GB2558977A - Method for production of fatty acids - Google Patents
Method for production of fatty acids Download PDFInfo
- Publication number
- GB2558977A GB2558977A GB1714542.6A GB201714542A GB2558977A GB 2558977 A GB2558977 A GB 2558977A GB 201714542 A GB201714542 A GB 201714542A GB 2558977 A GB2558977 A GB 2558977A
- Authority
- GB
- United Kingdom
- Prior art keywords
- saponification
- reactor
- specified
- fatty acids
- electrode
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 150000004665 fatty acids Chemical class 0.000 title abstract description 20
- 235000014113 dietary fatty acids Nutrition 0.000 title abstract description 19
- 239000000194 fatty acid Substances 0.000 title abstract description 19
- 229930195729 fatty acid Natural products 0.000 title abstract description 19
- 238000007127 saponification reaction Methods 0.000 claims abstract description 60
- 238000000034 method Methods 0.000 claims abstract description 54
- 239000000463 material Substances 0.000 claims abstract description 42
- 235000021588 free fatty acids Nutrition 0.000 claims abstract description 31
- 239000002253 acid Substances 0.000 claims abstract description 11
- 230000007935 neutral effect Effects 0.000 claims abstract description 5
- 239000000344 soap Substances 0.000 claims description 51
- 150000003904 phospholipids Chemical class 0.000 claims description 21
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical group Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 10
- 239000003784 tall oil Substances 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 5
- 239000004020 conductor Substances 0.000 claims description 5
- 235000011149 sulphuric acid Nutrition 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 239000010439 graphite Substances 0.000 claims description 4
- 229910002804 graphite Inorganic materials 0.000 claims description 4
- 239000001117 sulphuric acid Substances 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims 2
- 239000003921 oil Substances 0.000 description 29
- 235000019198 oils Nutrition 0.000 description 29
- 150000002632 lipids Chemical class 0.000 description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 27
- 239000000203 mixture Substances 0.000 description 18
- 239000000047 product Substances 0.000 description 16
- 125000005456 glyceride group Chemical group 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 229910001868 water Inorganic materials 0.000 description 10
- 150000003839 salts Chemical class 0.000 description 9
- 239000004359 castor oil Substances 0.000 description 7
- 235000019438 castor oil Nutrition 0.000 description 7
- ZEMPKEQAKRGZGQ-XOQCFJPHSA-N glycerol triricinoleate Natural products CCCCCC[C@@H](O)CC=CCCCCCCCC(=O)OC[C@@H](COC(=O)CCCCCCCC=CC[C@@H](O)CCCCCC)OC(=O)CCCCCCCC=CC[C@H](O)CCCCCC ZEMPKEQAKRGZGQ-XOQCFJPHSA-N 0.000 description 7
- 238000006386 neutralization reaction Methods 0.000 description 7
- 239000011541 reaction mixture Substances 0.000 description 7
- 150000003626 triacylglycerols Chemical class 0.000 description 7
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000010779 crude oil Substances 0.000 description 4
- 238000006073 displacement reaction Methods 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 239000000523 sample Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 241001465754 Metazoa Species 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 235000011187 glycerol Nutrition 0.000 description 3
- WBHHMMIMDMUBKC-XLNAKTSKSA-N ricinelaidic acid Chemical compound CCCCCC[C@@H](O)C\C=C\CCCCCCCC(O)=O WBHHMMIMDMUBKC-XLNAKTSKSA-N 0.000 description 3
- 229960003656 ricinoleic acid Drugs 0.000 description 3
- FEUQNCSVHBHROZ-UHFFFAOYSA-N ricinoleic acid Natural products CCCCCCC(O[Si](C)(C)C)CC=CCCCCCCCC(=O)OC FEUQNCSVHBHROZ-UHFFFAOYSA-N 0.000 description 3
- -1 triglycerides) Chemical class 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 239000002655 kraft paper Substances 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000004537 pulping Methods 0.000 description 2
- 238000012552 review Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 235000015112 vegetable and seed oil Nutrition 0.000 description 2
- 239000008158 vegetable oil Substances 0.000 description 2
- 239000001993 wax Substances 0.000 description 2
- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229920002488 Hemicellulose Polymers 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 description 1
- 229930182558 Sterol Natural products 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 239000010775 animal oil Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- OGBUMNBNEWYMNJ-UHFFFAOYSA-N batilol Chemical class CCCCCCCCCCCCCCCCCCOCC(O)CO OGBUMNBNEWYMNJ-UHFFFAOYSA-N 0.000 description 1
- 238000004061 bleaching Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000013068 control sample Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 150000002148 esters Chemical group 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 159000000011 group IA salts Chemical class 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 239000000123 paper Substances 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000012163 sequencing technique Methods 0.000 description 1
- 239000002195 soluble material Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 150000003432 sterols Chemical class 0.000 description 1
- 235000003702 sterols Nutrition 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 description 1
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/02—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils
- C11C1/025—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils by saponification and release of fatty acids
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
- C11B13/02—Recovery of fats, fatty oils or fatty acids from waste materials from soap stock
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process for production fatty acids comprising: adjusting pH of a saponifiable material to a value above pH 7 by adding alkaline material; saponifying all saponifiable material by passing alternate electrical current through the material, wherein the said step of saponification occurs in a saponification reactor; acidulating the saponified material by adding acid to pH value below 4; isolating obtained free fatty acids from aqueous layer. The saponification reactor can be an ohmic heater. Also claimed is a saponification reactor comprising at least two electrodes contained within a cylindrical vessel having inlet and outlet ports at opposite ends; wherein one electrode is electrically and mechanically connected with the vessel wall and is a neutral point connected to earth; wherein the second electrode is electrically isolated from the first electrode and is connected to a single phase of an electric power supply. A reactor assembly comprising three saponification reactors connected in series or in parallel is also disclosed.
