WO2009017389A2 - Procédé d'extraction d'huile de palme brute - Google Patents

Procédé d'extraction d'huile de palme brute Download PDF

Info

Publication number
WO2009017389A2
WO2009017389A2 PCT/MY2008/000076 MY2008000076W WO2009017389A2 WO 2009017389 A2 WO2009017389 A2 WO 2009017389A2 MY 2008000076 W MY2008000076 W MY 2008000076W WO 2009017389 A2 WO2009017389 A2 WO 2009017389A2
Authority
WO
WIPO (PCT)
Prior art keywords
oil
sludge
phase
decanter
liquor
Prior art date
Application number
PCT/MY2008/000076
Other languages
English (en)
Other versions
WO2009017389A3 (fr
Inventor
Sivasothy Kandiah
Ramachandran Batumalai
Original Assignee
Malaysian Palm Oil Board
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Malaysian Palm Oil Board filed Critical Malaysian Palm Oil Board
Publication of WO2009017389A2 publication Critical patent/WO2009017389A2/fr
Publication of WO2009017389A3 publication Critical patent/WO2009017389A3/fr

Links

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
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/06—Production of fats or fatty oils from raw materials by pressing

Definitions

  • the present invention relates to a method for extracting crude palm oil from oil palm fresh fruit bunches and more particularly to a crude palm oil extraction method for reducing the amount of effluent discharged compared to the prior art methods.
  • Fresh fruit bunches (FFB) 1 are cooked during sterilization 2 using steam at a pressure of 3 bar in horizontal autoclaves of cylindrical shape for about 60 to 90 minutes.
  • the sterilized fruit bunches 3 are then stripped 4 to separate the sterilized fruits from the empty fruit bunches.
  • the sterilized fruits 5 are then reheated and agitated in steam-heated vessels known as digesters 6 to loosen the mesocarp from the nuts in preparation for pressing 7.
  • the screw press expels a liquor of oil, water and finely divided solids, and a press cake of fibre and nuts.
  • the oil in the press liquor has to be separated from the water and solids and this takes place during clarification.
  • the primary separation is achieved in settling tanks using gravity.
  • the diluted press liquor is then screened 9 to remove the coarse fibrous solids 20 that are subsequently returned to the digesters 6.
  • the screened and diluted press liquor 10 is then heated and pumped into the clarification tank 11 where it separates into two phases, i.e. oil 12 and sludge 16.
  • the separation is carried out using either horizontal or vertical continuous clarifiers.
  • the horizontal clarifier is a long rectangular tank partitioned into three or more compartments along its length. A retention time of about two hours is normally used.
  • the cylindrical vertical clarifier is preferred in most modern palm oil mills. Dimensions of this tank have been significantly increased to allow a sludge retention time of about four to five hours, and stirrers with shear plates have also been fitted to improve the oil/ sludge separation efficiency.
  • the oil layer 12 in the clarification tank is skimmed off and passed to centrifugal purifier 13 which reduces the dirt content to 0.01 percent or less.
  • the centrifuged oil is then dried in vacuum drier 14 to give a product of crude palm oil 15 with a moisture content of approximately 0.1 percent.
  • Sludge 16 from the clarification tank has approximately 4 to 10 percent oil, the bulk of which can be recovered using centrifugal separator 18 after desander 17 leaving substantially de-oiled sludge 19.
  • the oil recovered by the sludge centrifuge i.e. the centrifugal separator 18 contains some water and dirt and is therefore returned to the clarification tank 11 for further treatment.
  • Two types of sludge centrifuge are currently used. The first is the stacked disk centrifuge. This centrifuge can handle a much larger capacity and its operation is quite easily automated. The second centrifuge uses a star-shaped rotating bowl. In spite of its smaller capacity, this centrifuge is still popular because of its lower capital and maintenance costs.
  • the conventional milling process generates about 0.6 tons of palm oil mill effluent
  • POME for every ton of FFB processed.
  • Malaysia produced about 42 million tons of POME from about 400 palm oil mills.
  • BOD biological oxygen demand
  • the biological oxygen demand (BOD) of the POME discharged from all palm oil mills in Malaysia had a population equivalent of about 62 million people (i.e., approximately 2.5 times the population of Malaysia).
  • BOD biological oxygen demand
  • Silting of ponds due to the high concentration of suspended solids reduces their effectiveness and leads to higher operating cost.
  • POME treatment under anaerobic conditions also leads to the emission of methane (i.e., a greenhouse gas that has a global warming effect that is 21 times more potent than carbon dioxide).
  • a decanter consists of a cylindrical-conical shaped bowl equipped with a screw conveyor rotating at a speed slightly different from that of the bowl.
  • the cylindrical section of the bowl is used for clarification of liquids or separation of two immiscible liquid phases, while the conical section is suitable fof drying of the separated solids.
  • the feed slurry enters the machine through a feed pipe into a feed zone in the centre of the conveyor.
