CA2063929A1 - Process for the continuous removal of a gum phase from triglyceride oil - Google Patents
Process for the continuous removal of a gum phase from triglyceride oilInfo
- Publication number
- CA2063929A1 CA2063929A1 CA002063929A CA2063929A CA2063929A1 CA 2063929 A1 CA2063929 A1 CA 2063929A1 CA 002063929 A CA002063929 A CA 002063929A CA 2063929 A CA2063929 A CA 2063929A CA 2063929 A1 CA2063929 A1 CA 2063929A1
- Authority
- CA
- Canada
- Prior art keywords
- oil
- stage
- gum phase
- centrifugal separator
- gum
- 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.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims abstract description 46
- UFTFJSFQGQCHQW-UHFFFAOYSA-N triformin Chemical compound O=COCC(OC=O)COC=O UFTFJSFQGQCHQW-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 238000005406 washing Methods 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 239000002253 acid Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 6
- 231100000252 nontoxic Toxicity 0.000 claims description 3
- 230000003000 nontoxic effect Effects 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 2
- 238000005119 centrifugation Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 101
- 235000019198 oils Nutrition 0.000 description 101
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 22
- 235000014786 phosphorus Nutrition 0.000 description 20
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 19
- 229910052698 phosphorus Inorganic materials 0.000 description 19
- 239000011574 phosphorus Substances 0.000 description 19
- 229910052742 iron Inorganic materials 0.000 description 11
- 238000004061 bleaching Methods 0.000 description 8
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 235000019484 Rapeseed oil Nutrition 0.000 description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 238000001637 plasma atomic emission spectroscopy Methods 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- 235000012424 soybean oil Nutrition 0.000 description 2
- 239000003549 soybean oil Substances 0.000 description 2
- 235000015112 vegetable and seed oil Nutrition 0.000 description 2
- 239000008158 vegetable oil Substances 0.000 description 2
- 101100352919 Caenorhabditis elegans ppm-2 gene Proteins 0.000 description 1
- 235000019482 Palm oil Nutrition 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000010775 animal oil Substances 0.000 description 1
- 239000011260 aqueous acid Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000727 fraction Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 235000014593 oils and fats Nutrition 0.000 description 1
- 210000002741 palatine tonsil Anatomy 0.000 description 1
- 239000002540 palm oil Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 150000003626 triacylglycerols Chemical class 0.000 description 1
Classifications
-
- 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
- C11B3/00—Refining fats or fatty oils
- C11B3/006—Refining fats or fatty oils by extraction
-
- 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
- C11B3/00—Refining fats or fatty oils
- C11B3/16—Refining fats or fatty oils by mechanical means
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Microbiology (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Fats And Perfumes (AREA)
- Peptides Or Proteins (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Centrifugal Separators (AREA)
- Treatment Of Liquids With Adsorbents In General (AREA)
Abstract
ABSTRACT
Process for the continuous removal of a gum phase from triglyc-eride oil comprising a) centrifugatian of the oil containing a separate gum phase in a first centrifugal separator to yield a gum phase with minimal oil content and oil that still contains a fraction of the gums originally present in the feed; b) mixing into the oil obtained from the first centrifugal separator an amount of washing water and optionally passing said mixture to a holding vessel; c) centrifugation of said mixture in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a rather high oil content; and d) recycling said wet gum phase into the oil stream fed to the first centrifugal separator.
Process for the continuous removal of a gum phase from triglyc-eride oil comprising a) centrifugatian of the oil containing a separate gum phase in a first centrifugal separator to yield a gum phase with minimal oil content and oil that still contains a fraction of the gums originally present in the feed; b) mixing into the oil obtained from the first centrifugal separator an amount of washing water and optionally passing said mixture to a holding vessel; c) centrifugation of said mixture in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a rather high oil content; and d) recycling said wet gum phase into the oil stream fed to the first centrifugal separator.
Description
PRn OESS FOR THK CONTINUOUS RKMO~AI OF A
GUM PHAS~ FROM TRIGLYCERIDK OIL
5 R~ n-n~ f t~ nvf~n1.~ nn The present invention relates to a process for the continuous removal ot a gum phase from triglyceride oil resulting in a gum phase with low oil content and a degummed oil which after bleaching may be physically refined The present process com-prises the following stages a) in a first stage the oil containing a separate gum phase is subjected to centrifugal çeparation in a first centri-lS fugal separator to yield a gum phase with minimal oil contentand an oil that still contains a fraction of the gums originally present in the feeds b) in a econd stage an amount of washing water is mixed into the oil obtained from the first centrifugal separator, which mixture i5 optionally passed to a holding vessel;
c) in a third stage the mixture obtained at stage b) is subjected to centrifugal separation in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a much higher oil content than the gum phase obtained at stage a~;
d) in a fourth stage the wet gum phase obtained at stage c) is recycled into the oil stream fed to the first centrifugal separator Crùd- triglycerid- oils as obtain-d by pr---ino and/or ~tract-ing oil s--ds or anlmal matt-r contaln sev-ral compounds other than triglycerides Some ot these compounds such as phos-phatides, fre- fatty acids, odours, colouring matter, wa~es and metal compounds must be removed because they adversely affect taste, smell, appearance and keepability of the refined oil Several processe6 for the removal of these unwanted compound~
are known and frequently discussed in the literature process for the continuous removal of a gum phase from triglyceride oil is described in EP O 348 004 This process involves in a first stage degumming the oil by any conventional degumming method causing phosphatides to be hydrated, and, in a second stage, separating the undissolved and originally non-centrifugable parti~les from the degummed oil after optionalagglomeration, by microfiltration, filtration, centrifugation, sedimentation or decantation. The main disadvantage of this process is the important 105s of triglyceride oil entrained S during removal of both gum phases.