Description
(54) Title of the Invention: Method for production of fatty acids Abstract Title: Method for production of fatty acids (57) A process for production fatty acids comprising: adjusting pH of a saponifiable material to a value above pH 7 by adding alkaline material; saponifying all saponifiable material by passing alternate electrical current through the material, wherein the said step of saponification occurs in a saponification reactor; acidulating the saponified material by adding acid to pH value below 4; isolating obtained free fatty acids from aqueous layer. The saponification reactor can be an ohmic heater. Also claimed is a saponification reactor comprising at least two electrodes contained within a cylindrical vessel having inlet and outlet ports at opposite ends; wherein one electrode is electrically and mechanically connected with the vessel wall and is a neutral point connected to earth; wherein the second electrode is electrically isolated from the first electrode and is connected to a single phase of an electric power supply. A reactor assembly comprising three saponification reactors connected in series or in parallel is also disclosed.
Production of Free Fatty Acids from Soapstock
Figure 1
- Soapstock tank; 2 ~ positive displacement pump; 3 -- reactor; 4 -- pressure regulation means; 5 - clarifier; 6 - finished product tanker
At least one drawing originally filed was informal and the print reproduced here is taken from a later filed formal copy.
1/2
CO
Drawings o
+J to
Giro
O to
E o
to <
>>
ω <u
- Soapstock tank; 2 - positive displacement pump; 3 - reactor; 4 - pressure regulation means; 5 - clarifier; 6 - finished product tanker
2/2
Figure 2
Saponification reactor
11 17 _3{P)
AC 10-1500 V
N | 2 | ||||||||
1 | product | ||||||||
7 / | X7 | \ 3(T) | |||||||
4 | / / | / / / / / | 3 | / / | 4 | ||||
5 | z / / | electric | X / / | ||||||
/ / / / / / | 7 / / / / Lz | / / / / X / | Vertical reactor | ||||||
t | 2 |
raw material
- pressure vessel (housing); 2 - hydraulic connections; 3 (P) - pressure sensor; 3 (T) - temperature sensor; 4 - zero/neutral) electrode; 5 -rod (pipe) phase electrode.
METHOD FOR PRODUCTION OF FATTY ACIDS
BACKGROUND
a. Field of the Invention
The present invention generally provides a process for treating a soapstock.
This invention particularly provides a systems and methods for realising the full free fatty acid yield of a soapstock by first converting substantially all of the saponifiable material in a soapstock to salts of fatty acids (soaps) and acidulating the soaps to generate free fatty acids, wherein the soapstock comprises soaps, saponifiable lipids, e.g. glycerides and phospholipids and the generating of free fatty acids is achieved by passing an alternating electric current through a soapstock.
Yet another aspect of the present invention relates to a reactor for treating the soapstock.
b. Related Art
Crude (unrefined) animal and vegetable oils (referred to herein collectively as natural oils) are typically subjected to a variety of processing steps to remove specific undesirable components of the crude oil prior to sale. The type, number, and sequencing of processing steps can vary depending on the crude oil feedstock, refinery type (e.g. physical vs. alkaline) and configuration, target product markets, and the like. In general, crude natural oils are refined to remove excess quantities of gums (comprised primarily of phospholipids), free fatty acids, as well as various colouring components and volatile compounds.
-2In most natural oil refineries utilizing the chemical refining process, phosphoric acid or an equivalent acid is added to the crude oil to increase the solubility of the phospholipids (gums) in water. Next, a strong base, typically sodium hydroxide (NaOH) is added, reacting with the free fatty acids in the oil to form soaps (salts of free fatty acids). Water is then added to the oil to remove the soaps and solubilized gums. Soapstock is typically acidulated to generate free fatty acids. Gums are typically sold into low-value animal feed markets
US patent 9546342 describes a process for treating a soapstock. The mixed lipid 10 feedstock is combined with a base to form a first mixture. The first mixture is allowed to react. Carbon dioxide is introduced into the reacted mixture in the reaction vessel to form a first carbonic acid within the reaction vessel. The first carbonic acid is mixed with the reacted mixture within the reaction vessel. The first carbonic acid and reacted mixture are allowed to settle within the reaction vessel.
A first aqueous layer is drained from the reaction vessel, thereby acidulating soaps in the first mixture to generate free fatty acids.
However, the method cited above requires quite substantial reaction time. The first step only proceeds for 4 hours that makes this method hardly suitable for continuous production.
SUMMARY OF THE INVENTION
Aspects of the invention are specified in the independent claims. Preferred features are specified in the dependent claims.
-3The object of the present invention to provide an improvement which overcomes the inadequacies of the prior art methods and devices and which is a significant contribution to the advancement to realizing the full fatty acid yield of saponifiable material.
-4BRIEF DESCRIPTION OF THE DRAWINGS
The present invention will now be further described, by way of example, with reference to the following figures, in which:
Figure 1 is a flow diagram of an exemplary method of the invention comprising generating free fatty acids from a mixed lipid feedstock comprising soaps, saponifiable material or equivalents thereof. The following detailed description is provided to give the reader a better understanding of certain details of aspects and embodiments of the invention, and should not be interpreted as a limitation on the scope of the invention.
Figure 2 shows the exemplary reactor schematics.
The drawings included in the present application are incorporated into, and form part of the specification. They illustrate embodiments of the present disclosure and, along with the description, serve to explain the principles of the disclosure. The drawings are only illustrative of certain embodiments and do not limit the disclosure.
DEFINITIONS
As used herein, the term saponifiable material is intended to mean by product streams of natural oil processing, i.e soapstock, gums, phospholipids or mixtures
-5thereof, glycerides (mono- di- and triglycerides), black liquor soaps or tall oil soaps.