  • centrifugal force causes feed material to pass through a series of feed ports to the bowl where it forms an annular layer. Within this layer, the solid particles of greater specific gravity than the liquid are sedimented under the high centrifugal force.
  • the clarified liquid is built up and to overflow over adjustable weirs at the cylindrical end of the bowl.
  • Action of the screw conveyor which rotates in the same direction as the bowl but at a slightly slower speed, conveys the sedimented solids in the opposite direction out of the liquid layer (i.e., drying zone or beach) and through discharge ports at the conical end of the bowl.
  • a three-phase decanter allows two immiscible liquid phases with different densities to be separated and discharged from the cylindrical end of the bowl, while the sedimented solids are discharged from the conical end.
  • Two-phase decanters have primarily been used in palm oil mills for separating out the suspended solids, which may subsequently be dried using a rotary drier. It is claimed that up to
  • 70 percent of the suspended solids and 20 percent of the dissolved solids can be separated by the decanter. Installing them prior to oil clarification leads to reduction in the amount of water needed to facilitate oil clarification. Nevertheless, they are normally used for treating the underflow from the clarification tank since this leads to lower oil loss in the cake. No significant reduction in the amount of POME is achievable in the latter case, since water is still needed to facilitate oil settling in the clarification tank.
  • three-phase decanter makes possible oil clarification and separation of the suspended solids concurrently. If press liquor is used as the feed to a three-phase decanter, it is possible to replace both the clarification tank and sludge centrifuge. This not only reduces the amount of water needed to facilitate oil clarification significantly, but also greatly simplifies the clarification process. Nevertheless, the oil loss was observed to be higher than with the conventional process.
  • three-phase decanters are normally used in large capacity mills, with or without sludge separators, for treating the underflow from the clarification tank. As in the case of two-phase decanters, no significant reduction in the amount of POME is achievable since primary oil/sludge separation using clarification tanks is still needed.
  • the POME from mills using the new extraction process can possibly be dried or co-composted with empty fruit bunches.
  • palm oil mills will be made more environmentally-friendly.
  • the above objectives are achieved in the present invention by providing a method for extracting crude palm oil from the press liquor obtained from FFB that comprises the steps of firstly removing the coarse fibrous solids and sand in the said press liquor to form a clean press liquor, secondly reducing the moisture content of the clean press liquor to form a concentrated liquor, and thirdly clarifying the concentrated liquor into a sludge phase and an oil phase for further processing to obtain crude palm oil.
  • the feature that characterizes the novelty of the invention is the second step, where the moisture content of the clean press liquor is reduced using an evaporator prior to clarification in the third step.
  • the concentrated liquor from the evaporator is clarified using a clarification system that is capable of achieving the separation of oil from sludge without water addition and without significantly increasing the oil loss from the clarification process compared to the prior art methods.
  • a clarification system that is capable of achieving the separation of oil from sludge without water addition and without significantly increasing the oil loss from the clarification process compared to the prior art methods.
  • a plurality of evaporators or any other suitable moisture-extracting system that is capable of reducing the moisture content of the liquor expelled by screw presses may be used in step two of this invention.
  • the method thereof may be adapted for FFB that may be sterilized using either the conventional batch sterilization process or the patented continuous sterilization process (Malaysian Patent Number MY-121530-A) or any other suitable sterilization process.
  • the amount of effluent produced by the continuous sterilization process is significantly less than the batch sterilization process.
  • Much of the effluent from a conventional mill is due to heating up of the sterilizer vessels and cages during the start-up of each batch sterilization cycle.
  • the continuous sterilization process is not subjected to the heating-cooling cycle typical of the batch sterilization process, and is therefore preferred for significantly reducing the quantity of effluent discharged.
  • At least one multiple-effect evaporator system is used to remove moisture from the press liquor prior to oil clarification.
  • the presence of a significant quantity of oil in the press liquor makes possible the use of a multiple-effect evaporator system to remove moisture using a fraction of the energy required by a drier system to remove an equal amount of moisture from POME, especially if heated air is used to supply the energy for drying.
