theory, this purification results from simultaneous water and glycerol washing of the oily phase and/or thermal effects.
In an embodiment the oil comprising chlorophyll comprises or consists of algal oil.
Algal oil is characterised by the total content of free fatty acids, mono-, di- and 15 triglycerides as analysed by ISO 15304M-2002 being lower than in typical vegetable oil and animal fat, i.e. < 90 % w/w.
In an embodiment the unsaponifiable residue of the oil comprising chlorophyll as analysed by ISO 18609-2000 is > 1 % w/w and more preferably > 5 % w/w.
In another embodiment the fat comprises or substantially consist of vegetable oil.
In an embodiment the feedstock consists of oil comprising chlorophyll and fat.
In another embodiment the blend has 200-2000ppm of phosphorus, preferably 220-2000ppm.
In an embodiment the phosphorus is calculated as elemental phosphorus.
In an embodiment in the oil comprising chlorophyll the total content of free fatty 25 acids, monoglycerides, diglycerides and triglycerides as analysed by ISO 15304M-2002 is lower than 90% w/w.
In an embodiment the fat is animal fat, vegetable oil, or a mixture thereof.
In an embodiment the feedstock contains less than 50 % w/w oil comprising chlorophyll, preferably algal oil. The remaining portion of the feedstock may 30 comprise fat, or fat and another source of hydrocarbons such as oil.
20176150 prh 22 -12- 2017
In an embodiment the feedstock contains 1-45 % w/w, preferably 5-45 % w/w, more preferably 5-35 % w/w, or 5-15 % w/w of oil comprising chlorophyll, preferably algal oil. The remaining portion of the feedstock may comprise fat, or fat and another source of hydrocarbons such as oil.
In an embodiment the feedstock contains about 10% w/w oil comprising chlorophyll, preferably algal oil. In another embodiment the feedstock contains 15% w/w, 25% w/w, 35% w/w, 45% w/w, 10-45% w/w, 10-35% w/w, 10-25% w/w, or 10-15% w/w oil comprising chlorophyll, preferably algal oil. This amount is preferred to obtain quick separation of the oily phase by settling. The remaining io portion of the feedstock may comprise fat, or fat and another source of hydrocarbons such as oil.
In an embodiment the feedstock contains fat at least 90% w/w, 85% w/w, 75% w/w, 65% w/w, or 55% w/w.
In an embodiment the blend contains 50% w/w or less oil comprising chlorophyll 15 and 50% w/w or more fat. Preferably the blend contains 10-45% w/w oil comprising chlorophyll and 90-55% w/w fat, more preferably 10-35% w/w oil comprising chlorophyll and 90-65% w/w fat, even more preferably 10-25% w/w oil comprising chlorophyll and 90-75% w/w fat, and most preferably 10-15% w/w oil comprising chlorophyll and 90-85% w/W fat.
In an embodiment the feedstock consist of the blend as defined above. In this particular embodiment the feedstock does not contain other free fatty acid sources in significant amounts.
In an embodiment the hydrolysing step is carried out in typical fat splitting conditions such as at a temperature selected from a range between 220 and 280 25 °C. In an embodiment a residence time ranging from 1 to 90 minutes is used. In another embodiment the amount of water ranges from 10 to 60 wt-%. In yet another embodiment emulsifiers or acidic catalysts are used in the hydrolysis step.
In an embodiment hydrolysing is carried out at a temperature selected from a 30 range between 220 and 280 °C.
20176150 prh 22 -12- 2017
In an embodiment the step c. further comprises separating an aqueous phase and a solid phase.
In an embodiment the step c. comprises separating about 5% w/w solids as the solid phase.
In an embodiment the oily phase recovered in step c. contains, compared to the feedstock before hydrolysis, less than 10% metals, preferably less than about 5% metals. In an embodiment the oily phase recovered in step c. contains, compared to the feedstock before hydrolysis, less than 5% phosphorus, preferably less than about 1% phosphorus. In another embodiment the oily phase recovered in step c.
io contains, compared to the feedstock before hydrolysis less than 10% chlorides, preferably less than about 6% chlorides.
In an embodiment in the step d. the distilling is carried out in conditions known in the prior art, where temperature ranges between 180 °C and 280 °C and pressure between 0.1 kPa and 1.0 kPa, to recover a fraction comprising free fatty 15 acids.
In an embodiment in the step d. the distilling is carried out at a temperature selected from the range between 220 and 300 °C and a pressure selected from the range between 0.01 and 50 kPa (given as an absolute pressure) to recover a fraction comprising free fatty acids.
In an embodiment the distilling is carried out to fractionate distinct algal oil free fatty acid fractions, i.e., fractions containing high amount of polyunsaturated fatty acids like 016:4, 018:3 and 020:5 that are typical of algal oils using methods known in the prior art.
In an embodiment the feedstock comprises at least lOOOppm total chlorophyll.
In an embodiment the feedstock comprises at least lOOOppm phosphorus.
In an embodiment the feedstock comprises at least 1000 ppm total chlorophyll and at least lOOOppm phosphorus.
In an embodiment the recovery in step c. is carried out by separating the oily phase from an aqueous phase and optionally from a solid phase. In an 30 embodiment phases are separated from each other by settling.
20176150 prh 22 -12- 2017