DETAILED DESCRIPTION
In alternative embodiments, the invention provides processes for the preparation 5 of fatty acids from mixed lipid feedstocks comprising saponifiable material, including by-product streams of natural oil processing e.g. soapstocks, gums, or mixtures thereof. In alternative embodiments, the feedstock comprises soapstock obtained from the alkaline neutralisation of crude natural oil. In alternative embodiments, the feedstock comprises the gums product (comprising primarily phospholipids) generated during the degumming of a natural oil. In alternative embodiments, the feedstock comprises a mixture of product streams generated during the processing of crude natural oil and comprises soaps as well as saponifiable lipids, e.g. phospholipids glycerides, e.g. mono-, di-, and/or triglycerides, or any combination thereof. In alternative embodiments, processes of the invention are more economical and efficient than currently used approaches for the treatment of natural oil processing by-products e.g. soapstocks and gums, to generate fatty acids.
The most surprising and unexpected result was that passing alternate electric current through the slightly alkaline soapstock results in the rapid saponification of triglycerides and phospholipids with the generation of alkaline salts of free fatty acids.
In alternative embodiments, a mixed lipid feedstock, e.g. a soapstock comprising soaps as well as saponifiable material (e.g. glycerides and/or phospholipids) is heated and its pH is adjusted to above 7. Thus prepared soapstock is subjected to the action of an alternative electric current and reacts with a base in a saponification reactor to convert the saponifiable material to soaps (salts of fatty acids), thereby generating a product in which substantially all of the saponifiable
-6material is converted to soaps. The soaps present in the product stream generated in the foregoing saponification step are then separated and reacted with an acid in a second acidulation step of the process in which substantially all of the soaps are acidulated to form free fatty acids (i.e. fatty acids with no ester moiety) and an inorganic sodium or calcium salt, if sodium hydroxide or calcium hydroxide are the selected bases used in the saponification step.
Crude (unrefined) natural oils, including plant- and animal-derived oils, are comprised primarily of triacylglycerols (i.e. triglycerides), as well as smaller portions of various lipids including mono- and diacyleglycerols, (i.e. mono10 glycerides and di-glycerides, respectively), free fatty acids, phospholipids, waxes, and other non-lipid components including, for example, ketones, aldehydes, and hydrocarbons. Prior to sale for human consumption or for further processing, a crude natural oil is usually refined to remove the majority of the non-triglyceride components. The majority of natural oils are refined using the chemical refining process. In the first stage of the chemical refining process, referred to as degumming, crude oils are first washed with water to remove the hydratable phospholipids (gums). The resulting product stream separated from the oil during the degumming step is referred to as gums. Second, the degummed oils are subjected to a neutralisation step in which the degummed oil is treated with a strong base, e.g. sodium hydroxide. During the neutralisation step, free fatty acids present in the oil react with the base to form soaps (salts of fatty acids). In some refineries, there is an additional processing step between the degumming and neutralisation step in which a small amount of a mineral acid, e.g. phosphoric acid or citric acid) is added to the degummed oil to convert any non-hydratable phospholipids into hydrated phospholipids. After the neutralisation step, the oil is washed to remove the soaps and, if the oil was treated with a mineral acid, the hydrated phospholipids. The resulting product stream separated from the oil during the neutralisation step is referred to as soapstock. If the oil is to be sold for
-7 human consumption, the degummed, neutralised oil is then subjected to further processing including, e.g. bleaching and deodorisation steps.
Depending on the configuration of the refinery, soapstock and gums are either stored separately or combined into a single storage container. When referred to herein, a mixed lipid feedstock refers to any material or composition comprising soaps as well saponifiable material, i.e. lipids capable of reacting to produce soaps (salts of fatty acids). Saponifiable material in the mixed lipid feedstock can include, without limitation, glycerides, e.g. mono-glycerides, di-glycerides, or triglycerides, or a combination thereof, and/or phospholipids. In alternative embodiments, the mixed lipid feedstock is a soapstock. In alternative embodiments, the mixed lipid feedstock comprises soaps and saponifiable lipids e.g. glycerides and/or phospholipids. In alternative embodiments, the mixed lipid feedstock is a mixture of soapstocks, comprising soaps, saponifiable material, e.g. glycerides and/or phospholipids, obtained during the processing of a natural oil. In alternative embodiments, the mixed lipid feedstock is a soapstock washwater obtained from the processing of a crude natural oil following the neutralisation step in the chemical refining process. In such embodiments, the washwater can comprise water and soapstock, wherein the soapstock comprises soaps, glycerides, phospholipids, free fatty acids, and unsaponifiable material e.g. waxes and/or sterols. In alternative embodiments, the soapstock washwater can comprise between about 1% soapstock to about 90% soapstock, e.g. between about 2% and 80% soapstock, about 3% and 70% soapstock, about 4% and about 60% soapstock, about 5% and about 50% soapstock, about 6% and about 40% soapstock, about 7% and about 30% soapstock, about 8% and about 20% soapstock, about 9% and about 15% soapstock, or between about 20% and about 12% soapstock, the remaining portion of the soapstock washwater comprising water. The composition of the soapstock used as a mixed lipid feedstock in accordance with the present invention can vary depending on the crude natural oil from which it was derived.
-8Other mixed lipid feedstocks suitable for use in the present process include tall oil soaps. Tall oil soaps are generated via the alkaline pulping of wood in the Kraft process. The alkaline pulping of wood using the Kraft process results in the production of black liquor, comprising the majority of the non-cellulose components of the wood. These products include hemicelluloses, lignin, and various salts of carboxylic acids including rosin salts and soaps (salts of fatty acids). After the black liquor is concentrated using multiple effect evaporators, it is allowed to settle or is centrifuged. As the concentrated black liquor settles, the soaps float to the surface where they are skimmed and removed. The skimmed product (referred to as black liquor soaps or tall oil soaps) is used as a feedstock in various embodiments of the process.