~nother process for the continuous removal of a separate gum phase from triglyceride oil is described in EP 34~ 71~. In a first stage of this process, the oil containing a separate gum phase is subjected to centrifugal separation to yield gums with minimal oil content and an oil that still contains a fraction of the gums originally present in the feed. In a second stage of this process, the oil obtained from the first stage is subjected to a second centrifugal separation to yield oil with a minimum residual gum content and a gum phase with a much higher oil content than the gums obtained in the first stage, which gums are recycled as such. This recycling results in a decreased loss of triglyceride oil.
Finally, if sale of degummed oil and thus a low phosphorus content i5 aimed at, one or more washing stages are recommended, because the oil leaving the second centrifugal separator still has a phosphorus content that is consldered to be unduly high.
These washing stages require additional centritugal separators and cause an effluent stream, and accordingly incr-ase invest-ment and processing costs.
Therefore it is an object of the invention to provide an alternative process for the continuous removal of a gum pha--from triglyceride oil re-ulting in gums with low oil content and degummed oil with low phosphorus cont-nt.
It is an additional object of the invention to provide a procefis for the continuous removal of a gum phase from trlglyceride oil, which process does not entail high investment and processing costs.
It is also an obiect of the invention to provide a process for the continuous removal of a gum phase from triglyceride oil, avoiding polluting effluents.
These and other objects and advantages of the invention will become apparent as the description of the invention proceeds.
~tAA.i~P~l ~lPfu~r~ n ~1 t.hP 1nY~nt.lnn The invention relates to a process for the continuous removal ot a gum phase from triglyceride oil resulting in a gum phase with low oil content and a degummed oil which after bleaching may be physically refined.
The process according to the invention i5 a process for the continuous removal of a gum phase from triglyceride oil, comprising the following stages:
a~ in a first stage the oil containing a separate gum phase is subiected to centrifugal separation in a first centri-fugal separator to yield a gum phase with minimal oil content lS and an oil that still contains a fraction of the gums originally present in the feed~
b) in a second stage an amount of washing water is mixed into the oil obtalned from the first centrifugal separator, which mixture is optionally passed to a holding vessel;
c) in a third stage the mixture obtained at stage b) is subjected to centrifugal separation in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a much higher oil content than the gum phase obtained at stage a), and d) in a fourth stage the wet gum phase obtained at stage c) is recycled into the oil stream fed to the first centrifugal separator.
It has surprisingly been found, that mi~ing an amount of washing water into the oil obtained from the first centrituyal s~parator prior to being fed to th- second c-ntrifugal separator do~- not affect triglyceride oil content o~ the gum phase leaving the first centritugal separator. It has also surprisingly been found that this additional amount of water does not affect the water content of the oil leaving the second centrifugal separator, in that the first centrifugal separator can effectively remove the additional amount of water that has been recycled together with the gum phase from the second centrifugal separator. This additional amount of water further causes the oil obtained from the second centrifugal separator to have a much lower phosphorus content.
2063~29 It has also been found, that a usual amount of bleaching earth is required for bleaching the oil obtained according to the present invention, to provide bleached oils having a phosphorus level which is consi~ered to be acceptable s It is thus an advantage of the process according to the inven-tion over the process disclosed in EP 0 349 71~ that one or both washing stages can be omitted, as a result of which loss of triglyceride oil entrained during these washing stages, effluent problems and investments in washing centrifuges are avoided In order that the invention may be fully understood, the accom-panying figure schematically represents a process line The process according to the invention can advantageously be used in the degumming process according to US 41~98,185 In this process water degummed vegetable oils are treated with finely dispersed aqueous acid whereupon this acid is partially neutralised 50 that a gum phase is formed If such oils containing a gum phase are processod according to the present invention, the oils thus obtained may be physically refined Similarly the process according to the invention can advantageously be applied to degum oils treated by the process according to G~ 1 5~5 569 This process entails adding an acid to crude oil, allowing a contact time of approximately 10 min~, partially neutralising this acid with a base and then allowing an extended contact time for the development of a separate gum phase which is finally to be removed from the oil The process according to the invention can also advantageously b- appli-d to d-gum oils treated by th- process according to US
4,049,~5~ In ~S 4,049,~8~ a proce-- ls d-scrib-d ln which oil is treated with an acid and coolQd to b-low 40 C wh-reupon thR
nonhydratabl- phospholipids form gums in a form that can be removed from the oil e g by centrifuge The type of oil to be degumm-d by the process according to the invention is not critical Thus edible triglyceride oils like soyb-an oil, suntlowerseed oil, rapese-d oil, palm oil and other vegetable oils as well as animal oils and fats can all be successfully processed provided the gum phase has been success-tully developed betore the oil is fed to the first centrifugal separator The washing water to be mixed into the oil obtained from the first centrifugal separator can be water, diluted non-toxic acid, e.g. citric acid, water containing salts or effluent water resulting from the optional washing stage.