  • Evaporation of moisture from the press liquor according to the present invention provides a number of advantages compared to evaporation of moisture from POME as proposed in a prior art method.
  • the presence of approximately 50 percent oil in the feed to the evaporator ensures that the evaporated liquor does not become viscous. Fouling of evaporator tubes will be significantly less, even if a large percentage of the moisture in the feed is removed.
  • the quantity of moisture to be removed from the undiluted press liquor is significantly less than the quantity of moisture to be removed from raw POME in a conventional mill.
  • the overall energy demand of the new oil extraction process can probably be met using just fibre and shell as the energy sources, making it unnecessary to burn the empty fruit bunches.
  • Removing moisture from the press liquor may also help to minimize the formation of the third layer that inhibits oil/sludge separation during the oil clarification process.
  • the separation of oil from sludge is achieved using a clarification system that can process the viscous liquor after evaporation without water addition.
  • a clarification system that can process the viscous liquor after evaporation without water addition.
  • the bulk of the oil can be separated quite easily using a settling tank or a decanter.
  • the decanter may be a two-phase decanter or a three-phase decanter.
  • a decanter makes possible the use of very high g-force to achieve the separation of oil from sludge. If a significant amount of the moisture in the feed to the decanter still exists as free moisture, a decanter with no drying zone can be used, similar in design to that used in a prior art method, for facilitating the oil/sludge separation without water addition using just one processing step.
  • the sludge phase from the oil/ sludge separation step has a low oil content, it is discharged directly as effluent, otherwise it undergoes further treatment using an oil recovery step before it is discharged. To minimize the quantity of effluent, this separation is also achieved without water addition. The actual method used will depend on the moisture content of the sludge.
  • the oil in the sludge from either the oil/ sludge separation step or the oil recovery step can be recovered by drying the sludge to a low enough moisture content to facilitate using a solvent extraction process.
  • a portion of the oil phase from the oil/ sludge separation step may be recycled back to the evaporator system to increase the oil content of the feed to minimize fouling of the evaporator tubes.
  • Figure 1 illustrates schematically the conventional crude palm oil extraction process using oil palm fresh fruit bunches as the feed.
  • Figure 2 illustrates one embodiment of the present invention using undiluted press liquor as the feed.
  • Figure 3 illustrates another embodiment of the present invention that facilitates the recovery of the residual oil in the sludge by solvent extraction.
  • Figure 4 illustrates the integration of the first embodiment of the present invention with the batch sterilization process.
  • Figure 5 illustrates the integration of the first embodiment of the present invention with the continuous sterilization process.
  • the liquor 51 expelled from screw presses is first fed to screening means 52 as illustrated in Figure 2 to remove the coarse fibrous solids 52a that are subsequently recycled.
  • the screened liquor is heated to approximately 95°C and fed to desanding means 53, such as a cyclone desanding system, for sand (53a) removal before it enters evaporation means 54 as clean press liquor (53b).
  • Evaporation means 54 is used to reduce the moisture content of the liquor expelled by the screw presses.
  • a multiple-effect falling film evaporator is preferably used as this evaporator has high heat transfer coefficients and can operate at small driving forces, and is less susceptible to scaling. It also permits very short product contact times, typically just a few seconds per pass.
  • a multiple-effect forced circulation evaporator may also be used for this purpose.
  • the liquor 55 from evaporation means 54 is stored in a holding tank, which also serves as the feed tank for oil/sludge separation means 56. The contents of this tank are agitated to keep the product homogenous. This is achieved by an agitator or by direct steam injection. It is essential that the product fed to oil/sludge separation means 56 has a temperature of approximately 95° C.
  • the liquor 55 from evaporation means 54 is clarified using a zero-dilution clarification process.
  • the bulk of the oil can be separated without water addition using oil/sludge separation means 56. This separation can be achieved by gravity using a settling tank or by centrifugal force using either a two-phase or a three-phase decanter. If the moisture content of the feed is high, much of the recoverable oil can be separated using a two-phase decanter with no drying zone, similar in design to that used in a prior art method, and no further treatment of sludge phase 61 to recover oil will be required.
  • sludge phase 61 from oil/ sludge separation means 56 contains oil that is recoverable, it is further treated using oil recovery means 62 before it is discharged as effluent.