In alternative embodiments, the mixed lipid feedstock in the present process is a saponified crude natural oil, e.g. a saponified vegetable oil. In alternative embodiments, the mixed lipid feed feedstock is a saponified castor oil, i.e. a composition comprising soaps derived from mixing a base with a castor oil, the saponifiable content in the castor oil, e.g. glycerides, and phospholipids, having been converted to soaps. It is known in that the majority of the fatty acid content in castor oil (e.g. between 80 to about 95% of the fatty acid content) is ricinoleic acid (12-hydroxy-9-cz's-octadecenoic acid). In alternative embodiments, the invention provides methods or processes for generating ricinoleic acid by first saponifying a castor oil by adding a base, e.g. sodium hydroxide, to the castor oil, passing alternate electric current through the obtained mixture, acidulating the saponified castor oil to generate free fatty acids, and then separating or isolating ricinoleic acid from the generated free fatty acids.
-9FIG. 1 shows an exemplary embodiment of the process for generating free fatty acids from a soapstock. A soapstock comprising soaps and unsaponified lipids is first combined with a strong base, e.g. sodium hydroxide in the vessel 1. The resulting combination is pumped by a pump 2 to a saponification reactor 3, where it is subjected to the action of an alternate electric current wherein substantially all of the saponifiable material in the soapstock is converted to soaps, glycerine and other products. From the saponification reactor 3 the obtained mixture is directed through a pressure regulation means 4 to a clarifier 5. The steam from the clarifier is used to preheat a soapstock in the tank 1. The soaps in water are then contacted with an acid which acidulates the soaps in an acidulation reaction to generate free fatty acids.
Alternative embodiments of the methods and processes are described in greater detail bellow.
Soapstock Saponification:
In alternative embodiments, the first stage of the process is a saponification reaction with a mixed lipid feedstock under the action of an alternate electric current. In alternative embodiments, a mixed lipid feedstock, e.g. a soapstock washwater comprising water, soaps as well as saponifiable material e.g. glycerides (e.g. mono- di- or triglycerides or any combination thereof) and phospholipids, is mixed with a base, e.g. a strong base such as sodium hydroxide or potassium hydroxide, and water to generate a saponification reaction mixture. The generated saponification reaction mixture is then subjected to the action of an alternate electric current to convert substantially all of the saponifiable material in the mixed lipid feedstocks to soaps. During the saponification reaction, the base serves to cleave substantially all of the ester bonds of the saponifiable lipids
-10present in the mixed lipid feedstock and the cation (e.g. sodium, potassium or calcium) joins the fatty acid molecule to form a salt of a fatty acid (soap). The resulting product comprises soaps as well as water-soluble material e.g. glycerine.
The following is a reaction scheme showing the saponification of a glyceride molecule in the mixed lipid feedstock in an exemplary embodiment of the present invention.
XfiOH
Aits<nete diatttL errant
-continued
oi-i
-11 The following is a reaction scheme showing the saponification of a phospholipid molecule in the mixed lipid feedstock in an exemplary embodiment of the present invention.
In alternative embodiments the frequency of an alternate electric current is in the range from 50 Hz to 10,000 Hz or from 50 Hz to 1000 Hz or from 50 Hz to 60 Hz.
In alternative embodiments, the saponification reaction is carried out at a 10 temperature in the range of between about room temperature (i.e. around 20 - 25 °C) to 150 °C e.g. between 50 °C to 140 °C , 60°C. to 120 °C.
In alternative embodiments, the saponification reaction is carried out at a pressure of between 0 to 5 barg, e.g. between 1 and 4 barg, or between 1.5 psig and 3 psig.
-12In alternative embodiments, the saponification reaction is carried out at ambient pressure.
In alternative embodiments, the base used in the saponification reaction is any base of hydroxide, e.g. sodium hydroxide (NaOH), potassium hydroxide (KOH) or calcium hydroxide (Ca(OH)2).
In certain embodiments, following the saponification reaction, the resulting reaction products (i.e. the saponification product mixture) are subjected to a separation step in which the soaps are separated from the reaming reaction products, e.g. glycerine. The separation step can be any suitable separation technique known in the art, e.g. filtration, centrifugation, water washing, or any combination of separation techniques. In an exemplary embodiment, the reaction products from the saponification step are allowed to settle and then the soaps are skimmed from the surface of the mixture. In alternative embodiments, the skimmed soaps are then subjected to a water wash in which substantially all of the non-soap material is removed from the soaps.
In alternative embodiments saponification step is carried out in an ohmic heater.
In alternative embodiments saponification step is carried out in a reactor described below.
Ohmic heaters as described in the paper “A comprehensive review on applications of ohmic heating (OH)” by Mohamed Sakr, Shuli Liu published in Renewable and Sustainable Energy Reviews 39( 2014) 262-269, DOI 10.1016/j.rser.2O14.07.061 or elsewhere can be used as saponification reactors for passing alternative electric current through the soapstock. However the preferable is the reactor shown in Fig 2 and described further herein.
-13The process is preferably carried out in a continuous manner, for example, by pumping the feedstock reaction mixture through a sufficiently long ohmic heater or the reactor described below.. Alternatively, it can be carried out as a batch process.
Instead of a conventional ohmic heater described elsewhere the exemplary construction of the saponification reactor is described below.
The examplary reactor chart is shown in fig 2.
The reactor consists of a pressure vessel 1 that could be manufactured from a suitable material required to withstand pressure, (for example stainless steel 316L) with hydraulic connections 2 (in case of a continuous process) and sensors for pressure and temperature, 3. Inside this casing is a tube 4 made of electrically conductive material (steel, graphite or other analogous suitable material) connected mechanically and electrically to the casing. The diameter and length of the tube is determined by a soapstock conversion requirements. The tube 4 is a zero electrode. In the center of the reactor is placed the phase electrode 5 made of electrically conductive material (steel, graphite or other suitable material). This electrode could be a rod or a hollow pipe cooled by the converted material. This electrode is electrically isolated from the housing and internal graphite tube. For the reactor operations requiring power greater than 20kW, a three-reactor system in parallel or in series configuration is used in order to ensure a uniform load on the network.