The amount of washing water to be mixed into the oil leaving the first centrifugal separator generally ranges from O.OS to 10 wt.%, preferably between 0.5 and 5 wt.%.
The oil - washing water mixture is then optionally passed to a holding vessel. This holding time generally ranges from 10 seconds to 30 minutes, preferably from 0.5 to 15 minutes. The temperature in said holding vessel is preferably between ~0 and 110 C.
The centrifugal separators to be used in the process according to the invention can be disc centrituges, decanters or other lS equipment capable of continuously separating a gum phase from an oil phase. The performance of such equipment can commonly be adjusted to yield either a gum stream with low oil content or an oil stream with low gum content as set out in EP 349 71~.
The oil phase obtained by the process according to the invention may further be dried and bleachQd with commonly known bleaching means prior to being physically refined or refined by alkali neutralisation.
The invention i5 now illustrated by the following examples.
E~a~pl e ' In this example the continuous removal of a gum pha~e ~rom triglyceride oil according to the invention is illustrated.
The feed consisted of water-degummed oybean oil having temperature of approximat-ly 90-C, a r-sidual phosphorus content of approximately 120 ppm and an iron cont-nt of approxlmately 1.15 ppm. The,~eparate gum phaGe was formed according to US
4,~9S,185 applying 0.20 vol.-/. phosphoric acid of 80 ~. strength, a contact time equal to 2.5 min. (at a throughput of 9.3 tons/h,) and a S0 /. neutralization of the phosphoric acid with 12-~ caustic soda, The soybean oil comprising a eparatQ gum phase was, in the first stage of the process according to the invention, fed to a centrifugal separator, resulting into a gum phase having a triglyceride oil content of approximately 19 wt./. (calculated on dry matter) and triglyceride oil which still contained a fraction of the phosphatides originally present in the feed.
7 2~929 Into the oil resulting from the first centrifugal separator, 4.10 % of washing water was mixed, which mixture was passed to a holding vessel and allowed to stand for approximately 2 minutes prior to being fed to the second centrifuge.
During the second centrifugal stage, a wet gum phase was removed from the triglyceride oil, which gum phase was fully recycled into the oil fed to the first centrifugal separator over a second holding vessel, which allowed a holding time of approxi-mately 1 hour. The flow rate of this recycled stream wasestimated at 2,3 tons/h.
In a comparative example, the same soybean oil, in which the separate gum pha~e was formed as mentioned above, was treated by the process according to EP 0 349 71~, including two washing stages.
The quality of the oils at different stages of the processes i5 summarized in table 1. The oils were analysed for phosphorus and iron by plasma emission spectroscopy (~.J. Dijkstra and D.
Meert, J.~.O.C.S. 59 (19~2), 199).
Table _ example 1 ex mple 1 before first centrifugal separator 30 moisture % ~. e~ 2.93 after first centrifugal separator moisture % 0.54 0.~0 phosphorus ppm 2~. e ~4. e 35 iron ppm O.lS 0.17 _ _ _ _ _ before second centrifugal separator moisture % 4.~ O.g9 .
after second centrifugal separator moisture % 0.42 0.42 phosphorus ppm 10.3 37.5 iron ppm 0.15 0.12 ..... _ .
45 after two washing stages moisture % _ 0.53 phosphorus ppm_ 13.3 iron ppm _ 0.10 . . __ 50 after drying phosphorus ppm9.~ 10.0 iron ppm 0.11 0.0 20~3929 The above table clearly illustrates that the residual phosphorus content of the oil resulting from the second centrifugal separa-tor is much lower when operating in accordance to the invention rather than according to EP 0 ~49 718. ~esides, the phosphorus content of the oil obtained according to the invention is about the same as the phosphorus content of the oil obtained according to EP 0 349 718, which process included two washing stages. This example thus illustrates that both washing stages can be omitted when processing in accordance to the invention.
The above table also shows that the moisture content of oil resulting from the second centrifugal separator does not increase when operating in accordance with the invention. It also demonstrates, that the first centrifugal separator is able lS to remove the extra water introduced into the oil at the stage in between the centrifugal separators.
In this example the continuous removal of a gum phase from triglyceride oil according to the invention is illustrated.
The feed consisted of partially water-degummed rapeseed oil having a temperature of approximately 90-C, a residual phospho-rus content of approximately 15e ppm and an iron content of approximately 1.58 ppm. The separate gum phase was formed according to US 4,~98,185 applying 0.1~ vol.% phosphoric acid of 80 /. strength, a contact time equal to 2.5 min. ~at a throughput of 9.0 tons/h.) and a 50 % neutralization of the pho~phoric acid with 12^~e caustic soda.