In another embodiment the phases are separated by centrifugation. Centrifugation may be advantageous in case an even faster separation of phases is desired.
In an embodiment also the solid phase is separated from the oily phase and the aqueous phase. Separation of the solid phase is advantageous and indicative of removal of elemental impurities. When these components are removed from the oily phase, impurities are removed that may be harmful e.g. for the performance of catalysts in later processing. Thus an advantage of the invention is that metal sensitive catalysts can be used to process the obtained free fatty acids.
io In an embodiment the hydrolysed algal oil is washed during hydrolysis and settling.
In an embodiment at least 90% w/w of metals, phosphorus and chlorides are removed in washing. In a preferable embodiment the washing is carried out during hydrolysis and separation of the oily phase from the aqueous phase and 15 the solid phase.
In an embodiment the aqueous phase contains glycerol.
In an embodiment distillation is carried out to obtain a free fatty acid containing fraction, which is essentially free from chlorophyll, preferably containing less than 10ppm chlorophyll. In another embodiment the free fatty acid fraction does not 20 contain metal or metals.
In an embodiment after distillation the free fatty acid phase has a colour ranging from yellow to dark orange. This colour is indicative of removal of impurities such as chlorophyll. In an embodiment the process is a batch process.
In an embodiment the process is a continuous process.
In an embodiment the free fatty acid fraction is used in to manufacture renewable fuel by hydrotreating the free fatty acids as such or blended with triglycerides into n-paraffins, optionally followed by catalytic conversion into branched paraffins (iparaffins).
In an embodiment the free fatty acid fraction is used in to manufacture chemicals.
EXAMPLES
20176150 prh 22 -12- 2017
The following examples are provided to illustrate various aspects of the present invention. They are not intended to limit the invention, which is defined by the accompanying claims.
Example 1 - processing algal oil
Materials
Feed for test was algal oil that was obtained by hexane extraction of Nannochloropsis biomass after the biomass was dried and the cells disrupted. This is called algal oil #1. Prior to the fat splitting experiment this oil was further treated to remove any solid material, e.g., sand by diluting the oil with 3 parts heptane and io centrifuging for 15 minutes. After this the heptane was evaporated in vacuum.
Procedure
Hydrolysis
Hydrolysis was performed by heating the pre-treated oil with water (1:1 mass ratio) in a 1 liter Parr reactor at 230 °C for 3h.
After hydrolysis the water phase did not separate by settling in oven at 60 °C for ca. 45 min. The water phase could, however, be separated from the oil phase by centrifugation at 40 °C/ 4400 rpm/15 min. Water was pipetted from the bottom of the centrifuge tube.
Some of the solids formed during hydrolysis could be separated with the water 20 phase, but high amounts remained between oil and water phase. After separating the water phase, oil was diluted with heptane (1:1 oil/heptane) and the remaining solid material was removed by filtering the oil-heptane solution through 4-12 pm filter paper. After this the heptane was evaporated to obtain the algal oil hydrolysate.
Also the water phase that was separated after centrifugation was filtered through 4-12 pm filter paper to remove solids. After this water was evaporated from this phase under vacuum in order to obtain a dry glycerol phase.
Distillation
The distillation of algal oil hydrolysate was performed in a short-path distillation 30 column. The temperature of the algal oil hydrolysate was 45 °C in the beginning of the distillation and it was gradually increased to 265 °C. During the distillation the pressure of the distillation equipment was 2.8 mbar in the beginning and gradually lowered to 1.9 mbar.
During the distillation six separate distillate fractions were taken. The separate 5 samples from the distillation are presented in Table 1. Both the individual fractions and a combined total distillate fraction were analysed.
Table 1. Separate distillate samples and the bottom sample taken during the distillation of the algal oil hydrolysate.
Boiling point range of the fraction in atmospheric equivalent temperature, °CPercentage of the original algal oil hydrolysateDistillate sample 1163-3111.0 %Distillate sample 2311-35515.5 %Distillate sample 3355-37213.7 %Distillate sample 4372-37718.1 %Distillate sample 5377-3816.0 %Distillate sample 6381-3842.6 %Bottom>38441.0 %
20176150 prh 22 -12- 2017
Analysis
Oil samples were analysed using the following methods: metals and phosphorus were analysed using ASTM D5185-13^e1, chlorides and sulphur using determination of elemental composition by QILQUANT-XRF method, nitrogen using ASTM 15 D4629-12, chlorophyll content using AOCS Official Method Cc 13d-55 and glyceride composition using gel permeation chromatography, where the molecules are separated based on their size and molecule weight. For this gel permeation method a calibration sample is made up from DL-a-Palmitin, Dipalmitin, Glyceryl tripalmitate, Palmitic acid. Instead of this gel permeation method mono- di- and 20 triglycerides could be analysed using AOCS Recommended Practice Cd 11c-93 and free fatty acids by total acidic number using IS0660-2009.
20176150 prh 22 -12- 2017