In alternative embodiments pluralities of three reactor assemblies could be employed depending on the required capacity.
-14It will be appreciated that any suitable techniques may be employed in the process; for example as a pressure regulation means ball valves, gate valves or a positive displacement pump operating at a lower speed than positive displacement pump 2 in Figure 1 can be used. Suitable device will be well known per se to those skilled in the art.
Acidulation of Soaps:
In alternative embodiments, the soaps, or the reaction product generated during the saponification step of the process (i.e. the saponification product mixture), is subjected to an acidulation step in which substantially all of the soaps are acidulated to generate free fatty acids. The soaps are acidulated by mixing them in any suitable reaction vessel with an acid to form an acidulation reaction mixture. In alternative embodiments acid used for acidulation is hydrochloric acid (HCI) or sulphuric acid (H2SO4).
In alternative embodiments, the desired pH of the acidulation reaction mixture is below 7, i.e. in the range of 2 - 6, preferably 4.5 - 5.5.
It should be understood, however, that the intention is not to limit the invention to the particular embodiments described. On the contrary, the intention is to cover all
-15modifications, equivalents, and alternatives falling within the spirit and scope of the invention.
The invention is illustrated by the following examples. The examples are intended 5 for illustration only and the present invention is not any way limited by the examples.
Example 1
Phospholopids (3 kg) were loaded to the reactor that was described above. Then 10 the reactor was sealed and the process started. The current frequency was 50 Hz.
After saponification reaction mixture was acidulated with hydrochloric acid to pH below 4. Free fatty acids were immediately separated as a top layer.
The residue after hydrolysis was saponificated again, no free fatty acids were detected. That proved the completeness of the saponification.
The control sample was treated in the same way without application of an electric current. No free fatty acids were separated.
The process parameters are listed in the table below.
Time, hr: min | Current, A | Voltage, 11!!!!!!!! | Power, Wt | Temperature |||i|l|||||| | Pressure, barg | Notes |
00:00:00 | 0.0 | 0.0 | 0.0 | 49 | 0.00 | Reactor loading |
00:01:00 | 24.1 | 51.0 | 1229.1 | 49 | 0.00 | Start |
00:02:00 | 28.0 | 49.1 | 1374.8 | 58 | 0.00 | |
00:03:00 | 28.8 | 47.9 | 1379.5 | 58 | 0.00 | |
00:04:00 | 26.2 | 47.9 | 1255.0 | 59 | 0.00 | Reactor full |
00:05:00 | 30.0 | 51.7 | 1551.0 | 55 | 0.00 | Manual voltage control |
00:06:00 | 34.0 | 49.8 | 1693.2 | 56 | 0.00 | |
00:07:00 | 33.3 | 53.1 | 1768.2 | 62 | 0.00 |
00:08:00 | 29.0 | 56.0 | 1624.0 | 66 | 0.00 | Manual voltage control |
00:09:00 | 29.0 | 56.0 | 1624.0 | 72 | 0.00 | |
00:10:00 | 0.0 | 0.0 | 0.0 | 89 | 0.00 | Stopping |
00:11:00 | 0.0 | 0.0 | 0.0 | |||
00:12:00 | 0.0 | 0.0 | 0.0 | Start | ||
00:13:00 | 50.0 | 49.1 | 2455.0 | 73 | 0.00 | |
00:14:00 | 47.7 | 49.8 | 2375.5 | 76 | 0.00 | |
00:15:00 | 44.4 | 50.8 | 2255.5 | 79 | 0.00 | |
00:16:00 | 43.5 | 51.7 | 2249.0 | 88 | 0.80 | |
00:17:00 | 41.2 | 51.9 | 2138.3 | 101 | 1.80 | |
00:18:00 | 42.8 | 51.2 | 2191.4 | 111 | 2.80 | |
00:19:00 | 43.2 | 51.0 | 2203.2 | 120 | 3.60 | |
00:20:00 | 41.9 | 51.7 | 2166.2 | 126 | 4.00 | |
00:21:00 | 40.0 | 51.6 | 2064.0 | 127 | 4.40 | |
00:22:00 | 0.0 | 0.0 | 0.0 | 130 | 2.80 | |
00:23:00 | 30.0 | 46.0 | 1380.0 | 133 | 4.50 | |
00:24:00 | 0.0 | 138 | Stopping | |||
00:25:00 | 45.0 | 51.0 | 2295.0 | 136 | 4.00 | Start |
00:26:00 | 33.0 | 47.0 | 1551.0 | 138 | 5.00 | |
00:27:00 | 0.0 | 139 | 4.30 |
Example 2
Soapstock (3 kg) was loaded to the reactor that was described above. Then the 5 reactor was sealed and the process started. The current frequency was 60 Hz.
After saponification reaction mixture was acidulated with sulphuric acid to pH below 4. Free fatty acids were immediately separated as a top layer.
The residue after hydrolysis was saponificated again, no free fatty acids were detected. That proved the completeness of the saponification.
The process parameters are listed in the table below.