The rapeseed oil comprising a s-parate gum phase was, in the first stage of the process according to the invention, fed to a centrifugal ~eparator, resulting into a gum phase having a triglyceride oil content of approximately 14 wt.% ~calculated on dry matter) and triglyceride oil which still contained a frac-tion of the phosphatides originally present in the feed.
Into the oil resulting from the first centrifugal separator, 2 %
of washing water was mi~ed, which mixture was passed to a hold-ing vessel and allowed to stand for approximately 2 minutes prior to being fed to the second centrifuge.
During the second centrifugal stage, a wet gum phase was removed from the triglyceride oil, which gum phase was fully recycled into the oil fed to the first centrifugal separator over a 9 2063~29 second holding vessel, which allowed a holding time of approxi-mately 30 minutes. The flow rate of this recycled stream was estimated at 2,4 tons/h.
In a comparative example, the same rapeseed oil, in which the separate gum phase was formed as mentioned above, was treated by the process according to EP 0 349 718, including two washing stages. The oil content of the gum phase obtained by the process according to EP 349 71e was approximately 12.~ % (calculated on dry matter).
The oils thus obtained were bleached with 0.5 wt.% bleaching earth ~ Tonsil ~CCFF, Sud Chemie, Munich, Germany) at lOO-C
under vacuum for ~0 minutes whereupon the oil was allowed to cool to below 90-C before the bleaching earth was filtered off.
Subsequently, the bleached oils were physically refined at 240-C
for 2 hours at a vacuum below 400 Pa (30 mmHg). Soth oils had a bland neutral taste and showed excellent keepability.
The quality of the oils is summarized in table 2. ~gain, the oils were analysed for phosphorus and iron by plasma emission spectroscopy (~.J. Dijkstra and D. Meert, J.~.O.C.S. 59 (1982), 199).
Iahle_Z
example 2 comparative example 2 .
30 after second centrifugal separator phosphorus ppm 13.7 22.4 iron ppm 0.00 0.07 aft-r drying ~S phosphorus ppm 9~2 4.~
iron ppm 0~10 0.10 attor bl-aching with qual amounts of bl-aching earth 40 phosphoru~ ppm 2.9 1.0 iron ppm 0.01 0.01 The above table 2 clearly illustrates that the residual phos-phorus content of the oil resulting from the second centrifugalseparator is much lower when operating in accordance to the invention rather than according to EP 0 ~49 718.
Furthermore, the above table shows that the oil according to the invention can, after drying, be bleached with the usual amount of bleaching earth in order to obtain a high quality refined oil.
GUM PHAS~ FROM TRIGLYCERIDK OIL
5 R~ n-n~ f t~ nvf~n1.~ nn The present invention relates to a process for the continuous removal ot a gum phase from triglyceride oil resulting in a gum phase with low oil content and a degummed oil which after bleaching may be physically refined The present process com-prises the following stages a) in a first stage the oil containing a separate gum phase is subjected to centrifugal çeparation in a first centri-lS fugal separator to yield a gum phase with minimal oil contentand an oil that still contains a fraction of the gums originally present in the feeds b) in a econd stage an amount of washing water is mixed into the oil obtained from the first centrifugal separator, which mixture i5 optionally passed to a holding vessel;
c) in a third stage the mixture obtained at stage b) is subjected to centrifugal separation in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a much higher oil content than the gum phase obtained at stage a~;
d) in a fourth stage the wet gum phase obtained at stage c) is recycled into the oil stream fed to the first centrifugal separator Crùd- triglycerid- oils as obtain-d by pr---ino and/or ~tract-ing oil s--ds or anlmal matt-r contaln sev-ral compounds other than triglycerides Some ot these compounds such as phos-phatides, fre- fatty acids, odours, colouring matter, wa~es and metal compounds must be removed because they adversely affect taste, smell, appearance and keepability of the refined oil Several processe6 for the removal of these unwanted compound~
are known and frequently discussed in the literature process for the continuous removal of a gum phase from triglyceride oil is described in EP O 348 004 This process involves in a first stage degumming the oil by any conventional degumming method causing phosphatides to be hydrated, and, in a second stage, separating the undissolved and originally non-centrifugable parti~les from the degummed oil after optionalagglomeration, by microfiltration, filtration, centrifugation, sedimentation or decantation. The main disadvantage of this process is the important 105s of triglyceride oil entrained S during removal of both gum phases.
~nother process for the continuous removal of a separate gum phase from triglyceride oil is described in EP 34~ 71~. In a first stage of this process, the oil containing a separate gum phase is subjected to centrifugal separation to yield gums with minimal oil content and an oil that still contains a fraction of the gums originally present in the feed. In a second stage of this process, the oil obtained from the first stage is subjected to a second centrifugal separation to yield oil with a minimum residual gum content and a gum phase with a much higher oil content than the gums obtained in the first stage, which gums are recycled as such. This recycling results in a decreased loss of triglyceride oil.
Finally, if sale of degummed oil and thus a low phosphorus content i5 aimed at, one or more washing stages are recommended, because the oil leaving the second centrifugal separator still has a phosphorus content that is consldered to be unduly high.