  • This oil recovery is also achieved without water addition using a two-phase decanter, a three-phase decanter, a rotary press, a membrane filter press or other equipment that can be used to achieve a similar objective.
  • a screw press may be used if sludge phase 61 can first be mixed with fibre from the kernel extraction process.
  • the oil 63 recovered by oil recovery means 62 will most likely be contaminated with water and solids, and is therefore recycled back to oil/ sludge separation means 56 for further processing.
  • the sludge phase 61 or 64 respectively from either the oil/ sludge separation means 56 or the oil recovery means 62 may be dried using drying means 65 as shown in Figure 3 to a moisture content of less than 15 percent and the oil in dried sludge 66 extracted by solvent extraction means 67 to produce dried and de-oiled sludge 68.
  • the oil phase 57 from oil/ sludge separation means 56 is discharged into a holding tank and is further processed using purification means 58 to remove traces of dirt in the oil to form a purified oil phase (58a) that is subsequently dried using drying means 59 to obtain crude palm oil (60).
  • Figure 4 illustrates how the present invention can be integrated with the rest of the milling process in a conventional palm oil mill, where sterilization is carried out using the batch sterilization process.
  • the FFB 30 are cooked during the sterilization process 31 using steam at a pressure of 3 bar in horizontal autoclaves of cylindrical shape for about 60 to 90 minutes.
  • a large amount of condensate is formed (i.e., approximately 20 percent of the FFB processed) and must be removed from sterilization process 31 if it is not to interfere with the heat transfer during sterilization. All or a portion of this condensate may be mixed with feed 51 to screening means 52.
  • the sterilized fruit bunches 32 are sent to stripper 33.
  • the objective of stripping is to separate the sterilized fruits from the empty fruit bunches.
  • the sterilized fruits 34 from stripper 33 are reheated to loosen the mesocarp from the nuts in preparation for pressing. This is carried out in the steam-heated digesters 35.
  • Digesters commonly used are vertical cylindrical vessels with rotating shafts to which are attached stirring arms. These arms agitate the fruits, loosening the mesocarp from the nuts and, at the same time, breaking open as many of the oil cells as possible.
  • the temperature of the digested fruit must be close to 100 0 C, which can be achieved by fitting the digester with a steam jacket or using live steam injection or a combination of both.
  • the screw press 36 consists essentially of a perforated cage in which runs either one or two screws. Cones restrict the discharge from the cage, and it is this restriction that creates pressure in the cage and thus controls the amount of de-oiling of the digested fruit mesh.
  • the screw press 36 expels liquor 51 consisting of oil, water and finely divided solids, and a press cake of fibre and nuts. The press liquor 51 is subjected to further processing using the present invention as described earlier.
  • the amount of POME is reduced to less than 0.4 tonnes per tonne of FFB processed by combining the batch sterilization process with the new oil extraction process.
  • Figure 5 illustrates how the present invention can be integrated with the patented continuous sterilization process.
  • FFB 40 is first disrupted using double-roll crusher 41.
  • the crushed bunches 42 are heated using live steam at low pressure during sterilization process 43 to facilitate continuous processing.
  • the sterilization process 43 is carried out using steam at low or atmospheric pressure, the process significantly improves the strippability of bunches compared to the batch sterilization process.
  • the amount of condensate discharged by the continuous sterilization process 43 is significantly lower than the batch sterilization process. This is because the continuous sterilization process is not subjected to the heating-cooling cycle typical of the batch sterilization process. Also, the bulk of the sterilizer condensate is trapped and discharged with bunches from the continuous sterilizer and is eventually discharged from the mill with the sludge from the clarification process.
  • the extent of cooking achieved by the continuous sterilization process 43 is insufficient to optimize the oil and kernel extraction by the rest of the milling process.
  • the fruits from the continuous sterilization process 43 are therefore further heated after stripping 45 using post-heating process 47.
  • Digestion 49 is carried out using either the conventional vertical digester described above or a new horizontal digester.
  • the fruits are heated and agitated during digestion to loosen the mesocarp from the nuts and to break open the oil cells to facilitate oil recovery during pressing.
  • the main advantage of using the horizontal digester is a slightly lower oil loss in the press cake due to improved drainage from the digester.
  • the press liquor 51 is subjected to further processing using the present invention as described earlier.
  • the amount of POME discharged from the palm oil milling process can be reduced to less than 0.3 tons per ton of FFB processed in a mill using the continuous sterilization and the new crude oil extraction processes.