Time, hr: min | Current, A | Voltage, V | Power, Wt | Temperature OC | Pressure, barg | Notes |
00:00:00 | 41.0 | 18.0 | 738.0 | 33 | 0.00 | |
00:01:00 | 42.5 | 12.5 | 531.3 | 33 | 0.00 | |
00:02:00 | 43.0 | 11.9 | 511.7 | 35 | 0.00 | |
00:03:00 | 43.1 | 11.3 | 487.0 | 38 | 0.00 | |
00:04:00 | 43.2 | 11.0 | 475.2 | 40 | 0.00 | |
00:05:00 | 43.3 | 10.6 | 459.0 | 42 | 0.00 | |
00:06:00 | 43.4 | 10.5 | 455.7 | 43 | 0.00 | |
00:07:00 | 43.5 | 10.3 | 448.1 | 44 | 0.00 | |
00:08:00 | 43.4 | 10.0 | 434.0 | 46 | 0.00 | |
00:09:00 | 43.4 | 9.8 | 425.3 | 48 | 0.00 | |
00:10:00 | 43.4 | 9.7 | 421.0 | 50 | 0.00 | |
00:11:00 | 43.4 | 9.6 | 416.6 | 51 | 0.00 | |
00:12:00 | 43.5 | 9.4 | 408.9 | 52 | 0.00 | |
00:13:00 | 43.5 | 9.3 | 404.6 | 54 | 0.00 | |
00:14:00 | 43.5 | 9.2 | 400.2 | 55 | 0.00 | |
00:15:00 | 43.5 | 9.1 | 395.9 | 56 | 0.00 | |
00:16:00 | 43.5 | 9.0 | 391.5 | 57 | 0.00 | |
00:17:00 | 43.6 | 8.9 | 388.0 | 58 | 0.00 | |
00:18:00 | 43.7 | 8.8 | 384.6 | 60 | 0.00 | |
00:19:00 | 43.6 | 8.7 | 379.3 | 61 | 0.10 | |
00:20:00 | 43.7 | 8.6 | 375.8 | 62 | 0.30 | |
00:21:00 | 43.7 | 8.4 | 367.1 | 63 | 0.40 | |
00:22:00 | 43.6 | 8.4 | 366.2 | 64 | 0.40 | |
00:23:00 | 43.6 | 8.3 | 361.9 | 65 | 0.50 | |
00:24:00 | 43.8 | 8.3 | 363.5 | 66 | 0.60 | |
00:25:00 | 44.0 | 8.3 | 365.2 | 68 | 0,,7 | |
00:26:00 | 43.8 | 8.3 | 363.5 | 69 | 0.70 | |
00:27:00 | 43.6 | 8.2 | 357.5 | 71 | 0.80 |
00:28:00 | 43.6 | 8.1 | 353.2 | 72 | 0.90 | |
00:29:00 | 43.6 | 8.1 | 353.2 | 72 | 0.90 | |
00:30:00 | 43.7 | 8.0 | 349.6 | 72 | 0.90 | |
00:31:00 | 43.6 | 8.0 | 348.8 | 73 | 1.00 | |
00:32:00 | 43.4 | 7.9 | 342.9 | 75 | 1.10 | |
00:33:00 | 43.7 | 7.9 | 345.2 | 76 | 1.10 | |
00:34:00 | 43.5 | 7.8 | 339.3 | 77 | 1.20 | |
00:35:00 | 43.7 | 7.8 | 340.9 | 78 | 1.20 | |
00:36:00 | 43.5 | 7.8 | 339.3 | 79 | 1.30 | |
00:37:00 | 43.6 | 7.7 | 335.7 | 80 | 1.30 | Taking first sample and acidulation |
00:38:00 | 43.5 | 8.4 | 365.4 | 81 | 0.60 | |
00:39:00 | 43.5 | 8.4 | 365.4 | 82 | 0.60 | |
00:40:00 | 43.2 | 9.0 | 388.8 | 82 | 0.50 | Second sample, alkalinisation |
00:41:00 | 43.2 | 9.0 | 388.8 | 83 | 0.50 | |
00:42:00 | 43.3 | 8.9 | 385.4 | 85 | 0.50 | |
00:43:00 | 43.3 | 8.8 | 381.0 | 87 | 0.50 | |
00:44:00 | 43.3 | 8.8 | 381.0 | 88 | 0.50 | |
00:45:00 | 43.4 | 8.8 | 381.9 | 89 | 0.50 | |
00:46:00 | 43.2 | 8.6 | 371.5 | 91 | 0.50 | |
00:47:00 | 43.3 | 8.6 | 372.4 | 92 | 0.50 | |
00:48:00 | 43.4 | 8.5 | 368.9 | 93 | 0.60 | |
00:49:00 | 43.3 | 8.5 | 368.1 | 93 | 0.60 | |
00:50:00 | 43.2 | 8.4 | 362.9 | 94 | 0.70 | |
00:51:00 | 43.2 | 8.4 | 362.9 | 95 | 0.70 | |
00:52:00 | 45.2 | 8.3 | 375.2 | 96 | 0.75 | |
00:53:00 | 45.2 | 8.3 | 375.2 | 97 | 0.80 | |
00:54:00 | 45.8 | 8.2 | 375.6 | 98 | 0.90 | |
00:55:00 | 44.1 | 8.2 | 361.6 | 98 | 0.90 | |
00:56:00 | 44.0 | 8.2 | 360.8 | 99 | 1.00 |
00:57:00 | 44.1 | 8.1 | 357.2 | 100 | 1.00 | |
00:58:00 | 44.1 | 8.5 | 374.9 | 101 | 0.95 | Third sample |
00:59:00 | 44.1 | 8.4 | 370.4 | 101 | 0.95 | |
01:00:00 | 44.1 | 8.4 | 370.4 | 102 | 1.00 | |
01:01:00 | 44.1 | 8.4 | 370.4 | 103 | 1.00 | |
01:02:00 | 44.1 | 8.4 | 370.4 | 104 | 1.00 | |
01:03:00 | 44.0 | 8.4 | 369.6 | 105 | 1.00 | |
01:04:00 | 44.0 | 8.3 | 365.2 | 105 | 1.00 | |
01:05:00 | 44.1 | 8.3 | 366.0 | 106 | 1.10 | |
01:06:00 | 44.0 | 8.3 | 365.2 | 107 | 1.10 | |
01:07:00 | 44.1 | 8.2 | 361.6 | 108 | 1.15 | |
01:08:00 | 44.0 | 8.2 | 360.8 | 108 | 1.15 | |
01:09:00 | 44.0 | 8.2 | 360.8 | 109 | 1.20 | |
01:10:00 | 43.9 | 8.1 | 355.6 | 110 | 1.20 | |
01:11:00 | 43.5 | 8.1 | 352.4 | 110 | 1.20 | |
01:12:00 | 43.3 | 8.0 | 346.4 | 111 | 1.25 | |
01:13:00 | 43.4 | 8.0 | 347.2 | 111 | 1.30 | |
01:14:00 | 43.9 | 8.0 | 351.2 | 112 | 1.30 | |
01:15:00 | 43.8 | 8.0 | 350.4 | 113 | 1.35 | |
01:16:00 | 43.9 | 8.0 | 351.2 | 113 | 1.35 | |
01:17:00 | 43.8 | 8.0 | 350.4 | 114 | 1.40 | |
01:18:00 | 44.0 | 8.0 | 352.0 | 114 | 1.40 | |
01:19:00 | 44.3 | 7.9 | 350.0 | 115 | 1.40 | |
01:20:00 | 44.1 | 7.9 | 348.4 | 115 | 1.40 | |
01:21:00 | 44.4 | 7.9 | 350.8 | 116 | 1.50 | |
01:22:00 | 44.3 | 7.9 | 350.0 | 116 | 1.50 | |
01:23:00 | 44.4 | 7.9 | 350.8 | 117 | 1.50 | |
01:24:00 | 44.3 | 7.9 | 350.0 | 117 | 1.50 | |
01:25:00 | 44.3 | 7.9 | 350.0 | 118 | 1.55 | |
01:26:00 | 44.3 | 7.8 | 345.5 | 118 | 1.55 |
01:27:00 | 44.2 | 7.8 | 344.8 | 119 | 1.66 | |
01:28:00 | 44.2 | 7.8 | 344.8 | 119 | 1.60 | |