These washing stages require additional centritugal separators and cause an effluent stream, and accordingly incr-ase invest-ment and processing costs.
Therefore it is an object of the invention to provide an alternative process for the continuous removal of a gum pha--from triglyceride oil re-ulting in gums with low oil content and degummed oil with low phosphorus cont-nt.
It is an additional object of the invention to provide a procefis for the continuous removal of a gum phase from trlglyceride oil, which process does not entail high investment and processing costs.
It is also an obiect of the invention to provide a process for the continuous removal of a gum phase from triglyceride oil, avoiding polluting effluents.
These and other objects and advantages of the invention will become apparent as the description of the invention proceeds.
~tAA.i~P~l ~lPfu~r~ n ~1 t.hP 1nY~nt.lnn The invention relates to a process for the continuous removal ot a gum phase from triglyceride oil resulting in a gum phase with low oil content and a degummed oil which after bleaching may be physically refined.
The process according to the invention i5 a process for the continuous removal of a gum phase from triglyceride oil, comprising the following stages:
a~ in a first stage the oil containing a separate gum phase is subiected to centrifugal separation in a first centri-fugal separator to yield a gum phase with minimal oil content lS and an oil that still contains a fraction of the gums originally present in the feed~
b) in a second stage an amount of washing water is mixed into the oil obtalned from the first centrifugal separator, which mixture is optionally passed to a holding vessel;
c) in a third stage the mixture obtained at stage b) is subjected to centrifugal separation in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a much higher oil content than the gum phase obtained at stage a), and d) in a fourth stage the wet gum phase obtained at stage c) is recycled into the oil stream fed to the first centrifugal separator.
It has surprisingly been found, that mi~ing an amount of washing water into the oil obtained from the first centrituyal s~parator prior to being fed to th- second c-ntrifugal separator do~- not affect triglyceride oil content o~ the gum phase leaving the first centritugal separator. It has also surprisingly been found that this additional amount of water does not affect the water content of the oil leaving the second centrifugal separator, in that the first centrifugal separator can effectively remove the additional amount of water that has been recycled together with the gum phase from the second centrifugal separator. This additional amount of water further causes the oil obtained from the second centrifugal separator to have a much lower phosphorus content.
2063~29 It has also been found, that a usual amount of bleaching earth is required for bleaching the oil obtained according to the present invention, to provide bleached oils having a phosphorus level which is consi~ered to be acceptable s It is thus an advantage of the process according to the inven-tion over the process disclosed in EP 0 349 71~ that one or both washing stages can be omitted, as a result of which loss of triglyceride oil entrained during these washing stages, effluent problems and investments in washing centrifuges are avoided In order that the invention may be fully understood, the accom-panying figure schematically represents a process line The process according to the invention can advantageously be used in the degumming process according to US 41~98,185 In this process water degummed vegetable oils are treated with finely dispersed aqueous acid whereupon this acid is partially neutralised 50 that a gum phase is formed If such oils containing a gum phase are processod according to the present invention, the oils thus obtained may be physically refined Similarly the process according to the invention can advantageously be applied to degum oils treated by the process according to G~ 1 5~5 569 This process entails adding an acid to crude oil, allowing a contact time of approximately 10 min~, partially neutralising this acid with a base and then allowing an extended contact time for the development of a separate gum phase which is finally to be removed from the oil The process according to the invention can also advantageously b- appli-d to d-gum oils treated by th- process according to US
4,049,~5~ In ~S 4,049,~8~ a proce-- ls d-scrib-d ln which oil is treated with an acid and coolQd to b-low 40 C wh-reupon thR
nonhydratabl- phospholipids form gums in a form that can be removed from the oil e g by centrifuge The type of oil to be degumm-d by the process according to the invention is not critical Thus edible triglyceride oils like soyb-an oil, suntlowerseed oil, rapese-d oil, palm oil and other vegetable oils as well as animal oils and fats can all be successfully processed provided the gum phase has been success-tully developed betore the oil is fed to the first centrifugal separator The washing water to be mixed into the oil obtained from the first centrifugal separator can be water, diluted non-toxic acid, e.g. citric acid, water containing salts or effluent water resulting from the optional washing stage.
The amount of washing water to be mixed into the oil leaving the first centrifugal separator generally ranges from O.OS to 10 wt.%, preferably between 0.5 and 5 wt.%.
The oil - washing water mixture is then optionally passed to a holding vessel. This holding time generally ranges from 10 seconds to 30 minutes, preferably from 0.5 to 15 minutes. The temperature in said holding vessel is preferably between ~0 and 110 C.
The centrifugal separators to be used in the process according to the invention can be disc centrituges, decanters or other lS equipment capable of continuously separating a gum phase from an oil phase. The performance of such equipment can commonly be adjusted to yield either a gum stream with low oil content or an oil stream with low gum content as set out in EP 349 71~.
The oil phase obtained by the process according to the invention may further be dried and bleachQd with commonly known bleaching means prior to being physically refined or refined by alkali neutralisation.
The invention i5 now illustrated by the following examples.