Water phase was analysed using the following methods: metals and phosphorus were analysed using ICP-OES, nitrogen using SFS EN 12260, COD using IS015705M-2002M, TOC using SFS EN1484 (1997).
The solid material separated after the hydrolysis step was analysed for its ele5 mental composition using SEM-EDS method.
Results
The aim of hydrolysis treatment was to hydrolyse the lipids as much as possible to free fatty acids. Algal oil #1 contained initially 1 % mono-, 22 di- and 70 % triglycerides, 1% oligomers and 6 % free fatty acids. After the hydrolysis the hydro10 lysed algal oil contained 3 % mono-, 12 di- and 8 % triglycerides, 2% oligomers and 75 % free fatty acids.
This incomplete hydrolysis into free fatty acids is considered a good result in batch operation and in continuous operation a higher level of free fatty acids would be reached. This would obviously decrease the amount of the distillation 15 bottom fraction.
After hydrolysis, oil phase, water phase and precipitate were separated as described earlier. Approximately 5 % solids were formed during the hydrolysis step and the water phase contained approximately 12 % water soluble material after the water was evaporated. The oil phase was significantly purified in the hydrolysis process 20 (Table 2) due to water washing and/or thermal effects. Metals were removed by
95%, phosphorus by 99%. Chlorides were also removed effectively by 94%. The nitrogen content of the oil is reduced, but this reduction is due to the removal of small molecular size nitrogen compounds such as degradation products of amino acids.
It seems that the chlorophyll content of the oil is reduced, but actually the chlorophyll is changed in a form that cannot be detected using the spectrographic analytical method (AOCS Official Method Co 13d-55). Although the fat splitting process has altered chlorophyll so that it cannot be analysed, the fat splitting process has not degraded the four membered porphyrin ring structure of chlorophyll that is highly stable and has a high molecular size leading to catalyst deactivation. In order to remove this high molecular weight component with a large size, the distillation step is needed.
The results after the distillation are presented in Table 3 and Table 4. Table 3 shows the analyses of the individual distillates and Table 4 shows the analyses of the bottom fraction and the combined total distillate fraction. The removal of the high molecular weight chlorophyll or chlorophyll originating components from the 5 free fatty acid fractions can be seen from the reduction of the nitrogen content, total lack of chlorophyll as analysed by AOCS Official Method Co 13d-55 and further from the colour of these fractions. The poor applicability of the chlorophyll method AOCS Official Method Co 13d-55 to analyse chlorophyll after thermal processing can be seen from the chlorophyll results of the bottom, which io obviously contains the high molecular weight porphyrin ring structures.
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Table 2. Elemental impurities in feed and oily phase after hydrolysis.
Algal oil #1 prior to hydrolysisAlgal oil #1 hydrolysisafter Unit 15Simg/kg32.51.7 Almg/kg4.30.7 Femg/kg122116 Namg/kg126035.7 Camg/kg2257.4 Mgmg/kg23609.5 Pmg/kg394027.4 Mnmg/kg16.20.4 Clmg/kg217014020Smg/kg23801200 Nmg/kg61004000 Total chlorophyllmg/kg25633414
Table 3. Analyses of the individual distillate fractions.
Distillate fraction 1Distillate fraction 2Distillate fraction 3Distillate fraction 4Distillate fraction 5Distillate fraction 6Nmg/kg65005803003908601500Monog lyse rides%not analyzed0.30.40.81.82.9Diglyserides%not analyzed0.10.10.30.81.9Triglyserides%not analyzed<0.1<0.1<0.1<0.10.1Fattyacids%not analyzed99.699.598.997.495.1Simg/kg299.6130.651.1107181Almg/kg<0.3<0.3<0.3<0.3<0.3<0.3Femg/kg<0.10.3<0.1<0.1<0.1<0.1Namg/kg<1.011.8<1.0<1.04.83.3Camg/kg<0.31.5<0.3<0.3<0.3<0.3Mgmg/kg<0.36.9<0.3<0.3<0.3<0.3Mnmg/kg<0.3<0.3<0.3<0.3<0.3<0.3Pmg/kg1426.7<0.6<0.6<0.6<0.6Smg/kgnot analyzed160100140300580Clmg/kgnot analyzed25540201525Total chlorophyllmg/kg<10<10<10<10<10<10
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Table 4. Analyses of the distillation bottom and the combined distillate fraction analyses.
Feed for distillationBottom phaseCombined distillate fractions Unit Nmg/kg40009000631.3Almg/kg0.71.5<0.3Femg/kg1162980.1Namg/kg35.7913.9Nimg/kg11.930.3<0.5Camg/kg7.415.70.4Mgmg/kg9.519.61.9Pmg/kg27.456.37.5Znmg/kg2.73.2<0.5Clmg/kg140<1088.0Smg/kg12001400170.2Total chlorophyllmg/kg414<10<10
The water phase recovered after hydrolysis step contained mostly of glycerol, but also some of the metal impurities end up in the water phase (Table 5).
The solid material removed after the hydrolysis step contained mostly magnesium phosphates.
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Table 5. Analysis results for water phase after hydrolysis.
Water phase recovered after hydrolysisAlmg/kg0.66Femg/kg0.95Mgmg/kg990Mnmg/kg4.97Namg/kg1420Camg/kg47.7Pmg/kg19.3Nmg/l1800CODmg/l130000TOCmg/l C44800
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As the Example indicates the phase separation of the 100 % algal oil after hydrolysis is highly difficult. The Example also indicates that hydrolysis step is able 5 to remove major portion of elemental impurities due to water washing and/or thermal effects as a solid material or as water soluble material. The quality of the hydrolysed oil fraction can be further increased by distilling the fatty acids, which removes the chlorophyll.