01:29:00 | 44.2 | 7.8 | 344.8 | 120 | 1.60 | |
01:30:00 | 44.2 | 7.8 | 344.8 | 120 | 1.65 | Fourth sample |
01:31:00 | 0.0 | End |
Claims (9)
1. A process for production of free fatty acids from saponifiable materials; i.e. soapstocks, gums, phospholipids, black liquor soaps or tall oil soaps, the process
5 comprising:
adjusting pH of a saponifiable material to a value above pH 7 by adding alkaline material;
saponifying all saponifiable material by passing alternate electrical current through the material, wherein the said step of saponification occurs in a saponification
10 reactor;
acidulating the saponified material by adding acid to pH value below 4;
isolating obtained free fatty acids from aqueous layer.
2. A process as specified in claim 1, wherein saponification is carried in a pH 15 range of 7.5 - 10, preferably 7.9 - 8.9.
3. A process as specified in claims 1 and 2 or claim 2, wherein saponification occurs in a temperature range of 70 °C - 160 °C,
20
4. A process as specified in claims 3, wherein saponification occurs in pressure range 1 - 6 bara.
5. A process as specified in claims 1 - 4, wherein the frequency of an alternative electric current is in the range 30 Hz to 10,000 Hz, preferable from about 50 to about 60 Hz.
5
6. A process as described in claims 1-5, wherein acidulation occurs at pH range 3-6, preferably 4.5 - 5.5.
7. A process as described in claims 1 - 6, wherein acidulation agent is hydrochloric acid or sulphuric acid.
8. A process as specified in claims 1 - 7, wherein the saponification is carried out in a continuous mode.
9. A process as specified in claim 1, wherein the saponification reactor is an 15 ohmic heater.
Intellectual
Property
Office
Application No: GB1714542.6
9. A process as specified in claim 1, wherein the saponification reactor is an 15 ohmic heater.
10. A saponification reactor comprising at least two electrodes contained within a cylindrical vessel having inlet and outlet ports at opposite ends;
wherein one electrode is electrically and mechanically connected with the vessel 20 wall and is a neutral point connected to earth;
wherein the second electrode is electrically isolated from the first electrode and is connected to a single phase of an electric power supply.
11. A reactor as specified in claim 10; wherein the neutral electrode connected to earth is a tube made of an electrically conductive material; wherein the second electrode is a hollow tube or a rod of a smaller diameter made of an electrically conductive material and affixed along the reactor axis.
12. A reactor as specified in claims 10 and 11; wherein electrically conductive material is graphite.
13. A reactor assembly comprising three reactors as in claim 10, wherein the 10 three saponification reactors are arranged in parallel, wherein the second electrode of each saponification reactor is connected to a different phase of an electric power supply.
14. A reactor assembly comprising three reactors as in claim 10, wherein the 15 three saponification reactors are arranged in series;
wherein the second electrode of each saponification reactor is connected to a different phase of an electric power supply.
Amendment to Claims have been filed as follows
11 06 18
1. A process for production of free fatty acids from saponifiable materials; i.e. soapstocks, gums, phospholipids, black liquor soaps or tall oil soaps, the process
5 comprising:
adjusting pH of a saponifiable material to a value above pH 7 by adding alkaline material;
saponifying all saponifiable material by passing alternate electrical current through the material, wherein the said step of saponification occurs in a saponification
10 reactor;
acidulating the saponified material by adding acid to pH value below 4;
isolating obtained free fatty acids from aqueous layer.
2. A process as specified in claim 1, wherein saponification is carried in a pH 15 range of 7.5 - 10, preferably 7.9 - 8.9.
3. A process as specified in claims 1 and 2 or claim 2, wherein saponification occurs in a temperature range of 70 °C - 160 °C,
20 4. A process as specified in claims 3, wherein saponification occurs in pressure range 1 - 6 bara.
11 06 18
5. A process as specified in claims 1 - 4, wherein the frequency of an alternative electric current is in the range 30 Hz to 10,000 Hz, preferable from about 50 to about 60 Hz.