E~a~pl e ' In this example the continuous removal of a gum pha~e ~rom triglyceride oil according to the invention is illustrated.
The feed consisted of water-degummed oybean oil having temperature of approximat-ly 90-C, a r-sidual phosphorus content of approximately 120 ppm and an iron cont-nt of approxlmately 1.15 ppm. The,~eparate gum phaGe was formed according to US
4,~9S,185 applying 0.20 vol.-/. phosphoric acid of 80 ~. strength, a contact time equal to 2.5 min. (at a throughput of 9.3 tons/h,) and a S0 /. neutralization of the phosphoric acid with 12-~ caustic soda, The soybean oil comprising a eparatQ gum phase was, in the first stage of the process according to the invention, fed to a centrifugal separator, resulting into a gum phase having a triglyceride oil content of approximately 19 wt./. (calculated on dry matter) and triglyceride oil which still contained a fraction of the phosphatides originally present in the feed.
7 2~929 Into the oil resulting from the first centrifugal separator, 4.10 % of washing water was mixed, which mixture was passed to a holding vessel and allowed to stand for approximately 2 minutes prior to being fed to the second centrifuge.
During the second centrifugal stage, a wet gum phase was removed from the triglyceride oil, which gum phase was fully recycled into the oil fed to the first centrifugal separator over a second holding vessel, which allowed a holding time of approxi-mately 1 hour. The flow rate of this recycled stream wasestimated at 2,3 tons/h.
In a comparative example, the same soybean oil, in which the separate gum pha~e was formed as mentioned above, was treated by the process according to EP 0 349 71~, including two washing stages.
The quality of the oils at different stages of the processes i5 summarized in table 1. The oils were analysed for phosphorus and iron by plasma emission spectroscopy (~.J. Dijkstra and D.
Meert, J.~.O.C.S. 59 (19~2), 199).
Table _ example 1 ex mple 1 before first centrifugal separator 30 moisture % ~. e~ 2.93 after first centrifugal separator moisture % 0.54 0.~0 phosphorus ppm 2~. e ~4. e 35 iron ppm O.lS 0.17 _ _ _ _ _ before second centrifugal separator moisture % 4.~ O.g9 .
after second centrifugal separator moisture % 0.42 0.42 phosphorus ppm 10.3 37.5 iron ppm 0.15 0.12 ..... _ .
45 after two washing stages moisture % _ 0.53 phosphorus ppm_ 13.3 iron ppm _ 0.10 . . __ 50 after drying phosphorus ppm9.~ 10.0 iron ppm 0.11 0.0 20~3929 The above table clearly illustrates that the residual phosphorus content of the oil resulting from the second centrifugal separa-tor is much lower when operating in accordance to the invention rather than according to EP 0 ~49 718. ~esides, the phosphorus content of the oil obtained according to the invention is about the same as the phosphorus content of the oil obtained according to EP 0 349 718, which process included two washing stages. This example thus illustrates that both washing stages can be omitted when processing in accordance to the invention.
The above table also shows that the moisture content of oil resulting from the second centrifugal separator does not increase when operating in accordance with the invention. It also demonstrates, that the first centrifugal separator is able lS to remove the extra water introduced into the oil at the stage in between the centrifugal separators.
In this example the continuous removal of a gum phase from triglyceride oil according to the invention is illustrated.
The feed consisted of partially water-degummed rapeseed oil having a temperature of approximately 90-C, a residual phospho-rus content of approximately 15e ppm and an iron content of approximately 1.58 ppm. The separate gum phase was formed according to US 4,~98,185 applying 0.1~ vol.% phosphoric acid of 80 /. strength, a contact time equal to 2.5 min. ~at a throughput of 9.0 tons/h.) and a 50 % neutralization of the pho~phoric acid with 12^~e caustic soda.
The rapeseed oil comprising a s-parate gum phase was, in the first stage of the process according to the invention, fed to a centrifugal ~eparator, resulting into a gum phase having a triglyceride oil content of approximately 14 wt.% ~calculated on dry matter) and triglyceride oil which still contained a frac-tion of the phosphatides originally present in the feed.
Into the oil resulting from the first centrifugal separator, 2 %
of washing water was mi~ed, which mixture was passed to a hold-ing vessel and allowed to stand for approximately 2 minutes prior to being fed to the second centrifuge.
During the second centrifugal stage, a wet gum phase was removed from the triglyceride oil, which gum phase was fully recycled into the oil fed to the first centrifugal separator over a 9 2063~29 second holding vessel, which allowed a holding time of approxi-mately 30 minutes. The flow rate of this recycled stream was estimated at 2,4 tons/h.
In a comparative example, the same rapeseed oil, in which the separate gum phase was formed as mentioned above, was treated by the process according to EP 0 349 718, including two washing stages. The oil content of the gum phase obtained by the process according to EP 349 71e was approximately 12.~ % (calculated on dry matter).
The oils thus obtained were bleached with 0.5 wt.% bleaching earth ~ Tonsil ~CCFF, Sud Chemie, Munich, Germany) at lOO-C
under vacuum for ~0 minutes whereupon the oil was allowed to cool to below 90-C before the bleaching earth was filtered off.