Example 2 - processing of pre-treated algal oil io In Example 1 100 % algal oil #1 was used as the raw material and the phase separation after hydrolysis was seen to be difficult. Further tests to examine the effect of conventional pre-treatment on phase separation with 100 % algal oil was experimented. These experiments were done using algal oil #2 that was produced as described in the chapter Materials in Example 1. For the experiments this algal oil was hydrolysed either as 100 % algal oil or 100 % algal oil after double degumming.
The hydrolysis of the algal oil was done described in the chapter Hydrolysis in Example 1. After the hydrolysis the separation of the phases was experimented by sedimentation in oven heated to 65 C and if no phase separation could be 20 seen centrifugation (40 °C/ 4400 rpm/15 min) was tried.
Degumming
The double degumming pre-treatment of the algal oil #2 was performed by heating the algal oil to 60 °C, blending 4000 ppm of 50 wt-% citric acid to the algal oil using a high-speed mixing for 2 minutes and low speed mixing for 15 25 minutes. After this 2 wt-% of deionized water was added and the mixture was mixed for 2 minutes using a high-speed mixing for 2 minutes and low speed mixing for 60 minutes. After this the mixture was centrifuged (60 °C/30 min/4300 rpm) and an oily phase was separated from the solid gums phase. In order to obtain double degumming the same procedure was done twice.
When fat splitting was performed on crude algal oil #2 it was seen that the oil and water phases were difficult to separate and even centrifugation in elevated temperatures was not able to separate all of the water from the oil.
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Hydrolysis of 100 w-% twice degummed algal oil #2 did not help in the phase separation. The phase separation was extremely difficult and again centrifugation at elevated temperature was not able to separate all of the water from the oil.
These difficulties were unexpected as the twice water degummed oil contained considerably less impurities than the crude oil. Conventional fat splitting processes are usually specified to be able to handle fats with <200 mg/kg phosphorus, because higher amounts of phospholipids can increase viscosity and create emulsions. Based on this it seems that the algal oil contains some additional emulsifying components that cannot be removed by water degumming.
io Example 3 - processing of algal oil blended in other fats
Examples and 1 and 2 showed that the phase separation after hydrolysis of either 100 % crude algal oil or twice degummed algal oil is highly difficult. After these experiments the hydrolysis of algal oil was tested in blends with other fats.
These experiments were done using algal oil #3 that was produced as described 15 in the chapter Materials in example 1. For the experiments this algal oil was hydrolysed as 100 % crude algal oil and blended in rendered animal fat (AF) and in a mixture of crude palm oil (CPO) and palm fatty acid distillate (PFAD) (40 wt% CPO and 60 wt-% PFAD in the mixture). The algal oil amount in the blend with CPO/PFAD was 10 wt-% and in the AF blend 10, 50 or 80 wt-%.
The hydrolysis of the algal oil and fat blends was done as described in the chapter Hydrolysis in Example 1. After the hydrolysis the separation of the phases was experimented by sedimentation in oven heated to 65 °C and if no phase separation could be seen centrifugation (40 °C/ 4400 rpm/ 15 min) was tried.
With CPO/PFAD blending tests both raw and degummed algal oils were tested. Both crude algal oil and degummed algal oil were used. The degumming was performed as described in the chapter Degumming in Example 2. The phase separation results were improved with both the crude and degummed algal oil blends and simple settling could be used to separate the two phases.
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With AF blending tests only crude algal oil was tested. With 10 wt-% algal oil blend the phase separation was fast and simple settling could be used to separate the two phases.
With the 50 w-% algal oil blend the settling was not as quick, but two phases 5 could be identified after the sample had settled at 80 °C overnight. This separation could be improved by centrifugation.
With the 80 w-% algal oil blend the settling did not lead to separation of any phases and only centrifugation was able to separate the phases.
When using 100 w-% algal oil in hydrolysis, even centrifugation was not effective io in separating the phases.
In this example it was shown that fat splitting of algal oils requires blending, because of the otherwise difficult phase separation. The reason behind the difficult phase separation is unknown, but without being bound to any theory this is most likely linked to the non-fatty acid part of the algal oils that usually ranges 15 between 15 and 40 w-%.
Different non-binding aspects and embodiments of the present invention have been illustrated in the foregoing. The above examples and embodiments are used merely to explain selected aspects or steps that may be utilized in 20 implementations of the invention. Some embodiments and examples may be presented only with a reference to certain aspects or embodiments of the invention. It should be appreciated that the corresponding embodiments and examples may apply to other aspects and embodiments as well. Any appropriate combinations of the embodiments may be formed.