5 6. A process as described in claims 1-5, wherein acidulation occurs at pH range 3-6, preferably 4.5 - 5.5.
7. A process as described in claims 1 - 6, wherein acidulation agent is hydrochloric acid or sulphuric acid.
8. A process as specified in claims 1 - 7, wherein the saponification is carried out in a continuous mode.
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB1809592.7A GB2563151B (en) | 2017-09-10 | 2017-09-10 | Reactor for the production of fatty acids |
GB1714542.6A GB2558977B8 (en) | 2017-09-10 | 2017-09-10 | Method for production of fatty acids |
PCT/EP2018/074236 WO2019048655A1 (en) | 2017-09-10 | 2018-09-08 | Method for production of fatty acids |
EP18811711.3A EP3759202A1 (en) | 2017-09-10 | 2018-09-08 | Method for production of fatty acids |
US16/641,246 US11377621B2 (en) | 2017-09-10 | 2018-09-08 | Method for production of fatty acids |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB1714542.6A GB2558977B8 (en) | 2017-09-10 | 2017-09-10 | Method for production of fatty acids |
Publications (4)
Publication Number | Publication Date |
---|---|
GB201714542D0 GB201714542D0 (en) | 2017-10-25 |
GB2558977A true GB2558977A (en) | 2018-07-25 |
GB2558977B GB2558977B (en) | 2019-01-16 |
GB2558977B8 GB2558977B8 (en) | 2019-02-20 |
Family
ID=60117367
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB1714542.6A Expired - Fee Related GB2558977B8 (en) | 2017-09-10 | 2017-09-10 | Method for production of fatty acids |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP3759202A1 (en) |
GB (1) | GB2558977B8 (en) |
WO (1) | WO2019048655A1 (en) |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3708513A (en) * | 1970-11-13 | 1973-01-02 | Stepan Chemical Co | Method of synthesizing fatty acids |
US4118407A (en) * | 1977-01-06 | 1978-10-03 | Scm Corporation | Fatty acid recovery from soapstock |
US9546342B1 (en) * | 2015-03-19 | 2017-01-17 | Inveture Renewables, Inc. | Complete saponification and acidulation of natural oil processing byproducts |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5164480A (en) * | 1991-08-20 | 1992-11-17 | Union Camp Corporation | Method for the manufacture of tall oils |
WO2005046861A2 (en) * | 2003-11-12 | 2005-05-26 | Ecr Technologies, Inc. | Chemical synthesis with a strong electrical field |
-
2017
- 2017-09-10 GB GB1714542.6A patent/GB2558977B8/en not_active Expired - Fee Related
-
2018
- 2018-09-08 WO PCT/EP2018/074236 patent/WO2019048655A1/en unknown
- 2018-09-08 EP EP18811711.3A patent/EP3759202A1/en not_active Withdrawn
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3708513A (en) * | 1970-11-13 | 1973-01-02 | Stepan Chemical Co | Method of synthesizing fatty acids |
US4118407A (en) * | 1977-01-06 | 1978-10-03 | Scm Corporation | Fatty acid recovery from soapstock |
US9546342B1 (en) * | 2015-03-19 | 2017-01-17 | Inveture Renewables, Inc. | Complete saponification and acidulation of natural oil processing byproducts |
Also Published As
Publication number | Publication date |
---|---|
WO2019048655A1 (en) | 2019-03-14 |
GB2558977B (en) | 2019-01-16 |
GB2558977B8 (en) | 2019-02-20 |
EP3759202A1 (en) | 2021-01-06 |
GB201714542D0 (en) | 2017-10-25 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US9546342B1 (en) | Complete saponification and acidulation of natural oil processing byproducts | |
US20200291327A1 (en) | Methods for making free fatty acids from soaps using thermal hydrolysis followed by acidification | |
Khot et al. | Lipid recovery from oleaginous yeasts: perspectives and challenges for industrial applications | |
US7998225B2 (en) | Methods of purifying biodiesel fuels | |
Leung et al. | A review on biodiesel production using catalyzed transesterification | |
WO2008120223A2 (en) | An integrated process for the preparation of fatty acid methyl ester (biodiesel) | |
US6426423B1 (en) | Methods for treating phosphatide-containing mixtures | |
CN101056985B (en) | Soapstock biodiesel | |
CN101565654A (en) | Method for producing acidification oil by using oil footings and/or soapstocks | |
US10975328B2 (en) | Methods for making free fatty acids and fatty acid derivatives from mixed lipid feedstocks or soapstocks | |
US11377621B2 (en) | Method for production of fatty acids | |
Echim et al. | Production of biodiesel from side-stream refining products | |
GB2558977A (en) | Method for production of fatty acids | |
US8435766B2 (en) | Enzymatic oil recuperation process | |
US20240124785A1 (en) | Method for the removal of chlorine from fats, oils and greases | |
JP2009242777A (en) | Method for producing fatty acid lower alkyl ester | |
US20090036705A1 (en) | Production of Alkyl Esters from High Fatty Acid Feedstocks | |
JP5620818B2 (en) | Process for producing fatty acids and fatty acid esters | |
KR20190088287A (en) | Method for Separating Biodiesel Raw Oil, Heavy Oil and Cutting Oil Using Animal Waste Oil | |
GB2458709A (en) | Centrifugal separation process for refining triglyceride oils | |
CN212894624U (en) | Large-batch refining system of vegetable insulating oil for transformer | |
US10988708B2 (en) | Systems and methods for fatty acid alkyl ester production with recycling | |
BRPI1000113B1 (en) | process for de-emulsification and integrated esterification of fatty acids and their derivatives using residual reagents and simultaneous alcohol recovery and water withdrawal | |
WO2008140432A1 (en) | A process for removal of free fatty acids from vegetable oils | |
Verhé et al. | Production of biofuel from lipids and alternative resources |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 20230910 |