Patent Application
20220267697
The present invention relates to a method for the separate extraction of rice bran oil and wax according to claim 1.
Rice bran is a by-product of the rice milling industries and contains 10-26% oil depending on the variety, milling process, and other agro-climatic conditions. Rice bran contains proteins, free fatty acids, glycerides, sterols, and polysaccharides. Recently, it has received some attention because of its unique health benefits that may be attributed to the nutritionally important compounds, such as tocopherols, tocotrienols, sterols and especially the unique antioxidant oryzanol, present in it.
Despite its high potential for use applications in food, pharmaceutical, cosmetics and chemical industries, effective large-scale production of rice bran oil is limited due to the high costs involved with the extraction of the oil as compared to other vegetable oils.
Firstly, the rice bran from rice milling processes needs to undergo a stabilization process to inactivate the enzymes and inhibit lipid oxidation. This stabilization is essential to prevent the deterioration of fat and valuable bioactive compounds of the bran. For commercial extraction of the rice bran oil, solvent extraction using hexane is the most popular used conventional method these days. Apart from recovering triglycerides and sterols from rice bran oil the extraction process also aims at limiting the recovery of free fatty acid (FFA) in crude oil. Minimizing the FFA content in refined rice bran oil is essential to achieve good stability and colour quality, yet this task is difficult to achieve with a liquid extracting agent, such as hexane, because solubility for specific group components of oilseed lipids (such as FFA) cannot be controlled. In addition, the use of hexane has further drawbacks due to its flammability, toxicity and high temperature involved in the process resulting in some undesirable components in the oil as a result of oxidative deterioration, developments of rancid and off-flavour.
Efforts have thus been made by many researchers to explore different other nonconventional techniques for the oil extractions and utilization. Some of these methods such as supercritical carbon dioxide extraction, subcritical water extraction, enzyme-assisted, ultrasonic-assisted and microwave-assisted processes.
Sparks et al. 2006 (JAOCS, Vol. 83, No.10) disclosed a method for small scale rice bran oil extraction using a batch of 40 g of rice bran and supercritical CO2 as extraction medium at 20-30 MPa and 45-85° C. The oil is separated from the supercritical CO2 through passing a cyclone.
However, low yields and high costs have so far limited the use of these alternative extraction methods in large scale production of rice bran oil.
An additional obstacle is that the primary product of all known extraction methods is a mixture of rice bran oil and waxes. In order to avoid turbidity in the final product, the waxes must be separated from the rice bran oil by means of cooling and filtration. Even though the rice bran wax that is obtained thereby as “waste material” has recently found increasing industrial application in itself, e.g. as thickener, binding agent, plasticizer, cosmetics, coating and gelling agent, the dewaxing process of crude rice bran oil adds to the complexity and overall costs of rice bran oil production.
The problem solved by the present invention is thus to provide a method that allows for the separate production of rice bran oil and rice bran wax, whereby the extracted products are free from toxic residues, have high concentration of nutritionally valuable components and are obtainable in a yield comparable to the conventional techniques.
This problem is solved by the method according to claim 1. Preferred embodiments are subject to the dependent claims.
Specifically, the present invention provides a method that allows for the separate extraction of rice bran oil and rice bran wax from rice bran. The method comprises the steps of
In the context of the present application, the following definitions apply:
The term “first product” as used throughout this application refers to a precipitate from the extract (comprising inter alia rice bran oil and rice bran waxes in supercritical CO2) at the extraction pressure p1 and the extraction temperature T1. Depending on the values of p1 and T1 the composition of the first product can vary but contains rice bran oil, preferably as a main component.
The term “supercritical CO2” as used throughout this application refers to a fluid state of carbon dioxide where it is held at or above its critical temperature of 31° C. and critical pressure of 74 bar.
The term “rice bran” as used throughout this application refers to the hard-outer layers of a rice grain. It consists of the combined aleurone and pericarp. Along with germ, it is an integral part of whole grains, and is often produced as a by-product of milling in the production of refined grains.
The term “extraction vessel” as used throughout this application refers to a container that is high pressure resistant (above 1000 bar) and in which the supercritical CO2 can be intermixed with the rice bran.
The inventors of the presented method have surprisingly found that rice bran oil and rice bran wax can be selectively separated from an extract comprising the two components in supercritical CO2 as extraction medium by adjusting the temperature and pressure within specific ranges. For instance, by reducing the pressure to the first separation pressure p2 in step b) of the inventive method, a first product comprising rice bran oil can be precipitated from the extract laden supercritical CO2, while at least most of the solubilized rice bran wax can be retained in the supercritical CO2. Thereafter, a further reduction of the pressure to a second separation pressure p3 causes the supercritical CO2 to change to gaseous CO2 and a subsequent separation of a second product comprising rice bran wax of from the gaseous CO2. Thus, the inventive method provides the benefit of a separate extraction of rice bran oil and rice bran wax.