权利要求:
Claims (14)
[1] Claims
1. A process for production of free fatty acids, the process comprising the steps of:
a. Providing a feedstock comprising a blend of: oil comprising
5 chlorophyll and fat;
b. Hydrolysing the feedstock to obtain at least an oily phase;
c. Recovering the oily phase; and
d. Distilling the oily phase for recovering free fatty acids contained therein.
io
[2] 2. The process of claim 1 wherein in the oil comprising chlorophyll the total content of free fatty acids, monoglycerides, diglycerides and triglycerides as analysed by ISO 15304M-2002 is lower than 90% w/w.
[3] 3. The process of claim 1 or 2 wherein the fat is animal fat, vegetable oil, or a mixture thereof.
15
[4] 4. The process of any one of claims 1-3 wherein the feedstock contains less than 50 % w/w oil comprising chlorophyll.
[5] 5. The process of claim 4 wherein the feedstock contains 1-45 % w/w, preferably 5-45 % w/w, more preferably 5-35 % w/w, and most preferably 5-15 w/w oil comprising chlorophyll.
20
[6] 6. The process of any one of claims 1-5 wherein hydrolysing is carried out at a temperature selected from a range between 220 and 280 °C.
[7] 7. The process of any one of claims 1-6 wherein the step c. further comprises separating an aqueous phase and a solid phase.
[8] 8. The process of any one of claims 1 -7 wherein in the step d. the distilling is
25 carried out at a temperature selected from the range between 220 and 300 °C and a pressure selected from the range between 0.01 and 50 kPa (given as an absolute pressure) to recover a fraction comprising free fatty acids.
[9] 9. The process of any one of claims 1-8 wherein the feedstock comprises at least lOOOppm total chlorophyll.
[10] 10. The process of any one of claims 1-9 wherein the feedstock comprises at least lOOOppm phosphorus.
[11] 11. A free fatty acid fraction obtained by the process of claims 1 -10 comprising at least 95% free fatty acids having carbon number C14-C28.
5
[12] 12. A method of producing renewable fuel comprising the steps of:
io
a. Providing a feedstock comprising a blend of: oil comprising chlorophyll and fat;
b. Hydrolysing the feedstock to obtain at least an oily phase;
c. Recovering the oily phase;
d. Distilling the oily phase for recovering free fatty acids contained therein; and
e. Subjecting the recovered free fatty acids to chemical reactions to generate hydrocarbons or alkylesters of fatty acids, wherein the free fatty acids are optionally used as: a co-feed in fuel production, 15 as the only feed in fuel production, and/or the fuel obtained from the free fatty acids is used in a blend with another fuel;
whereby renewable fuel is produced.
[13] 13. The method of claim 12 wherein in the oil comprising chlorophyll the total content of free fatty acids, monoglycerides, diglycerides and triglycerides 20 as analysed by ISO 15304M-2002 is lower than 90% w/w;
[14] 14. A method of removing chlorophyll from a feedstock comprising:
20176150 prh 22 -12- 2017
a. Providing a feedstock comprising a blend of: oil comprising chlorophyll and fat;
b. Hydrolysing the feedstock to obtain at least an oily phase;
c. Recovering the oily phase; and
d. Distilling the oily phase.