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)
  • Fats And Perfumes (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Abstract

L'invention concerne un procédé pour extraire de l'huile de palme brute à partir de grappes de fruits frais qui consiste à éliminer une partie de l'humidité dans la liqueur de presse (51) par évaporation (54) puis à procéder à une clarification de l'huile (56) au moyen d'un système pouvant assurer la séparation huile/boue sans ajout d'eau pour réduire l'effluent produit par le procédé d'extraction d'huile de palme.
PCT/MY2008/000076 2007-08-01 2008-07-31 Procédé d'extraction d'huile de palme brute WO2009017389A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
MYPI20071265 MY144226A (en) 2007-08-01 2007-08-01 Method for extracting crude palm oil
MYPI20071265 2007-08-01

Publications (2)

Publication Number Publication Date
WO2009017389A2 true WO2009017389A2 (fr) 2009-02-05
WO2009017389A3 WO2009017389A3 (fr) 2009-04-09

Family

ID=40305074

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/MY2008/000076 WO2009017389A2 (fr) 2007-08-01 2008-07-31 Procédé d'extraction d'huile de palme brute

Country Status (3)

Country Link
CO (1) CO6541507A2 (fr)
MY (1) MY144226A (fr)
WO (1) WO2009017389A2 (fr)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010101454A2 (fr) * 2009-03-04 2010-09-10 Malaysian Palm Oil Board Procédé d'extraction d'huile de palme par évaporation
WO2012096561A2 (fr) * 2011-01-10 2012-07-19 Low Teck Yin Procédé d'extraction d'huile de palme
WO2012167789A3 (fr) * 2011-06-10 2013-04-25 Steeper Energy Aps Procédé et appareil pour la production d'hydrocarbure liquide
WO2015037980A1 (fr) * 2013-09-10 2015-03-19 Malaysian Palm Oil Board Procédé de clarification d'huile de palme à zéro décharge liquide
WO2015190907A1 (fr) * 2014-06-10 2015-12-17 Palmite Process Engineering Sdn Bhd Procédé d'extraction d'huile de palme brute au moyen d'une technologie verte
WO2016129986A3 (fr) * 2015-02-10 2016-12-01 Ngan Teng Ye Procédé de traitement des effluents produits par le processus d'extraction de l'huile de palme
WO2017182667A1 (fr) * 2016-04-22 2017-10-26 Novozymes A/S Extraction d'huile assistée par enzyme utilisant un condensat de stérilisateur
WO2017183955A1 (fr) * 2016-04-19 2017-10-26 Liew Shun Bin @ Andrew Shun Bin Système de récupération de pétrole par élimination de matières solides pour le traitement des boues brutes d'un moulin à huile de palme et des raffineries associées, et procédé de traitement utilisant ledit système
WO2018067001A3 (fr) * 2016-10-06 2018-10-18 Liew Shun Bin @ Andrew Shun Bin Système de récupération d'huile par élimination de matières solides (srors), avec modules de filtration raccordés en parallèle, pour le traitement des boues brutes d'un moulin à huile de palme et des raffineries associées et procédé utilisant ledit srors
WO2018206827A1 (fr) * 2017-05-10 2018-11-15 Gea Westfalia Separator Ibérica, S.A. Dispositif et procédé pour le traitement continu d'un produit alimentaire
CN110981066A (zh) * 2019-12-23 2020-04-10 深圳市源禹环保科技有限公司 一种含钼酸铵废水回收处理工艺方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5039455A (en) * 1989-07-31 1991-08-13 Kooi Boon Lam Process for continuous extraction of palm oil or vegetable edible oil