Using carbon dioxide as a solvent is highly convenient thanks to its moderate critical pressure and temperature. Moreover, carbon dioxide is a non-toxic inexpensive and environmentally friendly solvent.
In a preferred embodiment of the invention the extraction pressure p1 for the extraction step a) is within the range of 100 and 600 bar, preferably within the range of 150 to 600 bar, preferably 300 to 600 bar, and most preferably about 550 bar.
Preferably the extraction temperature T1 for the extraction step a) is within the range of 50° C. to 80° C., more preferably 55° C. to 65° C. and most preferably about 60° C.
Within the above-defined ranges for the extraction pressure p1 and the extraction temperature T1, an increased amount of rice bran oil and rice bran wax can be extracted from rice bran with supercritical CO2.
In a preferred embodiment of the invention the first separation step b) is conducted at a first separation temperature T2 that is higher than the extraction temperature T1 of extraction step a).
Preferably said first separation temperature T2 is at least 65° C., more preferably within the range of 70° C. to 80° C. and most preferably about 75° C.
It was found that at a constant pressure, increasing the temperature decreases the solubility of solutes (i.e. the rice bran extract) because the density of the supercritical CO2 decreases. For that reason, the temperature increase from the extraction temperature T1 to first separation temperature T2 causes the rice bran oil to condense and starts precipitation of the rice bran oil from the extract—which can then be collected as the first product.
In a preferred embodiment of the invention the first separation pressure p2 for the first separation step b) is set below 230 bar, preferably below 200 bar, more preferably within the range of 170 to 190 bar and most preferably to about 180 bar.
In the context of the present invention, it has surprisingly been found that reducing the extraction pressure p1 to the first separation pressure p2 allows for an effective separation of the first product containing rice bran oil from the extract.
Preferably the second separation pressure p3 for the second separation step c) is set below 73.8 bar, preferably below 65 bar and most preferably to about 60 bar.
The reduction of the second separation pressure p3 below 73.8 bar leads to a change of state of the CO2 from supercritical to gaseous, which was found to facilitate precipitation of the second product.
In a preferred embodiment of the invention the second separation step c) is preferably conducted at a second separation temperature T3 that is lower than extraction temperature T1 of extraction step a).
Preferably said second separation temperature T3 is set below 70° C., preferably below 60° C., more preferably within the range of 45° C. to 55° C. and most preferably about 50° C.
The above temperature ranges for the second separation step lead to an increased yield of rice bran wax. Preferably, the reduction of pressure and temperature is achieved without the use of external energy, e.g. by means of simply opening a valve to decrease pressure, which in turn leads to a temperature reduction. Thereby, the energy consumption of the inventive process can be effectively reduced.
In a preferred embodiment of the invention the extraction step a) is conducted with a solvent/feed ratio within the range of 25 to 45, preferably 30 to 40 and most preferably about 36 to maximise the overall yield of rice bran oil and rice bran wax.
The term “solvent/feed ratio” as used throughout this application refers a ratio of supercritical CO2 and rice bran. For example, a solvent/feed ration of 2 indicates that there is twice as much supercritical CO2 than rice bran in the incubation vessel of step a).
In a preferred embodiment of the invention the process further includes a recovery step d) that is conducted after the second separation step c) and in which the temperature of the gaseous CO2 is decreased to a recovery temperature T4, at which the gaseous CO2 condenses to a liquid state. The recovery temperature T4 is preferably at most 30° C., preferably within the range of 20° C. to 30° C. and most preferably about 25° C.
Preferably, after the recovery step d), the pressure and the temperature of the liquid CO2 is increased to extraction pressure p1 and extraction pressure T1, such that the liquid CO2 is brought into supercritical state and can be re-used in extraction step a).
In an alternative preferred embodiment of the invention the gaseous CO2 of step c) is brought directly to supercritical state at temperature T1 and pressure p1 and is reused in step a).
The invention will be further explained based on the attached figures. It will be understood that these figures are intended to describe illustrative embodiments of the invention and are not intended to limit the scope of the invention in any way.