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同族专利:

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公开号 | 公开日

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CN111527188A|2020-08-11|

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IL275064D0|2020-07-30|

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EP3728534A1|2020-10-28|

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CA3085249A1|2019-06-27|

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FI128587B|2020-08-31|

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BR112020012688A2|2020-11-24|

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US20200392426A1|2020-12-17|

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WO2019122519A1|2019-06-27|

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SG11202005006XA|2020-07-29|

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CA3085249C|2021-07-06|

引用文献:

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公开号 | 申请日 | 公开日 | 申请人 | 专利标题

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US7560579B2|2003-07-10|2009-07-14|Oleon N.V.|Process for preparing purified fatty acids|

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US8563792B2|2008-12-16|2013-10-22|Cetane Energy, Llc|Systems and methods of generating renewable diesel|

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WO2013104660A1|2012-01-13|2013-07-18|Dupont Nutrition Biosciences Aps|Process for treating a plant oil comprising hydrolysing chlorophyll or a chlorophyll derivative and involving partial caustic neutralisation|

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UY35604A|2013-06-11|2015-01-30|Renewable Energy Group Inc|? THE METHODS AND DEVICES TO PRODUCE BIODIESEL AND PRODUCTS OBTAINED FROM THE SAME ?.|

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法律状态:
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优先权:

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FI20176150A|FI128587B|2017-12-22|2017-12-22|A process for producing free fatty acids|FI20176150A| FI128587B|2017-12-22|2017-12-22|A process for producing free fatty acids|

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BR112020012688-8A| BR112020012688A2|2017-12-22|2018-12-17|process for the production of free fatty acids|

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SG11202005006XA| SG11202005006XA|2017-12-22|2018-12-17|A process for producing free fatty acids|

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CN201880081995.5A| CN111527188A|2017-12-22|2018-12-17|Method for producing free fatty acid|

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PCT/FI2018/050934| WO2019122519A1|2017-12-22|2018-12-17|A process for producing free fatty acids|

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EP18839676.6A| EP3728534A1|2017-12-22|2018-12-17|A process for producing free fatty acids|

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CA3085249A| CA3085249C|2017-12-22|2018-12-17|A process for producing free fatty acids|

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US16/955,913| US20200392426A1|2017-12-22|2018-12-17|A process for producing free fatty acids|

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IL275064A| IL275064D0|2017-12-22|2020-06-02|A process for producing free fatty acids|