Subsequently, the bleached oils were physically refined at 240-C
for 2 hours at a vacuum below 400 Pa (30 mmHg). Soth oils had a bland neutral taste and showed excellent keepability.
The quality of the oils is summarized in table 2. ~gain, the oils were analysed for phosphorus and iron by plasma emission spectroscopy (~.J. Dijkstra and D. Meert, J.~.O.C.S. 59 (1982), 199).
Iahle_Z
example 2 comparative example 2 .
30 after second centrifugal separator phosphorus ppm 13.7 22.4 iron ppm 0.00 0.07 aft-r drying ~S phosphorus ppm 9~2 4.~
iron ppm 0~10 0.10 attor bl-aching with qual amounts of bl-aching earth 40 phosphoru~ ppm 2.9 1.0 iron ppm 0.01 0.01 The above table 2 clearly illustrates that the residual phos-phorus content of the oil resulting from the second centrifugalseparator is much lower when operating in accordance to the invention rather than according to EP 0 ~49 718.
Furthermore, the above table shows that the oil according to the invention can, after drying, be bleached with the usual amount of bleaching earth in order to obtain a high quality refined oil.
Claims (9)
1. Process for the continuous removal of a gum phase from triglyceride oil comprising the following stages:
a) in a first stage the oil containing a separate gum phase is subjected to centrifugal separation in a first centrifugal separator to yield a gum phase with minimal oil content and an oil that still contains a fraction of the gums originally present in the feed;
b) in a second stage an amount of washing water is mixed into the oil obtained from the first centrifugal separator, which mixture is optionally passed to a holding vessel;
c) in a third stage the mixture obtained at stage b) is subjected to centrifugal separation in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a much higher oil content than the gum phase obtained at stage a), and d) in a fourth stage the wet gum phase obtained at stage c) is recycled into the oil stream fed to the first centrifugal separator.
a) in a first stage the oil containing a separate gum phase is subjected to centrifugal separation in a first centrifugal separator to yield a gum phase with minimal oil content and an oil that still contains a fraction of the gums originally present in the feed;
b) in a second stage an amount of washing water is mixed into the oil obtained from the first centrifugal separator, which mixture is optionally passed to a holding vessel;
c) in a third stage the mixture obtained at stage b) is subjected to centrifugal separation in a second centrifugal separator to yield oil with a minimum residual gum content and a wet gum phase with a much higher oil content than the gum phase obtained at stage a), and d) in a fourth stage the wet gum phase obtained at stage c) is recycled into the oil stream fed to the first centrifugal separator.
2. Process according to claim 1, characterized in that the amount of washing water added in stage b) ranges from 0.05 to 10 wt.%, preferably from 1 to 5 wt.%.
3. Process according to claims 1 or 2, characterized in that the washing water is selected from the group consisting of water, diluted non-toxic acid and water containing salts
4. Process according to any of the preceding claims, characterized in that the washing water is demineralized water.
5. Process according to any of claims 1 to 3, characterized in that the washing water is diluted non-toxic acid, prefer-ably citric acid.
6. Process according to claims 1 or 2, characterized in that the washing water results from the optional washing stage.
7. Process according to any of the preceding claims, characterized in that the mixture in stage b) is passed through a holding vessel and allowed to stand for 10 seconds to 30 minutes, preferably for 0.5 to 15 minutes.
8. Process according to any of the preceding claims, characterized in that the temperature during the processing ranges between 60 and 110°C, preferably between 80 and 100°C.
9. Degummed oil as obtained according to any of the preceding claims.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP91105198.5 | 1991-04-02 | ||
| EP91105198 | 1991-04-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2063929A1 true CA2063929A1 (en) | 1992-10-03 |
Family
ID=8206595
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002063929A Abandoned CA2063929A1 (en) | 1991-04-02 | 1992-03-25 | Process for the continuous removal of a gum phase from triglyceride oil |
Country Status (13)
| Country | Link |
|---|---|
| EP (1) | EP0507363B1 (en) |
| JP (1) | JPH05117685A (en) |
| AT (1) | ATE89599T1 (en) |
| CA (1) | CA2063929A1 (en) |
| CZ (1) | CZ289672B6 (en) |
| DE (1) | DE69200004T2 (en) |