WO2000041976A1 (fr) * 1999-01-14 2000-07-20 Ebara Engineering Singapore Pte Ltd. Systeme de traitement d'effluent d'usine de trituration d'huile de palme
WO2007038963A1 (fr) * 2005-10-05 2007-04-12 Flottweg Gmbh & Co. Kgaa Processus et dispositif destinés à produire de l'huile de palme ou de l'huile végétale

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5039455A (en) * 1989-07-31 1991-08-13 Kooi Boon Lam Process for continuous extraction of palm oil or vegetable edible oil
WO2000041976A1 (fr) * 1999-01-14 2000-07-20 Ebara Engineering Singapore Pte Ltd. Systeme de traitement d'effluent d'usine de trituration d'huile de palme
WO2007038963A1 (fr) * 2005-10-05 2007-04-12 Flottweg Gmbh & Co. Kgaa Processus et dispositif destinés à produire de l'huile de palme ou de l'huile végétale

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010101454A3 (fr) * 2009-03-04 2010-12-09 Malaysian Palm Oil Board Procédé d'extraction d'huile de palme par évaporation
WO2010101454A2 (fr) * 2009-03-04 2010-09-10 Malaysian Palm Oil Board Procédé d'extraction d'huile de palme par évaporation
WO2012096561A2 (fr) * 2011-01-10 2012-07-19 Low Teck Yin Procédé d'extraction d'huile de palme
WO2012096561A3 (fr) * 2011-01-10 2012-11-29 Low Teck Yin Procédé d'extraction d'huile de palme
US9777223B2 (en) 2011-06-10 2017-10-03 Steeper Energy Aps Process and apparatus for producing liquid hydrocarbon
WO2012167789A3 (fr) * 2011-06-10 2013-04-25 Steeper Energy Aps Procédé et appareil pour la production d'hydrocarbure liquide
WO2015037980A1 (fr) * 2013-09-10 2015-03-19 Malaysian Palm Oil Board Procédé de clarification d'huile de palme à zéro décharge liquide
WO2015190907A1 (fr) * 2014-06-10 2015-12-17 Palmite Process Engineering Sdn Bhd Procédé d'extraction d'huile de palme brute au moyen d'une technologie verte
WO2016129986A3 (fr) * 2015-02-10 2016-12-01 Ngan Teng Ye Procédé de traitement des effluents produits par le processus d'extraction de l'huile de palme
WO2017183955A1 (fr) * 2016-04-19 2017-10-26 Liew Shun Bin @ Andrew Shun Bin Système de récupération de pétrole par élimination de matières solides pour le traitement des boues brutes d'un moulin à huile de palme et des raffineries associées, et procédé de traitement utilisant ledit système
WO2017182667A1 (fr) * 2016-04-22 2017-10-26 Novozymes A/S Extraction d'huile assistée par enzyme utilisant un condensat de stérilisateur
WO2017182665A1 (fr) * 2016-04-22 2017-10-26 Novozymes A/S Extraction d'huile de palme à l'aide d'enzymes et d'un stérilisateur continu
WO2018067001A3 (fr) * 2016-10-06 2018-10-18 Liew Shun Bin @ Andrew Shun Bin Système de récupération d'huile par élimination de matières solides (srors), avec modules de filtration raccordés en parallèle, pour le traitement des boues brutes d'un moulin à huile de palme et des raffineries associées et procédé utilisant ledit srors
WO2018206827A1 (fr) * 2017-05-10 2018-11-15 Gea Westfalia Separator Ibérica, S.A. Dispositif et procédé pour le traitement continu d'un produit alimentaire
CN110981066A (zh) * 2019-12-23 2020-04-10 深圳市源禹环保科技有限公司 一种含钼酸铵废水回收处理工艺方法