The above changes of CO2's aggregation states are utilized in the method of the present invention: For the extraction step a) of the inventive process, CO2 is brought to supercritical state 111 at the extraction pressure p1 112 and the extraction temperature T1 113. In the first separation step b), the pressure of the supercritical CO2 111 is lowered to the first separation pressure p2 and the temperature is increased to the first separation temperature T2 114, 115. During the second separation step c), the pressure and the temperature are lowered to the second separation pressure p3 and the second separation temperature T3 116, 117, respectively, at which the CO2 changes to a gaseous state 103. In the recycling step d), the temperature of the gaseous CO2 is further reduced to the recovery temperature T4 119, at which the CO2 changes to a liquid state 105. The liquid CO2 can then be reused for the extraction in the extraction step a) by increasing the temperature and pressure to the extraction pressure p1 and extraction temperature T1 112, 113, respectively, to bring the CO2 into supercritical state 111 again.
Raw stabilized rice bran (10 kg from FortiBran® as FORTIVIA® N° 09-050-2019-22) was introduced in an extraction basket, then placed in an extractor. The extractor was pressurized to an extraction pressure p1 of 280 bar. Supercritical CO2 (267 kg) was percolated through the raw rice bran in the extractor at the extraction pressure and at an extraction temperature T1 of 60° C. The solvent/feed ratio was 36.
In Example 1, the rice bran contained an initial oil/wax content of 15% oil and 3% waxes.
The supercritical CO2 and the extract solubilized therein were transferred to a first separation vessel. The pressure was reduced to a first separation pressure p2 of 180 bar and the temperature was increased to a first separation temperature T2 of 75° C. This caused rice bran oil to precipitate from the supercritical CO2 and was collected at the bottom of the separation vessel.
The supercritical CO2 and remaining extract were transferred to a second separation vessel and the pressure was reduced to a second separation pressure p3 of 60 bar and the temperature was reduced to a second separation temperature T3 of 50° C. At these conditions, rice bran wax precipitated (mostly in liquid state) from gaseous CO2 and was collected at the bottom of the second separation vessel.
The first and second products comprising rice bran oil and rice bran wax were collected in separators in real time. After separation, water was removed from the precipitated products by decantation at 70° C.
Yields of rice bran oil were determined by gravimetry and other analytical methods including fatty acid titration.
Yield of the collected rice bran oil and rice bran wax after decantation and water removal was 15% and 3%, respectively. Total yield of rice bran oil and wax was thus 18%.
The conditions and yields of Example 1 are summarized in Table 1 below:
Raw stabilized rice bran (FortiBran®—long grain rice type A Rombo, stabilized by vapor at 8 bar during 30 seconds, (by FORTIVIA®)) was used as starting material.
Preliminary note: The contents of rice bran oil and wax can vary quite significantly. The rice bran used for Example 2 had the same rice bran oil content as the one used for Examples 1 and 3, namely 15%, yet the initial rice bran wax content was found to be significantly lower, namely merely 0.5% instead of 3%.
In Example 2, the extraction and separation steps were carried out same way as for Example 1, yet with the conditions indicated in Table 2 below. The purpose of this Example 2 was to verify that a separate extraction of rice bran oil and rice bran wax was possible with a very low pressure and temperature. For this purpose, only a small fraction of rice bran oil was actually extraction and collected in the 1st separation stage. In the 2nd separation stage, it was tried to extract and separate as much rice bran wax as possible.
The conditions and yields of Example 2 are summarized in Table 2 below:
It was found that a separate extraction of rice bran oil and wax was possible under low pressure and temperature conditions (100 bar and 35° C.).
(**)While only a fraction of light rice bran oils was actually separated and collected during the first separation stage (0.55% of overall 15%), it could be verified that separation and extraction of essentially all rice bran wax contained in the raw rice bran was possible (0.45% of overall 0.5%).
Raw stabilized rice bran (from FortiBran® as FORTIVIA® N° 09-050-2019-22) was used as starting material (i.e. the same as in Example 1). The rice bran contained an initial oil/wax content of 15% oil and 3% waxes.
In Example 3, the extraction and separation steps were carried out same way as for Example 1, yet with the conditions indicated in Table 3 below.
The conditions and yields of Example 3 are summarized in Table 3 below:
It was found that at high pressure and a smaller solvent/feed ratio, a higher overall extraction yield was obtained (total 20% instead of 18%). It is assumed that all rice bran oil and waxes were extracted, yet together with some other compounds that were not co-extracted at lower pressure. This assumption is based on the observance that rice bran oil was effectively collected during the 1st separation stage, together with some other compounds, inter alia pigments and polar lipids. All waxes were collected during the 2nd separation stage.
| Number | Date | Country | Kind |
|---|---|---|---|
| 19187069.0 | Jul 2019 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2020/070245 | 7/17/2020 | WO |