| DK (1) | DK0507363T3 (en) |
| ES (1) | ES2055634T3 (en) |
| HU (1) | HU212977B (en) |
| MX (1) | MX9201460A (en) |
| PL (1) | PL169760B1 (en) |
| RU (1) | RU2008328C1 (en) |
| SK (1) | SK279220B6 (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0560121A3 (en) * | 1992-03-09 | 1994-07-27 | Vandemoortele Int Nv | Method for refining glyceride oil |
| EP0583648A3 (en) * | 1992-08-19 | 1995-02-01 | Vandemoortele Int Nv | Continuous refining process with reduced waste streams. |
| ID19109A (en) * | 1996-01-05 | 1998-06-18 | Grow Green Pty Ltd | PROTEIN RAW MATERIALS, COMPOSITIONS AND METHODS AND EQUIPMENT TO PRODUCE IT |
| CN1087339C (en) | 1997-07-09 | 2002-07-10 | 结晶及脱胶公司 | Method for eliminating metals from fatty substances and method for binding gus on said metals |
| US6844458B2 (en) | 1998-11-20 | 2005-01-18 | Ip Holdings, L.L.C. | Vegetable oil refining |
| US6426423B1 (en) * | 1998-11-20 | 2002-07-30 | I.P. Holdings | Methods for treating phosphatide-containing mixtures |
| AU2002322233C1 (en) | 2001-07-27 | 2014-02-13 | Aker Biomarine Antarctic As | Natural marine source phospholipids comprising flavonoids, polyunsaturated fatty acids and their applications |
| WO2009132463A1 (en) * | 2008-05-02 | 2009-11-05 | Neptune Technologies & Bioressources Inc. | New deodorization method and organoleptic improvement of marine oil extracts |
| DE102008048009A1 (en) | 2008-09-19 | 2010-03-25 | Rmenergy Umweltverfahrenstechnik Gmbh | Device for decentralized processing of native oils and fat for the utilization as fuel or raw material for producing bio-diesel, has three containers, and three arrangements for feeding reaction starting material into containers |
| AR078850A1 (en) | 2009-10-29 | 2011-12-07 | Acasti Pharma Inc | THERAPEUTIC COMPOSITIONS CONCENTRATED OF PHOSPHOLIPIDS |
| JP6801958B2 (en) * | 2015-12-24 | 2020-12-16 | 日清オイリオグループ株式会社 | Method for producing roasted oil and method for producing edible oil and fat composition |
| CN107011991B (en) * | 2017-04-12 | 2021-04-13 | 西北大学 | A kind of cation resin dephosphorization method of grease |
| WO2021124444A1 (en) * | 2019-12-17 | 2021-06-24 | 株式会社Ｉｈｉ原動機 | Degumming device for crude plant oil |
| WO2021124443A1 (en) * | 2019-12-17 | 2021-06-24 | 株式会社Ｉｈｉ原動機 | Power-generation system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE507650A (en) * | ||||
| GB481580A (en) * | 1935-06-29 | 1938-03-11 | Sharples Specialty Co | Improvements in or relating to the treatment of fatty oils |
| FR1108998A (en) * | 1954-07-10 | 1956-01-19 | Separation Sa Franc Pour La | Improvements in the treatment of vegetable oils |
| MX7580E (en) * | 1981-10-15 | 1989-11-23 | Cpc International Inc | PROCEDURE FOR THE REFINING OF RAW VEGETABLE OILS |
| US4927544A (en) * | 1988-07-06 | 1990-05-22 | N.V. Vandemoortele International | Process for the continuous removal of a gum phase from triglyceride oil |
-
1992
- 1992-02-26 DK DK92200543.4T patent/DK0507363T3/en active
- 1992-02-26 EP EP92200543A patent/EP0507363B1/en not_active Expired - Lifetime
- 1992-02-26 DE DE9292200543T patent/DE69200004T2/en not_active Expired - Lifetime
- 1992-02-26 ES ES92200543T patent/ES2055634T3/en not_active Expired - Lifetime
- 1992-02-26 AT AT92200543T patent/ATE89599T1/en not_active IP Right Cessation
- 1992-03-25 CA CA002063929A patent/CA2063929A1/en not_active Abandoned
- 1992-03-31 MX MX9201460A patent/MX9201460A/en unknown
- 1992-03-31 CZ CS1992957A patent/CZ289672B6/en not_active IP Right Cessation
- 1992-03-31 JP JP4108595A patent/JPH05117685A/en active Pending
- 1992-03-31 SK SK957-92A patent/SK279220B6/en unknown
- 1992-04-01 HU HU9201094A patent/HU212977B/en not_active IP Right Cessation
- 1992-04-01 PL PL92294068A patent/PL169760B1/en unknown
- 1992-04-01 RU SU925011279A patent/RU2008328C1/en active
Also Published As
| Publication number | Publication date |
|---|---|
| PL294068A1 (en) | 1992-12-14 |
| MX9201460A (en) | 1992-10-01 |
| HUT62646A (en) | 1993-05-28 |
| EP0507363A1 (en) | 1992-10-07 |
| ES2055634T3 (en) | 1994-08-16 |
| DK0507363T3 (en) | 1993-08-30 |
| EP0507363B1 (en) | 1993-05-19 |
| CZ289672B6 (en) | 2002-03-13 |
| SK279220B6 (en) | 1998-08-05 |
| CS95792A3 (en) | 1992-10-14 |
| HU212977B (en) | 1997-01-28 |
| HU9201094D0 (en) | 1992-06-29 |
| DE69200004D1 (en) | 1993-06-24 |
| JPH05117685A (en) | 1993-05-14 |
| ATE89599T1 (en) | 1993-06-15 |
| RU2008328C1 (en) | 1994-02-28 |
| PL169760B1 (en) | 1996-08-30 |
| DE69200004T2 (en) | 1993-09-09 |
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| Date | Code | Title | Description |
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| EEER | Examination request | ||
| FZDE | Discontinued |