Also Published As

Publication number Publication date
MY144226A (en) 2011-08-15
CO6541507A2 (es) 2012-10-16
WO2009017389A3 (fr) 2009-04-09

Similar Documents

Publication Publication Date Title
WO2009017389A2 (fr) Procédé d'extraction d'huile de palme brute
WO2010101454A2 (fr) Procédé d'extraction d'huile de palme par évaporation
US8168037B2 (en) Method and systems for enhancing oil recovery from ethanol production byproducts
KR101142928B1 (ko) 음식물 쓰레기 탈리액으로부터 유분 및 슬러지를 분리하는 장치
JP2016520093A (ja) 前処理ありのフェルラ酸の最適化抽出方法
US20090126719A1 (en) Method for processing sugar cane filter cake mud and extracting component products
WO2007038963A1 (fr) Processus et dispositif destinés à produire de l'huile de palme ou de l'huile végétale
EP2519620B1 (fr) Procédé pour procésser de fractions concentrées de savon à l'huile de pin à partir d'un mélange de liqueur noire et de savon à l'huile de pin provenant d'une methode de traitement sulphatée dans une usine de pâte à papier
WO2019216757A1 (fr) Appareil d'extraction d'huile intégré pour stériliser, digérer et presser des fruits égrapés de palmier à huile
US4039348A (en) Treatment of raw sugar juice
US4063960A (en) Treatment of sugar cane
CN101845038B (zh) 丙交酯精制残液处理方法及装置
US9394503B2 (en) Separation process of oil and sugars from biomass
WO2006099456A1 (fr) Methode de recuperation de l'huile a partir de sous-produits du mais et sous-systeme apparente (ii)
US3325308A (en) Process for the refining of sugar with two or more solvents
EP2600954B1 (fr) Procédé de purification d'huiles végétales par élimination des matières solides par centrifugation au stade du miscella
WO2015037980A1 (fr) Procédé de clarification d'huile de palme à zéro décharge liquide
BR122018076810B1 (pt) Método para remoção de água do efluente produzido a partir do processo de moagem de óleo de palma
EP3230422A1 (fr) Procédé et système de lavage d'un savon d'huile de pin brut
JP7254928B2 (ja) 低脂肪製品を産出する方法および低脂肪製品を産出するためのシステム
RU2779646C1 (ru) Способ получения обезжиренного продукта и система получения обезжиренного продукта
CN101239898A (zh) 使用一种高效脱水过滤机制备纯度达99.98重量%以上的纯对苯二甲酸的方法
WO2015190907A1 (fr) Procédé d'extraction d'huile de palme brute au moyen d'une technologie verte
KR20230158137A (ko) 음식물 폐기물 처리 시스템 및 방법
EP3956424A1 (fr) Procédé industriel pour entretenir la production d'huile d'olive vierge par conversion de constituants de fruit d'olivier en produits commercialisables: eau, solide déshydraté et huile d'olive vierge

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08793793

Country of ref document: EP

Kind code of ref document: A2

NENP Non-entry into the national phase in:

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: 10023927

Country of ref document: CO

122 Ep: pct application non-entry in european phase

Ref document number: 08793793

Country of ref document: EP

Kind code of ref document: A2